ppgeq.bib

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@STRING{AIChE = {AIChE Journal}}

@STRING{ATMS = {ACM Transactions on Mathematics and Software}}

@STRING{AUTO = {Automatica}}

@STRING{CCE = {Computers and Chemical Engineering}}

@STRING{CEJ = {Chemical Engineering Journal}}

@STRING{CEP = {Chemical Engineering and Processing}}

@STRING{CES = {Chemical Engineering Science}}

@STRING{CJ = {Computer}}

@STRING{ESCAPE = {ESCAPE}}

@STRING{FC = {Food Control}}

@STRING{IC = {IEEE Computer}}

@STRING{IEC = {Industrial and Engineering Chemistry Fundamentals}}

@STRING{IECR = {Industrial and Engineering Chemistry Research}}

@STRING{IJC = {International Journal of Control}}

@STRING{INME = {International J. for Numerical Methods in Engng.}}

@STRING{JANM = {J. Appl. Num. Math.}}

@STRING{JCAP = {J. Comp. Appl. Math.}}

@STRING{JMP = {J. Math. Phys.}}

@STRING{LAA = {Linear Algebra and its Applications}}

@STRING{NM = {Numerische Mathematik}}

@STRING{PC = {Parallel Computing}}

@STRING{SIAM = {SIAM Journal of Computing}}

@STRING{SJNA = {SIAM J. Numer. Anal.}}

@STRING{SJSC = {SIAM J. Stat. Comp.}}

@STRING{SJSS = {SIAM J. Sci. Stat. Comp.}}

@STRING{TAC = {IEEE Transactions on Automatic Control}}

@STRING{TC = {IEEE Transactions on Computing}}

@STRING{TCS = {IEEE Transactions on Circuits and System}}

@STRING{TCT = {IEEE Transactions on Circuit Theory}}

@STRING{TICE = {Trans. Inst. Chem. Engrs.}}

@STRING{TICS = {IEEE Transactions on CAD of Integrated Circuit Systems}}

@ARTICLE{Alejski:1996,
  author = {Krzysztof Alejski and Françoise Duprat},
  title = {Dynamic Simulation of the Multicomponent Reactive Distillation},
  journal = {Chemical Engineering Science},
  year = {1996},
  volume = {51},
  pages = {4237--4252},
  number = {18},
  abstract = {A dynamic mathematical model of reactive distillation in case of kinetically
	controlled chemical reaction is formulated using four basic assumptions:
	negligible vapour holdup compared to the molar liquid holdup, perfect
	mixing of phases, corrections of equilibrium values by plate efficiency,
	corrections of conversion for mixing effects by "conversion efficiency".
	The accuracy of the dynamic simulation results of reactive distillation
	obtained under different assumptions is verified by comparing with
	results of actual experiments on a pilot-scale distillation column.
	Both the unsteady-state period during start-up and the disturbances
	of continuous operation are considered. Esterification of ethanol
	with acetic acid with sulphuric acid as homogeneous catalyst is chosen
	for experiments. Accuracy of simulation is very good in case of model
	containing hydraulic description of plates with regard to temperatures
	inside column and in the reboiler. Responses of component concentrations
	are less accurate, but imposed disturbances were very large. Observed
	differences result from simplifications of mathematical model, inaccuracy
	of the kinetic and vapour-liquid equilibrium description for highly
	nonideal, multicomponent system and from precision of experimental
	measurements in case of transient state. Differences between experimental
	and simulation results in case of different models are the most significant
	for large holdup on plates in comparison with reboiler. As a general
	rule, in case of reactive distillation simulation for dynamics, description
	models taking into consideration plate hydraulics should be used.},
  comment = {Versão impressa.},
  owner = {Paula},
  pdf = {reactivedistillation/Alejski:1996.pdf},
  timestamp = {2006.09.22}
}

@ARTICLE{Alfradique:2005,
  author = {Marcelo F. Alfradique and Marcelo Castier},
  title = {Modeling and simulation of reactive distillation columns using computer
	algebra},
  journal = {Computers and Chemical Engineering},
  year = {2005},
  volume = {29},
  pages = {1875--1884},
  abstract = {This work presents an extension of a computer algebra (CA) program,
	Thermath, originally developed for the automatic implementation of
	physical property calculations, to generate computer codes in Fortran
	for the simulation of steady-state reactive distillation columns.
	The adopted procedure requires the simultaneous solution, using the
	Newton-Raphson method, of mass and energy balances, phase equilibrium
	equations, chemical equilibrium or rates of reaction equations and
	an additional equation needed to match the number of degrees of freedom.
	The Thermath program was used to obtain Fortran subroutines that
	implement these equations and their derivatives with respect to the
	process variables and the equation of state and/or excess Gibbs free
	energy model used in the simulation. The results are in excellent
	agreement with those available in the literature. By using Thermath,
	it was possible to reduce the time and effort needed to implement
	the mathematical models of multistage reaction-separation equipment.},
  comment = {Apenas versão eletrônica.},
  keywords = {Computer algebra; Reactive distillation; Mathematica; Simulation},
  owner = {Paula},
  pdf = {reactivedistillation/Alfradique:2005.pdf},
  timestamp = {2006.09.22}
}

@PHDTHESIS{Baur:2000_dissertation,
  author = {Richard Baur},
  title = {Modelling Reactive Distillation Dynamics},
  school = {Clarkson University},
  year = {2000},
  comment = {Apenas eletrônica},
  owner = {Paula},
  pdf = {reactivedistillation/Baur:2000_dissertation.pdf},
  timestamp = {2006.09.22}
}

@ARTICLE{Baur:2000,
  author = {R. Baur and A.P. Higler and R. Taylor and R. Krishna},
  title = {Comparison of equilibrium stage and nonequilibrium stage models for
	reactive distillation},
  journal = {Chemical Engineering Journal},
  year = {2000},
  volume = {76},
  pages = {33--47},
  abstract = {For modelling reactive distillation columns, two distinctly different
	approaches are available in the literature: (1) the equilibrium (EQ)
	stage model, in which the vapour and liquid phases are assumed to
	be in thermodynamic equilibrium, and (2) the nonequilibrium (NEQ)
	stage model in which the finite mass transfer rates across the vapour-liquid
	interface are accounted for. In this paper, these two approaches
	are compared using two case studies: (a) synthesis of MTBE and (b)
	hydration of ethylene oxide to ethylene glycol. It is shown that
	while the phenomena of multiple steady states is exhibited by both
	modelling approaches, the "window" in which these multiplicities
	occur is significantly reduced in the NEQ model. It is also shown
	that in actual column design, some of the steady states calculated
	by the EQ model cannot be realised due to e.g. flooding or weeping
	limitations on distillation trays. Another important conclusion that
	can be drawn from this work is that the hardware design can have
	a significant influence on the conversion and selectivity. It is
	concluded that for design of reactive distillation columns we must
	adopt the NEQ modelling approach.},
  comment = {versão eletrônica.},
  keywords = {Reactive distillation; Equilibrium stage model; Nonequilibrium stage
	model; Multiple steady states; Maxwell-Stefan equations; Methyl tert-butyl
	ether synthesis; Ethylene glycol; Tray design},
  owner = {Paula},
  pdf = {reactivedistillation/Baur:2000.pdf},
  timestamp = {2006.09.22}
}

@ARTICLE{Baur:2004,
  author = {R. Baur and R. Krishna},
  title = {Distillation column with reactive pump arounds:an alternative to
	reactive distillation},
  journal = {Chemical Engineering and Processing},
  year = {2004},
  volume = {43},
  pages = {435--445},
  abstract = {The hardware design of reactive distillation (RD) columns pose severe
	challenges with respect to the choice and design of the hardware;
	the requirements of reaction (i.e. high liquid or catalyst holdup)
	is not in consonance with the requirement of separation (high interfacial
	area). In this paper, we examine an alternative to the RD concept,
	namely a distillation column networked with a number of side (external)
	reactors. If each distillation stage is linked to a side reactor,
	the performance of the RD column is matched exactly. From a practical
	point of view, it is desirable to reduce the number of side reactors
	to below, say, six. The precise location of the chosen number of
	side reactors
	
	and the manner in which the liquid draw-offs and reactor effluent
	re-entry to the distillation column needs to be chosen carefully.
	We have developed an algorithm to determine an optimum configuration
	of the side-reactor concept in order to maximise conversion. For
	the case study of methyl acetate production, we see that it is possible
	to match the conversion level of an RD column by appropriate choice
	of the number of side reactors and the pump around ratio. The higher
	the conversion target the larger the number of side reactors and
	pump around ratios. For modest conversion levels, say <90%, even
	a 3-side-reactor configuration will be able to match the performance
	of the RD column. The study presented here reveals the potential,
	and limitations, of the side-reactor concept for use as an alternative
	to RD technology.},
  keywords = {Reactive distillation; Equilibrium stage model; Methyl acetate; Column
	hardware; Hydrodynamics; Mass transfer; Flooding; Side-reactors;
	
	Pump-arounds},
  owner = {Paula},
  pdf = {reactivedistillation/Baur:2004.pdf},
  timestamp = {2006.09.22}
}

@ARTICLE{Baur:2001,
  author = {R. Baur and R. Taylor and R. Krishna},
  title = {Dynamic behaviour of reactive distillation columns described by a
	nonequilibrium stage model},
  journal = {Chemical Engineering Science},
  year = {2001},
  volume = {56},
  pages = {2085--2102},
  abstract = {In this paper we develop a generic, dynamic, nonequilibrium (NEQ)
	stage model for reactive distillation (RD) columns. The main features
	of our model are: (1) use of the Maxwell-Stefan equations for describing
	mass transfer between fluid phases, (2) solid catalysed reactions
	are treated using a pseudo-homogeneous liquid phase model with the
	appropriate pseudo-homogeneous kinetic expressions and (3) a comprehensive
	set of design correlations, for both trays (sieve, bubble caps) and
	packings (random dumped, structured), for hold-up and mass transfer
	have been incorporated into the software package following earlier
	work (Taylor et al., Comput. Chem. Eng. 18 (1994) 205). We report
	some interesting dynamic features of RD columns by examining the
	response of a column for methyl tert-butyl ether (MTBE) synthesis
	to perturbations in the feed of methanol, iso-butene or n-butene.
	When operating at a highconversion branch of the bifurcation diagram,
	small perturbations are shown to lead to a transition to a low-conversion
	branch. The NEQ model is shown to be more susceptible to feed perturbations
	than a conventional equilibrium (EQ) model with constant component
	eficiencies. The di!erences between the dynamic behaviour of trayed
	and random-packed columns are also emphasised in this work. The dynamic
	behaviour of the column has been interpreted on the basis of the
	iso-butene recycle flow in the column. It has been shown that the
	size, type and duration of a feed perturbation causing a transition
	from one to another steady state depends on the model description,
	on the column configuration and on the residence time distribution
	along the column height. Experimental
	
	verification of the developed dynamic model is obtained by comparison
	with the experimental results of Mohl et al. (Chem. Eng. Sci. 54
	(1999) 1029) for synthesis of tertiary amyl ether (TAME).},
  comment = {versão eletrônica.},
  keywords = {Reactive distillation; Equilibrium stage model; Nonequilibrium stage
	model; Multiple steady states; Nonlinear dynamics; Maxwell-Stefan
	
	equations; Methyl tert-butyl ether synthesis},
  owner = {Paula},
  pdf = {reactivedistillation/Baur:2001.pdf},
  timestamp = {2006.09.22}
}

@ARTICLE{Baur:2001a,
  author = {R. Baur and R. Taylor and R. Krishna},
  title = {Dynamic behaviour of reactive distillation tray columns described
	with a nonequilibrium cell model},
  journal = {Chemical Engineering Science},
  year = {2001},
  volume = {56},
  pages = {1721--1729},
  abstract = {In this paper we develop a generic, dynamic, nonequilibrium (NEQ)
	cell model for reactive distillation (RD) tray columns. The features
	of our model are (1) the use of Maxwell-Stefan equations for describing
	mass transfer between fluid phases, (2) the reaction is assumed to
	take place in the liquid phase, both within the di!usion layer and
	in the bulk, (3) the coupling between mass transfer and chemical
	reactions within the di!usion layer is accounted for, and (4) the
	use of multiple well-mixed cells in the liquid and vapour flow directions
	in order to account for staging in either fluid phase. The utility
	of the developed model is demonstrated by carrying out simulations
	of a RD column for production of ethylene glycol (EG) by hydration
	of ethylene oxide. The introduction of staging in the vapour and
	liquid phases improves the conversion to EG and also reduces the
	formation of the unwanted di-ethylene glycol. Furthermore, there
	are marked di!erences between the dynamic column response to feed
	perturbations between the developed NEQ model and the more commonly
	used equilibrium (EQ) stage model.},
  comment = {versão eletrônica.},
  keywords = {Reactive distillation; Equilibrium stage model; Nonequilibrium stage
	model; Dynamics; Maxwell-Stefan equations; Ethylene glycol},
  owner = {Paula},
  pdf = {reactivedistillation/Baur:2001a.pdf},
  timestamp = {2006.09.22}
}

@ARTICLE{Baur:2000a,
  author = {R. Baur and R. Taylor and R. Krishna},
  title = {Development of a dynamic nonequilibrium cell model for reactive distillation
	tray columns},
  journal = {Chemical Engineering Science},
  year = {2000},
  volume = {55},
  pages = {6139--6154},
  abstract = {In this paper we develop a nonequilibrium (NEQ) cell model to describe
	the dynamic operation of reactive distillation (RD) tray columns.
	The features of our model are: (1) use of the Maxwell-Stefan equations
	for describing mass transfer between fluid phases, (2) chemical reactions
	are assumed to take place only in the liquid phase, (3) coupling
	between mass transfer and chemical reactions within the difusion
	layer is accounted for, and (4) the use of multiple well-mixed cells
	in the liquid and vapour flow directions accounts
	
	for staging in either fluid phase. When the chemical reactions are
	suppressed, our model describes the dynamic behaviour of conventional
	distillation columns. We demonstrate the utility of the dynamic NEQ
	cell model by means of three case studies: (1) metathesis of 2-propene
	in an RD column, (2) distillation of methanol-iso-propanol-water,
	and (3) synthesis of methyl tert-butylether (MTBE) in an RD column.
	For comparison purposes we have also carried out dynamic simulations
	using the equilibrium stage (EQ) model. These case studies help us
	to draw the following conclusions. The introduction of staging in
	the liquid and vapour phases not only influences the steady-state
	performance, by increasing reaction conversion and separation capability,
	but also has a significant influence on column dynamics. With multiple
	cells per stage the column dynamics becomes much more sensitive to
	perturbations. Furthermore, we show that even when the NEQ cell model
	and EQ stage model exhibit almost identical steady-state characteristics,
	the dynamic responses of an RD column could even be qualitatively
	diferent. When operating close to the distillation boundary for nonreactive,
	conventional, distillation, small disturbances in feed compositions
	can lead to completely di!erent product compositions.},
  keywords = {Reactive distillation; Equilibrium stage model; Nonequilibrium cell
	model; Multiple steady states; Dynamics; Maxwell-Stefan equations;
	
	Methyl tert-butyl ether synthesis; Metathesis reaction},
  owner = {Paula},
  pdf = {reactivedistillation/Baur:2000a.pdf},
  timestamp = {2006.09.22}
}

@ARTICLE{Benallou:1986,
  author = {A. Benallou and D. E. Seborg and D. A. Mellichamp},
  title = {Dynamic Compartmental Models for Separation Processes},
  journal = {AIChE Journal},
  year = {1986},
  volume = {32},
  pages = {1067--1078},
  comment = {artigo apenas utilizado como referência (apud).},
  owner = {Paula},
  timestamp = {2006.09.02}
}

@ARTICLE{Betlem:2000,
  author = {B. H. L. Betlem},
  title = {Batch distillation column low-order models for quality program control},
  journal = {Chemical Engineering Science},
  year = {2000},
  volume = {55},
  pages = {3187--3194},
  abstract = {For batch distillation, the dynamic composition behaviour can be described
	by the dominant time constant and the bottom exhaustion. Its magnitude
	is determined by the change of the composition distribution and is
	maximal when the inflection point of the molar fraction profile is
	located in the middle of the column. Then, the tray interactions
	are minimal. The distribution change during the batch run strongly
	depends on the applied control strategy. Under constant quality control,
	the dominant time constant proved to be nearly constant whereas under
	constant reflux control the dominant time constant can vary by more
	than a factor of four. To calculate the dominant time constant from
	static design calculations, two di!erent methods are discussed: the
	retention time and the "change of inventory" time method. These methods
	are experimentally verified.},
  comment = {Apenas versão eletrônica.},
  keywords = {Batch distillation; Dominant time constant; Distillation control;
	Distillation modelling},
  owner = {Paula},
  pdf = {distillationColumn/Betlem:2000.pdf},
  timestamp = {2006.08.24}
}

@ARTICLE{Betlem:1998,
  author = {B. H. L. Betlem and J. E. Rijnsdorp and R. F. Azink},
  title = {Influence of tray hydraulics on tray column dynamics},
  journal = {Chemical Engineering Science},
  year = {1998},
  volume = {53},
  pages = {3991--4003},
  number = {23},
  abstract = {To column control, in contrast to column design, tray hold-up and
	dependencies of tray holdup on the operating conditions play an important
	role. The essence of this article is the development of an improved
	model of tray hydraulics over a broad operating range and its experimental
	validation by means of batch distillation. First, the column dynamics
	are related to tray column design parameters and operating conditions.
	The model parameters are fitted by column residence time measurements.
	Two tray load regimes are distinguished: an aeration regime and an
	obstruction regime. At low column load a vapour increase will decrease
	the tray mass since the liquid is driven out by larger aeration.
	At high load the opposite is the case, since the liquid is driven
	up by stowage. The resulting dynamic behaviour is studied by linearising
	the
	
	rigorous tray model in an operating point. Especially the influence
	of the vapour flow on the column dynamics is investigated. For the
	influence of the tray composition change on the molar mass, a new
	composition-shift parameter k is defined. The influence appeared
	to be small.},
  comment = {versão impressa.},
  keywords = {Tray hydraulics; distillation dynamics; column dynamics; column design;
	distillation modelling},
  owner = {Paula},
  pdf = {distillationColumn/Betlem:1998.pdf},
  review = {O artigo apresenta várias equações de hidrodinâmica. É baseado no
	livro de Lockett.
	
	Considera a massa de liquido do downcomer no cálculo da massa total
	do prato. Apresenta outras equações de hidrodinâmica para deixar
	a equação da massa de líquido do prato em função de variáveis simples.},
  timestamp = {2006.08.15}
}

@ARTICLE{Biardi:1989,
  author = {G. Biardi and M. G. Grottoli},
  title = {Development of a new Simulation Model for Real Trays Distillation
	Column},
  journal = CCE,
  year = {1989},
  volume = {13},
  pages = {441--449},
  number = {4/5},
  comment = {Foi adquirido na CIENTEC. Apenas cópia impressa.},
  owner = {Paula},
  review = {Este artigo trata de uma modelagem rigorosa baseada no conceito de
	prato real. Dois aspectos são analisados: a modelagem físico-química
	(transferência de massa e energia) e uma definição de eficiência,
	e a estrutura matemática do modelo para propor um procedimento numérico
	para a solução do sistema.
	
	
	Um "dilema" apresentado é a complexidade de sistema matemático gerado
	quando relações de transferência de massa inter e intrafases são
	adicionadas ao sistema.
	
	
	São listados os motivos pelo qual a modelagem de pratos reais (com
	difusão e convecção de massa) não são utilizadas normalmente na modelagem:
	1) o sistema de equações gerado se torna um problema numérico muito
	pesado e delicado de ser resolvido 2) ainda não há um conhecimento
	consolidado a cerca de simplificações possíveis nesse tipo de modelagem
	de acordo com cada caso a ser modelado. 
	
	
	Foram implementados dois modelo rigorosos para simular colunas de
	destilação multicomponente com pratos reais com diferentes níveis
	de complexidade de detalhamento. O modelo A apresenta uma forma mais
	simples (menos rigorosa) com coeficientes de transferência de massa
	constantes para todos os componentes, um para o lado da fase líquida
	e outro para o lado da fase vapor. O modelo B usa a equação de difusão
	multicomponente de Maxwell-Stefan calculando os coeficiente de difusão
	para ambas as fases através da matriz de coeficientes.
	
	Estes dois modelos coincidem quando não há diferença entre os vários
	coeficientes binários de difusão calculados.
	
	
	Foram utilizados três sistemas para teste e três modelos foram comparados:
	
	- Modelo com pratos de equilíbrio ideais
	
	- Modelo A
	
	- Modelo B
	
	
	Como era de se esperar, o modelo B necessitou de mais tempo computacional.
	Os modelos A e B apresentaram resultados parecidos, ambos com o número
	de estágios necessários maior que o indicado pelo modelo convencional.}
}

@BOOK{Brennan:1989,
  title = {Numerical Solution of Initial Value Problems in Differential-Algebraic
	Equations},
  publisher = {North-Holland},
  year = {1989},
  author = {Brennan, K. E. and Campbell, S. L. and Petzold, L. R. },
  address = {New York}
}

@MASTERSTHESIS{Brooks:1993,
  author = {Braden Alan Brooks},
  title = {Modeling of a Distillation Column using Bond Graphs},
  school = {The University of Arizona},
  year = {1993},
  abstract = {Modeling and simulating distillation columns is not a new enterprise.
	All of the models described in the literature either contain algebraic
	loops or simplifying assumptions that render the model ill-equipped
	for dynamic simulations. The structure and the equations that represent
	a trayed distillation column are explored using bond graphs. Bond
	graphs model the power flow in a system, an inherently instructive
	way to view complex systems. The power of bond graphs is evident
	by providing a clear, graphical representation of a distillation
	column that systematically organizes the equations and possible approximations.
	The model of a distillation column is explored in general and then
	by using a specific model developed by Steven Gallun. Results of
	this study reveal several ways of eliminating the algebraic loops
	and producing a dynamic model. The bond graph model can be expanded
	by introducing other elements including chemical reactions and thermal
	interaction with other columns.},
  comment = {Apenas versão eletrônica.},
  owner = {Paula},
  pdf = {distillationColumn/Brooks:1993.pdf},
  review = {No primeiro capítulo a operação de destilação é explicada. Na página
	14 é apresentada uma definição interessante de componente chave leve.
	
	No capítulo 2, é mostrada a modelagem baseada em equações de coluna
	de destilação.
	
	No capítulo 3 a modelagem via grafos -> ignorei!
	
	Na seção 4.1, as primeiras modelagens de colunas são abordadas.
	
	Na seção 4.2, apresenta o modelo base para a dissertação de Brooks,
	o modelo de Gallun
	
	No capítulo 5, conclusões sobre modelagem de colunas de destilação.},
  timestamp = {2006.08.16}
}

@ARTICLE{Cameron:1986,
  author = {I. T. Cameron and C. A. Ruiz and R. Gani},
  title = {A Generalized Model for Distillation Columns - II - Numerical and
	Computational Aspects},
  journal = CCE,
  year = {1986},
  volume = {10},
  pages = {199--211},
  number = {3},
  comment = {Foi adquirido na CIENTEC. Apenas cópia impressa.},
  owner = {Paula},
  review = {Neste artigo, são discutidos os aspectos numéricos envolvidos na solução
	dos sistemas gerados pela modelagem de colunas de destilação.
	
	São investigados aspectos estruturais do sistema como a esparsidade
	e aspectos de estabilidade como a rigidez.
	
	Duas classes de métodos de discretização são analisadas na solução
	deste sistema: um método BDF (backward-differentiation) e um método
	baseado em um RK (Runge-Kutta) implícito.
	
	
	As conclusões do artigo apontam para o uso do método DIRK em problemas
	onde não é necessário alta precisão e o método BDF onde se prefere
	altas precisões.
	
	
	OBS: Apesar de a modelagem dinâmica gerar um sistema DAE, na época
	em que o artigo foi publicado não existiam solvers para este tipo
	de sistema, apenas solvers para sistemas ODE's.
	
	Assim, o sistema era dividido em variáveis diferenciais (acúmulos
	de massa e energia) e variáveis algébricas (procedures).}
}

@ARTICLE{Carta:1995,
  author = {R. Carta and G. Tola and A. Servida and M. Morbidelli},
  title = {Error analysis of collocation models for steady-state multistage
	separation units},
  journal = {Computers and Chemical Engineering},
  year = {1995},
  volume = {19},
  pages = {123--127},
  number = {1},
  abstract = {The stagewise collocation method is applied to reduce the full-order
	models using for simulate multistage separation units. In particular
	we refer to steady-state, high-puity (xd > 0.9999) and simmetric
	(xb=1-xd) binary distillation columns. The performance of these reduced-order
	models is represented in a master plot wich provides, rather syntetically,
	the model error as a function of the reduction order.},
  comment = {Apenas versão eletrônica.},
  owner = {Paula},
  pdf = {distillationColumn/Carta:1995.pdf},
  review = {Não foi referenciado.},
  timestamp = {2006.08.24}
}

@ARTICLE{Castillo:1998,
  author = {F. J. L. Castillo and G. P. Towler},
  title = {Influence of multicomponent mass transfer on homogeneous azeotropic
	distillation},
  journal = {Chemical Engineering Science},
  year = {1998},
  volume = {53},
  pages = {963--976},
  number = {5},
  comment = {Apenas versão eletrônica.},
  keywords = {Azeotropic distillation; residue curve maps; mass transfer; distillation
	line maps},
  owner = {Paula},
  pdf = {distillationColumn/Castillo:1998.pdf},
  review = {Artigo interessante caso queira saber mais sobre destilação com formação
	de azeótropo. Não li o artigo por inteiro.
	
	Não foi referenciado.},
  timestamp = {2006.08.16}
}

@ARTICLE{Cervantes:1998,
  author = {A. Cervantes and L. T. Biegler},
  title = {Large-Scale DAE Optimization Using a Simultaneous NLP Formulation},
  journal = {AIChE Journal},
  year = {1998},
  volume = {44},
  pages = {1038--1050},
  number = {5},
  month = {May},
  comment = {apenas versão eletrônica.},
  owner = {Paula},
  pdf = {optimization/Cervantes:1998.pdf},
  timestamp = {2007.03.22}
}

@ARTICLE{Chang:1998,
  author = {Byoungmu Chang and Seunghoon Lee and Hyeoktae Kwon and Il Moon},
  title = {Rigorous Industrial Dynamic Simulation of a Crude Distillation Unit
	Considered Valve Tray Rating Parameters},
  journal = {Computers and Chemical Engineering},
  year = {1998},
  volume = {22},
  pages = {S863--S866},
  number = {Suppl.},
  abstract = {A rigorous dynamic simulation is performed to find optimal operating
	conditions of a crude distillation unit with 56 trays and 65,000
	barrel per day capacity. The model includes not only mass and energy
	balance equations but also nonlinear equations capturing the fluid
	behavior in the column such as downcomer load, jet flooding, hole
	velocity limit and downcomer backup. Discrete behavior of pump and
	heater on/off, valve open/close are also included. Hundreds of thousand
	differential algebraic equations(DAEs) are set up and solved by gPROMS
	simultaneously. As a result. the dynamic behavior of the unit during
	the starting and shutdown procedure is fully understood.},
  comment = {Versão impressa.},
  keywords = {Rigorous dynamic simulation, Valve tray rating parameters. Dynamic
	behavior},
  owner = {Paula},
  pdf = {distillationColumn/Chang:1998.pdf},
  review = {A modelagem básica não apresenta novidades...o que difere dos outros
	artigos é a modelagem baseada nas válvulas dos pratos. Nos balanços
	é considerado o arraste de líquido.
	
	Apenas estão presentes as considerações e parâmetros das válvulas
	a serem considerados. Não é apresetando o equacionamento.},
  timestamp = {2006.08.16}
}

@ARTICLE{Cho:1984,
  author = {Y. S. Cho and B. Joseph},
  title = {Reduced order Models for separation Columns - III - Aplication to
	columns with multiple feeds and sidestreams},
  journal = {Computers and Chemical Engineering},
  year = {1984},
  volume = {8},
  pages = {81--90},
  number = {2},
  abstract = {Reduced order dynamic models for distillation columns are developed
	using the polynomial approximation method (orthogonal collocation).
	The discontinuities in column profiles introduced by feeds and sidedraws
	are partially removed through suitable redefinition of variables,
	thus enabling the column profiles to be fitted with a single polynomial
	across the entire column. The strengths and weakness for these reduced
	order models are explored by application studies in multicomponent
	distillation. These included a nonideal system of four components.
	The accuracy and efficiency of the reduced models are also compared
	with simulation results obtained using a dynamic modela developed
	at Monsanto Company.},
  comment = {Apenas verão impressa. Retirado da CIENTEC.},
  owner = {Paula},
  timestamp = {2006.09.04}
}

@ARTICLE{Dave:2003,
  author = {Dhaval J. Dave and Murtuza Z. Dabhiya and S.V.K. Satyadev and Saibal
	Ganguly and Deoki N. Saraf},
  title = {Online tuning of a steady state crude distillation unit model for
	real time applications},
  journal = {Journal of Process Control},
  year = {2003},
  volume = {13},
  pages = {267--282},
  abstract = {The steady state simulators, used for on-line performance prediction
	and for on-line optimization in crude distillation units are often
	sensitive to small variations in the feed composition, which is specified
	in terms of a True Boiling Point (TBP) vs volume percent distilled
	curve. The exact feed TBP is often not available during the plant
	operation. Also stratification of raw crude oil into layers in the
	large tank farm sections cause severe operating problems in terms
	of the stability of the column. If feed TBP can be predicted online,
	necessary feedforward action can considerably reduce the operating
	problems. A model has been developed for backcalculation of feed
	TBP using measured plant parameters. A heat balance is performed
	around an envelope encompassing the rectifying section of the fractionator
	and is followed by the calculation of Equilibrium Flash Vaporization
	(EFV) temperatures at six different locations of the column which
	are correlated with corresponding feed TBP temperatures. The second
	part of model tuning consists of calculating model parameters in
	the form of point efficiencies so as to minimize the discrepancy
	between the simulator predicted and measured column parameters which
	arises out of modelling approximations such as assumption of phase
	equilibria at each stage and use of imperfect thermodynamics correlations.
	The simulator results, after tuning, were found to match the plant
	measurements within two percent in all the cases investigated. The
	simulator output was used to predict various product properties using
	a Property Prediction package and these were also found to match
	well with those of laboratory measurements.Both the backcalculation
	of feed TBP and the efficiency tuning need to be implemented on-line
	for inferential control and supervisory optimization.},
  comment = {Apenas versão eletrônica.},
  keywords = {Online tuning; Crude distillation; Crude TBP backcalculation; Distillation
	model tuning},
  owner = {Paula},
  pdf = {distillationColumn/Dave:2003.pdf},
  review = {Não foi referenciado.},
  timestamp = {2006.08.24}
}

@ARTICLE{Diwekar:1987,
  author = {U. M. Diwekar and R. K. Malik and K. P. Madhavan},
  title = {Optimal reflux rate policy determination for multicomponent batch
	distillation columns},
  journal = {Computers and Chemical Engineering},
  year = {1987},
  volume = {11},
  pages = {629--637},
  number = {6},
  abstract = {This paper describes a procedure to obtain optimal reflux or optimal
	distillate rate policy for multicomponent batch distillation columns
	using the Pontryagin's continuous maximum principle. For application
	to multicomponent systems, a reduced order model is used using short-cut
	procedure develop specially for analysis and design of batch columns.},
  comment = {Apenas versão impressa. Retirado da CIENTEC.},
  owner = {Paula},
  timestamp = {2006.09.04}
}

@MASTERSTHESIS{Domingues:2005,
  author = {Tito Livio Domingues},
  title = {Avaliação da eficiência de pratos valvulados com downcomer e pratos
	dualflow em colunas de destilação industriais},
  school = {Universidade Federal do Rio Grande do Sul, Escola de Engenharia,
	Departamento de Engenharia Química},
  year = {2005},
  owner = {Paula},
  timestamp = {2007.08.15}
}

@BOOK{Eckel:2000,
  title = {Thinking in C++},
  publisher = {Prentice Hall},
  year = {2000},
  author = {Bruce Eckel},
  volume = {1},
  edition = {2nd},
  month = {April},
  comment = {Versão impressa.},
  owner = {Paula},
  timestamp = {2006.10.11}
}

@ARTICLE{Eckert:1995,
  author = {E. Eckert and M. Kubicek},
  title = {Dynamic Simulations of a Distillation with multiple liquid phases},
  journal = {Computers and Chemical Engineering},
  year = {1995},
  volume = {19},
  pages = {S393 --S398},
  number = {Suppl.},
  abstract = {A rigorous mathematical model of dynamical behaviour of a distillation
	column with a possible occurrence of several (e.g. three ) liquid
	phases on individual trays is described. The generalized model is
	based on the concept of the equilibrium tray. By solving the algebraic
	part of DAE system, the phase situation is tested and the system
	is changing adaptively in the course of the integration. Examples
	of a distillation of mixtures with possible existence of two and
	three liquid phases are presented.},
  comment = {Apenas versão eletrônica.},
  keywords = {Distillation; equilibrium stage column; dynamic model; multiple liquid-vapour
	equilibrium; phase splitting},
  owner = {Paula},
  pdf = {distillationColumn/Eckert:1995.pdf},
  review = {Apresenta um equacionamento que permite a predição de mais de uma
	fase líquida em equilíbrio.
	
	Artigo muito bom!!!},
  timestamp = {2006.08.16}
}

@ARTICLE{Eckert:2001,
  author = {Egon Eckert and Tomás Vanek},
  title = {Some aspects of rate-based modelling and simulation of three-phase
	distillation columns},
  journal = {Computers and Chemical Engineering},
  year = {2001},
  volume = {25},
  pages = {603--612},
  abstract = {The application of the bate-based approach to the dynamic and stationary
	modelling of three-phase distillation columns is presented. The main
	problem can be seen in finding adequate models for the mass and heat
	transfer over phase interfaces to be utilised in the Maxwell-Stefan
	equations. While for the vapour-(continuous) liquid interface, there
	are a number of methods and data available, the interface between
	continuous and dispersed liquid phases has not been studied for the
	case of distillation processes. A reasonable alternative approach
	to modelling of a three-phase distillation column can be found where
	the
	
	liquid-liquid interface is treated as equilibrium. The adequacy of
	this modification is supported by phenomena observed on distillation
	trays, e.g. strong agitation of liquid phases. The resulting combined
	non-equilibrium and equilibrium model is compared to the classical
	equilibrium model and also to experimental data for ethanol-water-cyclohexane
	separation in a number of examples.},
  comment = {Apenas versão eletrônica.},
  keywords = {Rate-based approach; Three-phase distillation; Non-equilibrium tray
	model; Simulation},
  owner = {Paula},
  pdf = {distillationColumn/Eckert:2001.pdf},
  review = {Rate-based = non equilibrium
	
	O foco do artigo é a separação com três fases de equilíbrio (V-L1-L2).
	
	A modelagem (balanços...) é apresentada por partes, dividida conforme
	as fases consideradas: fase vapor, fase líquida (contínua e dispersa)
	, interface líquido-vapor.
	
	Ler mais atentamente a parte de exemplos e conclusões.
	
	Excelente artigo!},
  timestamp = {2006.08.16}
}

@ARTICLE{Eiden:1997,
  author = {Ulrich Eiden and Stephan Scholl},
  title = {Use of Simulation in Rating and Design of Distillation Units},
  journal = {Computers and Chemical Engineering},
  year = {1997},
  volume = {21},
  pages = {S199--S204},
  number = {Suppl.},
  abstract = {The appropriate level of modelling detail in steady state flowsheet
	simulations is an important question for the calculation of thermal
	separation operations such as absorption, distillation, and liquid/liquid
	extraction. The generation of consistent mass and energy balances
	may often be performed employing standard implementations for the
	various unit operations. Surprisingly, operability and sensitivity
	aspects of the process may be estimated with the help of black box
	mass balance cosiderations. As soon as flowsheet simulation is to
	serve as a basis for the rating of existing or the design of new
	distillation units, the level of modelling detail has to be increased
	significantly and a Complex Topology Simulation (CTS) is required.
	Thus, the level of the modelling detail depends strongly on the current
	project state as well as the information desired. These aspects will
	be discussed through four examples of practical relevance concerning
	distillation feed sections and liquid distributors, reboiler section,
	condensation stage and operability aspects.},
  comment = {Apenas versão eletrônica.},
  owner = {Paula},
  pdf = {distillationColumn/Eiden:1997.pdf},
  review = {Não foi referenciado.},
  timestamp = {2006.08.24}
}

@ARTICLE{Elgue:2004,
  author = {S. Elgue and L. Prat and M. Cabassud and J.M. Le Lann and J. Cézerac},
  title = {Dynamic models for start-up operations of batch distillation columns
	with experimental validation},
  journal = CCE,
  year = {2004},
  volume = {28},
  pages = {2735--2747},
  abstract = {The simulation of batch distillation columns during startup operations
	is a very challenging modelling problem because of the complex dynamic
	behaviour. Only few rigorous models for distillation columns startup
	are available in literature and generally required a lot of parameters
	related to tray or pack geometry. On an industrial viewpoint, such
	a complexity penalizes the achievement of a fast and reliable estimate
	of start-up periods. In this paper, two "simple" mathematical models
	are proposed for the simulation of the dynamic behaviour during startup
	operations from an empty cold state. These mathematical models are
	based on a rigorous tray by tray description of the column described
	by conservation laws, liqui/vapour equilibrium relationships and
	equations representative of hydrodynamics. The models calibration
	and validation are studied through experiments carried out on a batch
	distillation pilot plant, with perforated trays, supplied by a water
	methanol mixture. The proposed models are shown by comparison between
	simulation and experimental studies to provide accurate and reliable
	representations of the dynamic behaviour of batch distillation column
	startups, in spite of the few parameters entailed.},
  comment = {Versão Impressa.},
  keywords = {Dynamic simulation, Batch distillation column, Startup operation,
	Experimental validation},
  owner = {Paula},
  pdf = {distillationColumn/Elgue:2004.pdf},
  review = {O objetivo deste artigo é estudar, simular e validar o comportamento
	dinâmico de uma coluna de destilação em batelada, durante a sua partida,
	utilizando dois modelos diferentes.
	
	
	É citado o procedimento necessário para rodar uma partida: a detecção
	de eventos. (Problema que não tenho no EMSO)
	
	
	A modelagem hidráulica não é capaz de prever gotejamento, arraste
	e inundação.
	
	Fornece uma forma interessante de representar a eficiência de MURPHREE.
	Como se a corrente de vapor fosse dividida em duas. e*V é a corrente
	que entra no cálculo de equilíbrio e (1-e)*V é a corrente que by-passa
	o prato indo direto para o prato acima. A eficiência de Murphree
	representa essa fração "e".
	
	
	Explica com detalhes a procedimento de partida de uma coluna batelada.
	
	Com um modelo simplificado é gerado um parâmetro chamado de razão
	de enchimento do prato que representa o valor de holdup de líquido
	em que o prato já está cheio o suficiente para começar a gerar vapor
	para entrar no prato de cima. Antes deste parâmetro atingir o valor
	especificado, todo o vapor que chega ao prato condensa imediatamente
	contribuindo para o acúmulo de líquido.
	
	No modelo realístico, o vapor que sobre para os pratos condensa na
	parede de prato e cai para o prato abaixo até que o prato encha e
	a parede do prato esquente. Depois disso o vapor sobe mais um prato
	e assim por diante até que todos os pratos encham. O modelo realístico
	necessita de dados sobre o prato para calcular o seu aquecimento.
	
	
	Estes modelos foram validados com dados experimentais retirados de
	uma coluna batelada piloto.
	
	
	Como conclusão: o modelo simplificado apresenta bons resultados e
	necessita de menos dados do equipamento. Já o modelo realístico apresenta
	resultados mais precisos porém requer mais detalhamento do equipamento
	e é mais demorado.}
}

@PHDTHESIS{Feehery:1998,
  author = {William Fracis Feehery},
  title = {Dynamic Optimization with Path Constraints},
  school = {Massachusetts Institute of Technology},
  year = {1998},
  month = {June},
  comment = {Apenas versão eletrônica.},
  owner = {Paula},
  pdf = {optimization/Feehery:1998.pdf},
  review = {No capítulo 8 é apresentada a modelagem de coluna de destilação.},
  timestamp = {2007.03.20}
}

@ARTICLE{Fletcher:2000,
  author = {R. Fletcher and W. Morton},
  title = {Initialising Distillation Column Models},
  journal = CCE,
  year = {2000},
  volume = {23},
  pages = {1811--1824},
  abstract = {Difficulties associated with the optimisation of distillation column
	models by non-linear programming are considered. The paper presents
	a systematic procedure to enable these difficulties to be overcome
	and proposes a particular formulation of the distillation column
	model. A certain limiting case of the column model is examined, that
	of infinite reflux or zero feed. This limiting case considerably
	simplifies the model and provides a system of non-linear equations
	that is readily solved. The solution of this problem gives useful
	information about the purity that can be achieved in the general
	case and the number of plates needed
	
	to attain a given level of purity. The limiting problem provides starting
	values for the solution of the general column and suggests a homotopy
	that can be followed if difficulties arise in obtaining convergence.
	To obtain a stable form of the limiting case requires the general
	column model to be formulated in a certain way, which to our knowledge
	has not previously been considered. The ideas have been successfully
	tested on various multi-column flowsheets involving distillation
	columns with heat integration.},
  comment = {Versão impressa.},
  keywords = {Distillation column, Mathematical model, Zero-feed column; Non-linear
	programming, AMPL},
  owner = {Paula},
  pdf = {distillationColumn/Fletcher:2000.pdf},
  review = {O artigo apresenta uma nova modelagem para facilitar a inicialização
	do sistema a fim de utilizar rotinas de otimização. Ele propõe a
	análise de dois casos limites (refluxo infinito e alimentação zero)
	para a geração de valores iniciais para as variáveis para solução
	de otimização via NLP. Ele diz também que o resultado da análise
	destes estados oferece estimativas da pureza que pode ser alcançada
	pela separação ou o número de estágios necessários para alcançar
	uma dada pureza desejada.
	
	Com a diferente formulação proposta, o sistema de equações se torna
	mais simples (um sistema de equações não linear) e de fácil resolução.
	
	
	É utilizada a linguagem de modelagem AMPL.
	
	
	É considerado apenas a solução em EE. A dinâmica não é levada em conta!
	O modelo utiliza apenas equações algébricas.}
}

@BOOK{Forbes:1948,
  title = {A Short History of the Art of Distillation},
  publisher = {Leiden, Netherlands},
  year = {1948},
  editor = {E. J. Brill},
  author = {R. J. Forbes},
  comment = {como referência apud},
  owner = {Paula},
  review = {como referência apud.},
  timestamp = {2006.09.21}
}

@ARTICLE{Gani:1989,
  author = {R. Gani and I. T. Cameron},
  title = {Extension of Dynamic Models of Distillation Columns to Steady-State
	Simulation},
  journal = CCE,
  year = {1989},
  volume = {13},
  pages = {271--280},
  number = {3},
  abstract = {The steady state simulation problem has been successfully coupled
	to an existing dynamic model for distillation columns. The coupling
	fo the dynamic and the steady state problems has been made by modifying
	the numerical procedure for solving ordinary-differential equations
	to solving as well, a set of purely algebraic equations. This has
	allowed the development of a versatile simulation model capable o
	solving dynamic and some steady state simulation problems. The solution
	strategy is presented along with numerical results illustrating the
	special features of the proposed simulation model.},
  comment = {Foi adquirido na CIENTEC. Apenas cópia impressa.},
  owner = {Paula},
  review = {Primeiramente, os autores falam que é mais difícil de conseguir a
	convergência de um modelo estacionário (sistema algébrico) que dinâmico
	(DAE), porém, o problema estacionário necessita um tempo computacional
	menor. A proposta é acoplar características dos dois modelos para
	tornar a solução de problemas estacionários mais robusta.
	
	O modelo é baseado no artigo I do Gani.
	
	
	Embora o artigo proponha a simulação de estado estacionário a partir
	de um modelo dinâmico, ele defende que resultados melhores podem
	ser obtidos com modelos propriamente estacionários. A justificativa
	do método proposto é de que muitas vezes os problemas estacionários
	oferecem muita dificuldade na sua inicialização. Nestes casos, um
	acoplamento com modelo dinâmico resolveria o problema.
	
	
	A troca entre o modo estacionário e o modo dinâmico depende do cálculo
	dos resíduos das equações. Se com os chutes iniciais o problema algébrico
	não consegue ser resolvido, o problema passa para o modo dinâmico
	para um rápida integração para que os estados sejam estimados com
	os chutes iniciais correspondendo às condições iniciais. Assim que
	o RES < tol, ou tenha passado um dado tempo de integração, ou ainda
	o passo da integração já esteja grande o suficiente, o problema volta
	para o modo estacionário.
	
	
	Os resultados da aplicação do método proposto foram apresentados com
	a utilização de 4 problemas teste.}
}

@ARTICLE{Gani:1986,
  author = {R. Gani and C. A. Ruiz and I. T. Cameron},
  title = {A Generalized Model for Distillation Columns - I - Model Description
	and Applications},
  journal = CCE,
  year = {1986},
  volume = {10},
  pages = {181--198},
  number = {3},
  abstract = {A generalized model for the dynamic simulation of distillation columns
	is presented. The model allows the solution of a wide variety fo
	problems, from open and closed-loop responses of single (and multiple)
	columns to operability studies (of feed changeover and startup operations)
	and column instability studies (effect of plate hydraulics during
	transient operations). Results are given for single columns (including
	industrial) as well as multiple columns for a different types of
	operations. The problems include thermodynamically close to ideal
	systems to highly ninideal systems. Efficient and robust numerical
	integrators are used to obtain reliable solutions even for difficult
	discontinuous operations.},
  comment = {Foi adquirido na CIENTEC. Apenas cópia impressa.},
  owner = {Paula},
  review = {Inicialmente, os autores enfatizam a necessidade da elaboração de
	um modelo genérico, para vários tipos de estudos e vários tipos de
	configurações de colunas de destilação mas que ao mesmo tempo seja
	numericamente robusto, eficiente e realístico.
	
	O modelo utiliza o paradigma orientado a equações para resolver os
	sistema de equações diferenciais (ODEs) e o paradigma sequencial
	modular para resolver cada subgrupo de equações algébricas.
	
	Então, o sistema final que é composto por um sistema de ODEs, balanços
	de massa e energia, e um sistema de equações algébricas, que correspondem
	aos cálculos termodinâmicos, hidráulica dos pratos, controladores
	e outros. As equações algébricas, divididas em subconjuntos, são
	resolvidas para a determinação do lado direito das equações diferenciais
	necessário pelo integrador. Com a estimativa do lado direito, as
	variáveis diferenciais são estimadas seus valores retornam para as
	algébricas e assim segue o procedimento até o tempo final requerido.
	
	
	O artigo é dividido em duas partes: a primeira descreve e modelagem
	e a segunda a resolução do sistema gerado. Alguns exemplos são apresentados
	para a validação do sistema proposto.}
}

@ARTICLE{Gao:2003,
  author = {Wuzi Gao and Robert L. Robinson Jr. and Khaled A.M. Gasem},
  title = {Alternate equation of state combining rules and interaction parameter
	generalizations for asymetric mixtures},
  journal = {Fluid Phase Equilibria},
  year = {2003},
  volume = {213},
  pages = {19--37},
  owner = {Paula},
  timestamp = {2007.10.23}
}

@ARTICLE{Gross:1998,
  author = {E Gross and E. Baumann and A. Geser and D.W.T. Rippin and L. Lang},
  title = {Modelling, simulation and controllability analysis of an industrial
	heat-integrated distillation process},
  journal = {Computers and Chemical Engineering},
  year = {1998},
  volume = {22},
  pages = {223--237},
  number = {1-2},
  abstract = {A controllability analysis of an industrial heat-integrated distillation
	process is described. The rigorous process model includes the important
	interactions of the liquid inventories between each other and with
	the heat transfer rate. Three different control schemes are investigated
	using steady-state and dynamic controllability measures. These schemes
	are compared with an unconventional control structure. The application
	of controllability analyses to real world examples is discussed.},
  comment = {Apenas versão eletrônica.},
  owner = {Paula},
  pdf = {distillationColumn/Gross:1998.pdf},
  review = {LER O ARTIGO MAIS A FUNDO PARA SABER DE INTEGRAÇÃO DE COLUNAS DE DESTILAÇÃO.
	Não foi referenciado.},
  timestamp = {2006.08.16}
}

@ARTICLE{Grossmann:2005,
  author = {Ignacio E. Grossmann and Pio A. Aguirre and Mariana Barttfeld},
  title = {Optimal synthesis of complex distillation columns using rigorous
	models},
  journal = {Computers and Chemical Engineering},
  year = {2005},
  volume = {29},
  pages = {1203--1215},
  abstract = {The synthesis of complex distillation columns has remained a major
	challenge since the pioneering work by [Sargent, R.W.H., & Gaminibandara,
	K. (1976). Optimal design of plate distillation columns. In L.C.W.
	Dixon (Ed.), Optimization in action. New York: Academic Press]. In
	this paper, we first provide a review of recent work for the optimal
	design of distillation of individual columns using tray-by-tray models.
	We examine the impact of different representations and models, NLP,
	mixed-integer nonlinear programming (MINLP) and generalized disjunctive
	programming (GDP), as well as the importance of appropriate initialization
	schemes. We next provide a review of the synthesis of complex column
	configurations for zeotropic mixtures and discuss different superstructure
	representations as well as decomposition schemes for tackling these
	problems. Finally, we briefly discuss extensions for handling azeotropic
	mixtures. Numerical examples are presented to demonstrate that effective
	computational strategies are emerging that are based on disjunctive
	programming models that are coupled with thermodynamic initialization
	models and integrated through hierarchical decomposition techniques.},
  comment = {Apenas versão eletrônica.},
  keywords = {Disjunctive programming; Complex distillation columns; Initialization},
  owner = {Paula},
  pdf = {optimization/Grossmann:2005.pdf},
  review = {Síntese por otimização. Artigo não lido.Não foi referenciado.},
  timestamp = {2006.08.16}
}

@ARTICLE{Gumus:1997,
  author = {Zeynep H. Gumus and Amy R. Ciric},
  title = {Reactive Distillation Column Design with Vapor/Liquid/Liquid Equilibria},
  journal = {Computers and Chemical Engineering},
  year = {1997},
  volume = {21},
  pages = {S983--S988},
  number = {Suppl.},
  abstract = {This paper explores the design of reactive distillation columns with
	vapor/liquid/liquid equilibria. The number of phases and the phase
	equilibria on each tray are determined by minimizing the Gibbs free
	energy, allowing for a variable number of phases on each tray. The
	minimization problems are embedded within a larger problem that minimizes
	the annualized cost of the column, creating a bilevel optimization
	problem. A novel sequential approximation approach that can identify
	global solutions of the inner optimization problems is also introduced.
	The sequential approximation approach is employed to design reactive
	distillation and reactive flash processes.},
  comment = {APenas versão eletrônica.},
  owner = {Paula},
  pdf = {reactivedistillation/Gumus:1997.pdf},
  timestamp = {2006.09.22}
}

@ARTICLE{Higler:1999,
  author = {A.P. Higler and R. Taylor and R. Krishna},
  title = {The influence of mass transfer and mixing on the performance of a
	tray column for reactive distillation},
  journal = {Chemical Engineering Science},
  year = {1999},
  volume = {54},
  pages = {2873--2881},
  comment = {versão eletrônica.},
  keywords = {Reactive distillation; Ethylene glycol; Maxwell-Stefan equations;
	Energy balance; Multiple steady states; Tray design},
  owner = {Paula},
  pdf = {reactivedistillation/Higler:1999.pdf},
  timestamp = {2006.09.22}
}

@PHDTHESIS{Higler:1999_dissertation,
  author = {Arnoud Peter Higler},
  title = {A Nonequilibrium Model for Reactive Distillation},
  school = {Clarkson University},
  year = {1999},
  month = {September},
  comment = {Apenas eletrônica.},
  owner = {Paula},
  pdf = {reactivedistillation/Higler:1999_dissertation.pdf},
  timestamp = {2006.09.22}
}

@ARTICLE{Hongyan:2002,
  author = {Zhang Hongyan and Wang Shuying and Zhou Rongqi and Duan Zhanting},
  title = {Mixing pool model for prediction of distillation tray efficiency
	with liquid entrainment},
  journal = {Chemical Engineering Journal},
  year = {2002},
  volume = {88},
  pages = {21--26},
  abstract = {In order to make clear the effect of liquid entrainment on the distillation
	tray efficiency, a new type of mixing pool model is developed in
	this paper to calculate the apparent distillation tray efficiencies
	when the liquid entrainment happens for the counter current tray
	with vapour unmixing between trays and liquid partially mixing on
	trays. The analytical solutions are obtained and compared with the
	calculated results
	
	of Bennett's experimental correlations. The mean relative error between
	them is 5.6% for the range of 0 <= Pe <= 1000, 0.5 <= lambda <= 3.0
	and 0.4 <= E <= 1.0. The result shows that the model presented in
	this paper is reliable.},
  comment = {Apenas versão eletrônica.},
  keywords = {Distillation; Tray; Mixing pool model; Liquid entrainment; Apparent
	tray efficiency; Analytical solution},
  owner = {Paula},
  pdf = {distillationColumn/Hongyan:2002.pdf},
  review = {Artigo que trás uma formulação detalhada a cerca dos gradientes de
	mistura no prato, do arraste e outras variáveis que podem influenciar
	o cálculo da eficiência.},
  timestamp = {2006.08.16}
}

@TECHREPORT{Solomon:2007,
  author = {{HSB Solomon Associates LLC}},
  title = {2006 Worldwide Refining APC/Automation Performance Analysis - Part
	II: Special Topics},
  institution = {HSB Solomon Associates LLC},
  year = {2007},
  owner = {Paula},
  timestamp = {2007.10.23}
}

@ARTICLE{Humphrey:1992,
  author = {J. L. Humphrey and A. F. Siebert},
  title = {Separation technologies: An opportunity for energy savings},
  journal = {Chem. Eng. Progr.},
  year = {1992},
  volume = {88},
  pages = {32--41},
  number = {3},
  comment = {Artigo citado como apud!},
  owner = {Paula},
  timestamp = {2006.08.29}
}

@ARTICLE{Huss:1996,
  author = {Robert S. Huss and Arthur W. Westerberg},
  title = {Collocation Methods for Distillation Design. 1. Model Description
	and Testing},
  journal = {Ind. Eng. Chem. Res.},
  year = {1996},
  volume = {35},
  pages = {1603--1610},
  abstract = {Fast and accurate distillation design requires a model that significantly
	reduces the problem size while accurately approximating a full-order
	distillation column model. This collocation model builds on the concepts
	of past collocation models for design of complex real-world separation
	systems. Two variable transformations make this method unique. Polynomials
	cannot accurately fit trajectories which flatten out. In columns,
	flat sections occur in the middle of large column sections or where
	concentrations go to 0 or 1. With an exponential transformation of
	the tray number which maps zero to an infinite number of trays onto
	the range 0-1, four
	
	collocation trays can accurately simulate a large column section.
	With a hyperbolic tangent transformation of the mole fractions, the
	model can simulate columns which reach high purities. Furthermore,
	this model uses multiple collocation elements for a column section,
	which is more accurate than a single high-order collocation section.},
  comment = {Apenas versão eletrônica.},
  owner = {Paula},
  pdf = {distillationColumn/Huss:1996.pdf},
  timestamp = {2006.08.28}
}

@ARTICLE{Jobson:1997,
  author = {Megan Jobson},
  title = {Short-cut Evaluation of Distillation Sequences},
  journal = {Computers chem. Engng,},
  year = {1997},
  volume = {21},
  pages = {S553--S557},
  number = {Suppl.},
  abstract = {For screening sequences of distillation columns, heuristic rules may
	be used, but the many contradictions and limitations of heuristics
	are well known. Vapour load is often used as a cost indicator for
	separation sequences. However, capital costs, which vapour load does
	not incorporate, also make a significant and variable contribution
	to the total annual costs of distillation processes. 
	
	A "boiling capacity variable" has been developed, which is calculated
	from the number of stages and internal flow rates in a column. It
	measures the total internal vaporization rate in a process. That
	is, for a distillation column, the overall boiling capacity is the
	sum over all stages (including the reboiler and the condenser) of
	the molar vapour flow rate. The short-cut methods of Fenske, Underwood,
	Gilliland and others exist for calculating the reflux ratio and number
	of stages of distillation columns. The overall capacity variable
	can therefore be calculated using these short-cut methods.
	
	The optimal separation sequence for an ideal five-component mixture
	is investigated in this work. Distillation sequences are evaluated
	using both rigorous simulation with detailed cost analysis and the
	capacity variable and short-cut methods. The short-cut results are
	found to agree with the rigorous results, but have the benefits of
	requiring fewer detailed assumptions and being less computationally
	demanding.},
  comment = {Apenas versão eletrônica.},
  owner = {Paula},
  pdf = {distillationColumn/Jobson:1997.pdf},
  review = {ler mais profundamente.Não foi referenciado.},
  timestamp = {2006.08.23}
}

@ARTICLE{Kaeser:2006,
  author = {M. Kaeser and C.L. Pritchard},
  title = {The impact of heat transfer on Murphree tray efficiency},
  journal = {Energy},
  year = {2006},
  volume = {Article in Press},
  pages = {--},
  abstract = {This work features the experimental determination of heat transfer
	coefficients and Murphree tray efficiencies on a diabatic (heat-transferring)
	distillation tray. The present investigation, focussing on the impact
	of heat transfer on sieve tray performance, is part of a long-term
	project on heat integrated distillation columns (HIDiC). Heat transfer
	coefficients and tray efficiencies have been determined experimentally
	for the methanol/water system in a 150mm diameter distillation column.
	The heat-transferring tray was operated in both heating and cooling
	modes, with heat fluxes up to 50 and 100kW/m2, respectively. The
	experimental data from these diabatic experiments were compared with
	data obtained from the same column in adiabatic mode and were correlated
	with the vapour velocity and the heat flux to/from the tray.},
  comment = {Article in Press. Apenas versão eletrônica.},
  keywords = {HIDiC; Murphree tray efficiency; Sieve trays},
  owner = {Paula},
  pdf = {distillationColumn/Kaeser:2006.pdf},
  review = {Neste artigo, o foco é a energia. Alternativas de integração energética
	para reduzir o consumo de energia em uma coluna de destilação. Porém,
	diz-se na literatura que quanto maior o grau de integração de energia
	mais prejudicada fica a eficiência desse processo. Assim, o artigo
	estuda uma maneira de quantificar esta relação.
	
	Um trabalho experimental foi realizado com uma coluna com um prato
	central com troca de calor, uma forma de poupar energia. Como conclusão,
	a Emv aumenta com o fornecimento de calor ao prato diabático e diminui
	com a retirada de calor. Este efeito é devido à variação na vazão
	de vapor.
	
	
	Não foi referenciado.},
  timestamp = {2006.08.18}
}

@ARTICLE{Karacan:1998,
  author = {S. Karacan and Y. Cabbar and M. Alpbaz and H. Hapoglu},
  title = {The steady-state and dynamic analysis of packed distillation column
	based on partial differential approach},
  journal = {Chemical Engineering and Processing},
  year = {1998},
  volume = {37},
  pages = {379--388},
  abstract = {The steady-state and dynamic behavior of a binary packed distillation
	column has been simulated using the two film back-mixing model. The
	model solution has been obtained employing orthogonal collocation
	on finite elements. The approach using the Legendre or Jacobi polynomial
	has been tested on the solution of related models. A pilot plant
	scaled packed distillation
	
	column distilling methanol-water mixture was used for experimental
	work. The variation of overhead and bottom temperatures have been
	monitored by an on-line computer control system. A number of comparisons
	have been made between the results predicted in this work from back
	mixing model based on the two film theory and those obtained experimentally.
	In most cases the prediction of this work gave results which were
	closer to experiment than other numerical solutions, showing that
	Legendre polynomials for orthogonal collocation on finite element
	can be applied effectively to simulate the packed distillation column
	by using a partial differential approach.},
  comment = {Apenas versão eletrônica.},
  keywords = {Packed distillation column; Modeling; Orthogonal collocation; Finite
	element},
  owner = {Paula},
  pdf = {distillationColumn/Karacan:1998.pdf},
  review = {Não foi referenciado.},
  timestamp = {2006.08.24}
}

@BOOK{Khoury:2005,
  title = {Multistage Separation Processes},
  publisher = {CRC Press},
  year = {2005},
  author = {Fouad M. Khoury},
  edition = {Third Edition},
  owner = {Paula},
  pdf = {distillationColumn/Khoury:2000.pdf},
  timestamp = {2007.03.20}
}

@ARTICLE{Kienle:2000,
  author = {Achim Kienle},
  title = {Low-order dynamic models for ideal multicomponent distillation processes
	using nonlinear wave propagation theory},
  journal = {Chemical Engineering Science},
  year = {2000},
  volume = {55},
  pages = {1817--1828},
  abstract = {A new approach to the development of low-order dynamic models for
	multicomponent distillation processes is presented. This approach
	makes direct use of well-known spatio-temporal pattern formation
	phenomena also termed as nonlinear wave propagation. It takes into
	account the typical features of multicomponent systems, i.e. coexistence
	of di!erent constant pattern waves within a single section of a distillation
	column and the resulting wave interactions. In a first step, constant
	molar holdups and flow rates, constant pressure and constant relative
	volatilities are assumed. Under these conditions a rigorous analytical
	treatment is possible and a comparably simple but sound and robust
	method for nonlinear model reduction is developed. The approach applies
	to packed as well as staged columns provided the number of column
	stages is suficiently large. Application is demonstrated for two
	di!erent distillation processes with a three and a five component
	mixture, respectively. It is shown that the dynamic behaviour of
	the low-order model is in good agreement with corresponding reference
	model for a large set of operating conditions. Finally, extensions
	of the present approach to processes with variable molar flow rates
	as well as variable volatilities are discussed.},
  comment = {Apenas versão eletrônica.},
  keywords = {Low-order model; Reduced-order model; Distillation; Nonlinear wave
	propagation; Constant pattern waves},
  owner = {Paula},
  pdf = {distillationColumn/Kienle:2000.pdf},
  review = {Não foi referenciado.},
  timestamp = {2006.08.24}
}

@ARTICLE{Kim:1999,
  author = {Y. H. Kim},
  title = {Optimal design and operation of a multi-product batch distillation
	column using dynamic model},
  journal = CEP,
  year = {1999},
  volume = {38},
  pages = {61--72},
  abstract = {Although the operation of a batch distillation column involves dynamic
	behavior from the beginning to the end, the quasi-steady state model
	or the short-cut method has been widely implemented in the design
	of the column owing to simple computation in spite of the expected
	discrepancy with real process operation. In this study, a dynamic
	process model is utilized in the optimal design of the batch distillation
	process and the successive quadratic programming is employed as an
	optimization procedure. A ternary system is examined to see that
	the dynamic model design gives a significant improvement, especially
	for the operation having a dynamic manipulation of reflux ratio.
	The outcome of the optimization for the example system indicates
	that more amount of product with less operation time than that of
	the quasi-steady model is available. In addition, the optimization
	of net profit tells that the optimum number of trays is 23 for the
	sample system. The optimum operation schedule of the system is also
	obtained from the optimization of operational profit. Finally, the
	effect of side product recycle is investigated.},
  comment = {Versão impressa.},
  keywords = {Process design; Batch distillation; Dynamic model; Optimal design;
	Optimal operation},
  owner = {Paula},
  pdf = {distillationColumn/Kim:1999.pdf},
  review = {O autor enfatiza que a operação de uma coluna de destilação batelada
	tem caráter dinâmico do início ao fim, então o uso de modelos reduzidos
	(short-cut) ou quasi-steady state podem levar a resultados menos
	precisos.
	
	A otimização de uma coluna batelada passa por três objetivos:
	
	1)maximização do produto (destilado)
	
	2) minimização do tempo da batelada
	
	3)maximização do lucro por unidade de tempo de operação
	
	
	O autor diz que a hidráulica do prato deve ser incluída na modelagem
	utilizada na simulação para obter uma resposta real de condições
	de operação. O artigo defende que deve ser utilizado um modelo rigoroso
	para otimização.
	
	Neste artigo é implementado um modelo dinâmico para otimizar o perfil
	de operação da uma coluna de destilação batelada. Apesar de ser dinâmico
	os acúmulos de líquido no prato e no topo são constantes só variando
	com o tempo o acúmulo de líquido do fundo. Para as estimativas iniciais,
	foi construído outro modelo dinãmico com cálculos de equilíbrio via
	UNIQUAC e não via volatilidade constante.
	
	O problema é resolvido via colocação ortogonal, onde as equações diferenciais
	se tornam algébricas. Na otimização estas equações são consideradas
	restrições.
	
	
	O restante do artigo fala da formulação da função objetivo e do resultado
	encontrado para o otimização.}
}

@ARTICLE{Kiva:1997,
  author = {Valeri N. Kiva and Bella M. Aiukhanova},
  title = {Multiple steady states of distillation and its realisation},
  journal = {Computers and Chemical Engineering},
  year = {1997},
  volume = {21},
  pages = {S541--S546},
  number = {Suppl.},
  abstract = {Multiplicity of steady states is known for distillation of mixtures
	with certain type of distillation line map. This paper presents the
	study of its realisation for the ternary mixture with one binary
	azeotrope formed between light and heavy component. Continuous single-feed
	distillation column with a finite number of trays is considered.
	The steady states are determined by simulation of the dynamic process
	where the initial composition profile is the result of certain operating
	policy. There is a range of parameters where distinct operating policies
	give distinctly different product compositions. The paper concludes
	with a discussion of the ways to obtain and to maintain a desired
	steady state and to restore it in case of disruption.},
  comment = {Apenas versão eletrônica.},
  owner = {Paula},
  pdf = {distillationColumn/Kiva:1997.pdf},
  review = {Não foi referenciado.},
  timestamp = {2006.08.18}
}

@MASTERSTHESIS{Klingberg:2000,
  author = {A. Klingberg},
  title = {Modeling and Optimization of Batch Distillation},
  school = {Department of Automatic Control, Lund Institute of Technology},
  year = {2000},
  address = {Lund, Sweden},
  month = Feb,
  abstract = {The detailed dynamic modelling, simulation and optimisation of a batch
	distillation process at Bayer AG is presented. The model considers
	a mixture of 10 components separated in a 40 tray column. Simulations
	performed in the process modelling tool gPROMS proved that themodel
	gives a very accurate description of the process behaviour. To increase
	the profit of the process an optimisation of the operating procedure
	was performed, with the reflux ratio as the only control variable.
	The optimisation resulted in an increased profit, i.e. the product
	yield was increased while at the same time production time was decreased.
	Another optimisation was performed to account for the periodicity
	of the process, by optimising the initial conditions of the batch.
	These depend on the amount of fresh feed and the amount and composition
	of material which is recycled from the intermediate cut and mixed
	with the fresh feed. This optimisation also resulted in an increased
	profit. Overall, gPROMS proved to be a powerful tool for solving
	optimisation problems of large scale models of great complexity such
	as the batch distillation process.},
  comment = {Versão impressa.},
  owner = {Paula},
  pdf = {distillationColumn/Klingberg:2000.pdf},
  review = {A dissertação está baseada na modelagem de uma coluna de destilação
	batelada em gPROMS, sua simulação e otimização. O objetivo da otimização
	era maximizar o lucro da operação: minimizando o tempo de batelada
	e ao mesmo tempo maximizando o rendimento do produto. Os resultados
	obtidos no gPROMS foram comparados com o programa SPEEDUP da Aspen
	e com o programa de otimização DYNOPT da RWTH Aachen.
	
	Na seção 2, o processo utilizado como exemplo é explicado.
	
	Na seção 3, o modelo é descrito.
	
	Na seção 4, as características do gPROMS. Dentro destas características,
	é apresentada a inexistência da condicional da linguagem do gPROMS.
	Para sanar esta deficiência é apresentada a função tanh(bx+1)/2.
	
	Na seção 5, é montado o problema de otimização.
	
	Na seção 6, a simulação da coluna e seus procedimentos.
	
	Na seção 7, a otimização do sistema.
	
	Na seção 8, é explicado como uma batelada influencia outra através
	da reintrodução sucessiva do corte intermediário nas bateladas.
	
	Na seção 9, são apresentadas as conclusões.
	
	No apêndice A é mostrada uma composição típica da carga.
	
	No apêndice B são apresentadas as equações do modelo.}
}

@ARTICLE{Koeijer:2004,
  author = {Gelein M. de Koeijer and Signe Kjelstrup},
  title = {Application of Irreversible Thermodynamics to Distillation},
  journal = {Int. J. of Thermodynamics},
  year = {2004},
  volume = {7},
  pages = {107--114},
  number = {3},
  month = {September},
  abstract = {We compare three different ways of modelling tray distillation to
	each other, and to experimental data: the most common way that assumes
	equilibrium between the liquid and vapour phases at the outlets of
	each tray, and two more precise methods that use irreversible thermodynamics.
	Irreversible thermodynamics determines the driving forces and fluxes
	of a system in agreement with the second law. It is shown that the
	methods using irreversible thermodynamics (Maxwell-Stefan equations)
	are superior to the method that assumes that equilibrium is reached
	on each tray. The Soret effect must be included to have a good description
	of the heat flux.},
  comment = {Versão impressa.},
  keywords = {Irreversible Thermodynamics, Distillation, Maxwell-Stefan Equation,
	Soret/Dufour effects, Interface},
  owner = {Paula},
  pdf = {distillationColumn/Koeijer:2004.pdf},
  review = {O artigo apresenta uma boa introdução sobre destilação e sobre eficiência
	de Murphree.
	
	"In irreversible thermodynamics the fluxes and forces of the system
	are derived in a systematic way: All possible coupling effects can
	be included, or discarded, within a framework that complies with
	the second law."
	
	
	"Instead of assuming equilibrium between the liquid and vapour at
	the outlets of each tray, in the Maxwell-Stefan approach one introduces
	a liquid film and a vapour film with gradients in temperature and
	concentration. The films meet at the interface, where equilibrium
	is assumed between the vapour and liquid, however."
	
	
	"This work compares the performance of the Maxwell-Stefan approach,
	the interface integrated approach and the model assuming equilibrium
	reached on each tray for a binary tray distillation column that separates
	water and ethanol."
	
	
	Na introdução, o artigo apresenta os principais métodos de modelagem
	de colunas existentes na literatura.
	
	
	A modelagem proposta no artigo é baseada no balanço de entropia. Esta
	modelagem é uma alternativa mais rigorosa que a modelagem baseada
	em equilíbrio.
	
	
	ARTIGO MUITO INTERESSANTE, QUE CONTÉM UMA BOA DESCRIÇÃO DOS MÉTODOS
	DE MODELAGEM DE PRATOS REAIS.},
  timestamp = {2006.08.18}
}

@PHDTHESIS{Kooijman:1995a,
  author = {Hendrik Adriaan Kooijman},
  title = {Dynamic Nonequilibrium Column Simulation},
  school = {Clarkson University},
  year = {1995},
  month = {February},
  abstract = {Simulation of distillation columns usually is carried out using an
	equilibrium model based on the assumption that thermodynamic and
	thermal equilibrium exists on each tray in the column. To deal with
	departures from thermodynamic equilibrium it is common practice to
	specify an efficiency that is the same for all components on all
	stages. However, component efficiencies are not equal in systems
	with more than two components and cannot be correlated, especially
	for nonideal systems. This makes the equilibrium model inappropriate
	for dynamic simulations where these efficiencies are subject to change
	and cannot be specified beforehand. Using constant efficiencies neglects
	the influence of the tray hydrodynamics on the mass transfer and
	the consequences for the column dynamics. Additionally, in certain
	column operations there is a departure from thermal equilibrium which
	cannot be modeled with the equilibrium model either.
	
	In this thesis a nonequilibrium model for the dynamic simulation of
	distillation columns is described. The nonequilibrium model incorporates
	the rigorous calculation of the mass and energy transfer rates and
	avoids the use of efficiencies. The influence of mass transfer correlations
	on column dynamics has been investigated. A new design mode is implemented
	that eliminates the need for a previously known column layout in
	order to do a nonequilibrium (dynamic) simulation, which enlarges
	the range of application of the model. Alternative plug-flow models
	are proposed to improve the modeling of mass transfer on large trays.},
  comment = {Versão impressa.},
  owner = {Paula},
  pdf = {distillationColumn/Kooijman:1995a.pdf},
  review = {No capítulo 1 é dada uma boa introdução a cerca da modelagem dinâmica
	e especialmente, de colunas de destilação.
	
	No capítulo 2 a modelagem estacionária de não equilíbrio é mostrada,
	assim como equações para perda de carga e hidráulica.
	
	O capítulo 3 fala do mesmo assunto retratado na referência Kooijman:1995.
	
	No capítulo 4, o modelo dinâmico de não equilíbrio
	
	No 5, as simulações e seus resultados são apresentados.
	
	No 6, as conclusões.
	
	No Apêndice A são mostradas correlações.},
  timestamp = {2006.08.21}
}

@ARTICLE{Kooijman:1995,
  author = {Hendrik A. Kooijman and Ross Taylor},
  title = {Modelling mass transfer in Multicomponent distillation},
  journal = {The Chemical Engineering Journal},
  year = {1995},
  volume = {57},
  pages = {177--188},
  abstract = {This paper highlights inconsistencies in the modelling of mass tranfer
	in multicomponent distillation columns. Models of flow and mass tranfer
	are developed that seek to avoid this inconsistencies based on the
	usual assumptions of plug flow of vapor and plug flow or axial dispersion
	of the liquid. These models are used together with a nonequilibrium
	model of trayed distillation column. It is shown that the revised
	models as capable of sensible predictions of column performance.
	Methods of evaluating binary (Maxwell-Stephan) mass transfer coefficients
	are evaluated and it is found that mass transfer on sieve trays is
	best modelled with Chan and Fair correlation. Mass transfer in multicomponent
	distillation should be modelled using the Maxwell-Stephan equations;
	simpler approaches may be significantly less demanding of computer
	time but column design based on such methods can be very different
	from those obtained using the more rigorous approach.},
  comment = {Apenas versão eletrônica.},
  keywords = {Mass tranfer; Multicomponent distillation},
  owner = {Paula},
  pdf = {distillationColumn/Kooijman:1995.pdf},
  review = {" A nonequilibrium model uses separeted balances of the (two) phases
	which are coupled through terms for the interphase mass transfer
	rates."
	
	Toda a modelagem rigorosa é mostrada (fluxos de vapor e líquido, equações
	de transferência de massa......)
	
	
	São feitas simulações para avaliar o cálculo da eficiência de Murphree
	variando as vazões e a forma de mistura das fases (mistura perfeita,
	plug flow, dispersão).
	
	As principais contribuições do artigo são uma nova proposição de modelo
	para plug-flow e dispersão nas fases líquidas e vapor. Também a discussão
	a cerca do cálculo dos coeficientes binários de troca de massa. O
	método de Maxwell-Stephan foi discutido e tido como muito pesado
	computacionalmente.},
  timestamp = {2006.08.21}
}

@ARTICLE{Laurance:1974,
  author = {D. R. Laurance and G.W.Swift},
  journal = {J.Chem.Eng.Data},
  year = {1974},
  volume = {19},
  pages = {61},
  owner = {Paula},
  timestamp = {2007.09.10}
}

@ARTICLE{Lee:1998,
  author = {Jin-Ho Lee and M.P. Dudukovic},
  title = {A comparison of the equilibrium and nonequilibrium models for a multicomponent
	reactive distillation column},
  journal = {Computers and Chemical Engineering},
  year = {1998},
  volume = {23},
  pages = {159--172},
  abstract = {Appropriate models and computational algorithms were developed and
	a series of simulations for a reactive distillation tray column were
	performed in order to compare the equilibrium and nonequilibrium
	model. The homogeneous liquid phase reversible reaction between acetic
	acid and ethanol in production of ethyl acetate was employed as a
	test chemical reaction. Both the Newton-Raphson and homotopy-continuation
	methods were applied to solve the set of model equations. The homotopy-continuation
	method was found superior to the Newton-Raphson method in guaranteeing
	the desired solution for the nonequilibrium model. The comparison
	between the equilibrium and the nonequilibrium model reveals that
	the nonequilibrium model is to be preferred for the simulation of
	a tray column for reactive distillation because of the dificulty
	in the accurate prediction of tray eficiency for the equilibrium
	model. Close agreement in the prediction of the two models arises
	only when the tray eficiency can be correctly guessed for the equilibrium
	model. The efects of reaction rate and reflux ratio on the column
	performance were illustrated using the nonequilibrium model. The
	use of the heat generated by the exothermic reaction as an internal
	heat source in the column is discussed.},
  comment = {Versão Impressa.},
  keywords = {Reactive distillation; Nonequilibrium model; Homotopy-continuation
	method; Ethyl acetate; Equilibrium model; Newton method},
  owner = {Paula},
  pdf = {reactivedistillation/Lee:1998.pdf},
  timestamp = {2006.08.25}
}

@ARTICLE{Liu:2000,
  author = {C. J. Liu and X. G. Yuan and K. T. Yu and X. J. Zhu},
  title = {A fluid-dynamic model for flow pattern on a distillation tray},
  journal = {Chemical Engineering Science},
  year = {2000},
  volume = {55},
  pages = {2287--2294},
  abstract = {A fluid-dynamic model for describing the liquid-phase flow on a sieve
	tray with consideration of both the resistance and the bubbling efect
	created by the uprising vapor phase is presented, and solved numerically
	by the method of control volume. For verifying the proposed model,
	the liquid velocity distributions on a sieve tray were measured by
	the hot-film anemometry. The theoretical predictions by present model
	are in agreement with the experimental results by the authors and
	from the literature.},
  comment = {Apenas versão eletrônica.},
  keywords = {Distillation; Fluid mechanics; Mathematical modeling; Multiphase flow;
	Flow pattern on a distillation tray; Local velocity measurement},
  owner = {Paula},
  pdf = {distillationColumn/Liu:2000.pdf},
  review = {Não foi referenciado.},
  timestamp = {2006.08.21}
}

@BOOK{Lockett:1986,
  title = {Distillation tray fundamentals},
  publisher = {Press Syndicate of the University of Cambridge},
  year = {1986},
  editor = {Cambridge University Press},
  author = {M. J. Lockett},
  address = {New York},
  comment = {Apenas versão impressa.},
  owner = {Paula}
}

@ARTICLE{Luyben:2006,
  author = {William L. Luyben},
  title = {Evaluation of criteria for selecting temperature control trays in
	distillation columns},
  journal = {Journal of Process Control},
  year = {2006},
  volume = {16},
  pages = {115--134},
  abstract = {The use of tray temperatures to infer compositions is widespread in
	distillation control. A number of criteria have been proposed for
	selecting which trays to hold at constant temperature. The most commonly
	used are (1) choosing a tray where there are large changes in temperature
	from tray to tray ("slope" of the temperature profile), (2) finding
	the tray where there is the largest change in temperature for a change
	in the manipulated variable ("sensitivity"), (3) using singular value
	decomposition (SVD) analysis, (4) selecting the tray where the temperature
	does not change as feed composition changes while producing the desired
	distillate and bottoms purities and (5) choosing the tray that produces
	the smallest changes in product purities when it is held constant
	in the face of feed composition disturbances. 
	
	This paper provides a quantitative comparison of the effectiveness
	of these five alternative criteria. Several systems are considered,
	ranging from ideal binary to azeotropic multi-component. Results
	show that SVD analysis provides a simple and effective method for
	selecting temperature control tray location.},
  comment = {Apenas versão eletrônica.},
  owner = {Paula},
  pdf = {distillationColumn/Luyben:2006.pdf},
  review = {Não foi referenciado.},
  timestamp = {2006.08.21}
}

@ARTICLE{McKay:1997,
  author = {Ben McKay and Mark Willis and Geoffrey Barton},
  title = {Steady-state modelling of chemical process systems using genetic
	programming},
  journal = {Computers and Chemical Engineering},
  year = {1997},
  volume = {21},
  pages = {981--996},
  number = {9},
  abstract = {Complex processes are often modelled using input-output data from
	experimental tests. Regression and neural network modelling techniques
	are commonly used for this purpose. Unfortunately, these methods
	provide minimal information about the model structure required to
	accurately represent process characteristics. In this contribution,
	we propose the use of Genetic Programming (GP) as a method for developing
	input-output process models from experimental data. GP performs symbolic
	regression, determining both the structure and the complexity of
	the model during its evolution. This has the advantage that no a
	priori modelling assumptions have to be made. Moreover, the technique
	can discriminate between relevant and irrelevant process inputs,
	yielding parsimonious model structures that accurately represent
	process characteristics. Following a tutorial example, the usefulness
	of the technique is
	
	demonstrated by the development of steady-state models for two typical
	processes, a vacuum distillation column and a chemical reactor system.
	A statistical analysis procedure is used to aid in the assessment
	of GP algorithm settings and to guide in the selection of the final
	model structure.},
  comment = {Apenas versão eletrônica.},
  keywords = {genetic programming; symbolic regression; process modelling},
  owner = {Paula},
  pdf = {distillationColumn/McKay:1997.pdf},
  review = {Não foi referenciado.},
  timestamp = {2006.08.24}
}

@ARTICLE{Mehlhorn:1996,
  author = {Arndt Mehlhorn and Antonio Espuña and Ana Bonsfills and Andrzej Gorak
	and Luis Puigjaner},
  title = {Modelling and Experimental Validation of both mass transfer and tray
	hydraulics in batch distillation},
  journal = {Computers and Chemical Engineering},
  year = {1996},
  volume = {20},
  pages = {S575--S580},
  number = {Suppl.},
  abstract = {A sinmlation model for batch distillation in colunms with perforated
	plates has been devdoped. Its novelty consists in the use of both
	the non-equilibrium and the equilibrium model making up together
	a better integrated model. The motivation for the building-up of
	the new model has been pointed out by Voigtlander (Voigtlander,1994)
	where some shortcomings of the nonequilibrium stage model of Krishnamurthy
	and Taylor (Krishnamurth) et a1.,1985) have been claimed. In this
	model no detailed accounting for the plate hydraulics is possible.
	Simulation runs have been made and are compared with experimental
	results.},
  comment = {Apenas versão eletrônica.},
  owner = {Paula},
  pdf = {distillationColumn/Mehlhorn:1996.pdf},
  review = {"The rigorous simulation of distillation with a nonequilibrium model
	has been described by Krishnamurthy and Taylor (Krislmamurthy et
	al., 1985). The main motivation for the launch of this model is to
	avoid the calculation of the separation process by use of stage efficiencies.
	Stage efficiencies do not have any physical explanation and must
	be measured. As they are not the same for each component the calculation
	of multicomponent separation processes might be faulty."},
  timestamp = {2006.08.21}
}

@ARTICLE{Mortaheb:2002,
  author = {H.R. Mortaheb and H. Kosuge and K. Asano},
  title = {Hydrodynamics and mass transfer in heterogeneous distillation with
	sieve tray column},
  journal = {Chemical Engineering Journal},
  year = {2002},
  volume = {88},
  pages = {59--69},
  abstract = {Hydrodynamics and separation performance of a sieve tray column in
	heterogeneous distillation are studied experimentally under total
	reflux conditions. A correlation for clear liquid height in the heterogeneous
	liquid region is obtained by modifying the correlation of the homogeneous
	systems. The volumetric dimensionless diffusion fluxes in the heterogeneous
	liquid region are smaller than those in the homogeneous liquid region.
	This may be due to the mass transfer resistance in the liquid phases.
	
	In order to examine the effect of liquid-phase resistance on separation
	performance, a simulation is carried out by either considering or
	neglecting the liquid-phase resistance. The simulation shows that
	the liquid-phase resistance affects the vapor-phase concentration
	driving forces, volumetric diffusion fluxes and convective mass flux
	in the heterogeneous liquid region. It also shows that the predicted
	top vapor
	
	concentrations and flow rate are in reasonable agreement with the
	experimental data in the heterogeneous liquid region by considering
	the liquid-phase mass transfer resistance.},
  comment = {Apenas versão eletrônica.},
  keywords = {Heterogeneous distillation; Sieve tray; Clear liquid height; Diffusion
	flux; Liquid-phase resistance},
  owner = {Paula},
  pdf = {distillationColumn/Mortaheb:2002.pdf},
  review = {"Heterogeneous distillation is involved in several industrial processes.
	Steam distillation and heterogeneous azeotropic distillation, which
	is used for separation of mixtures that are hardly separated by conventional
	distillation methods, are two examples of the heterogeneous distillation
	processes."},
  timestamp = {2006.08.21}
}

@ARTICLE{Musch:1993,
  author = {H. -E. Musch and M. Steiner},
  title = {Order Reduction of Rigorous Dynamic Models for Distillation Columns},
  journal = {Computers and Chemical Engineering},
  year = {1993},
  volume = {17},
  pages = {S311--S316},
  number = {Suppl.},
  abstract = {A method for order reduction of rigorous dynamic models of distillation
	columns is presented. The approach is a modification and extension
	of the comportamental models presented in 1986 by Benallou et. al.
	Formulating the algebraic equations and the differential equations
	for total holdup for the compartments, but keeping the differential
	equations for concentration dynamics for each tray, Murphree tray
	efficiencies can be used and response accuracy increased. The resulting
	models of substantially lower order show good dynamic and steady-state
	conformity with the complete rigorous model. The example of an industrial
	binary distillation column will demonstrate the effectiveness of
	this approach.},
  comment = {Somente verão impressa. Cópia realizada na cientec.},
  keywords = {Distillation columns; order reduction; compartmental models; dynamic
	simulation; differential-algebraic},
  owner = {Paula},
  timestamp = {2006.09.02}
}

@ARTICLE{Muller:2000,
  author = {Niels P. Müller and Hugo Segura},
  title = {An overall rate-based stage model for cross flow distillation columns},
  journal = {Chemical Engineering Science},
  year = {2000},
  volume = {55},
  pages = {2515--2528},
  abstract = {In this work a nonequilibrium stage model for cross flow distillation
	columns is developed. Concentration gradients on trays are integrated
	analytically for simple flow patterns on the basis of an overall
	rate approach. Empirical mixing corrections for bulk and interface
	concentrations and the assumption of constant interface properties
	of other nonequilibrium stage (NEQ) models are completely avoided.
	Simulations were carried out for two distillation cases of non-ideal
	mixtures. The importance of flow modelling on separation is shown
	and compared with mass transfer cross e!ects. Calculated separations
	for distillation trays, over a wide range of operating conditions,
	suggest that the proposed model provides a better approximation of
	concentration profiles, compared with the multicomponent eficiency
	(MEF) and the NEQ stage model. It is also shown that the eficiency-based
	model may predict incorrect mass transfer directions for trace components;
	this behaviour is caused by neglecting the convective contribution
	in the calculation of multicomponent mass transfer rates.},
  comment = {Apenas versão eletrônica.},
  keywords = {Distillation; Nonequilibrium stage model; Multicomponent eficiency},
  owner = {Paula},
  pdf = {distillationColumn/Muller:2000.pdf},
  review = {"Advances in multicomponent mass transfer theory and the development
	of convenient matrix methods have lead to more realistic stage models,
	known as rate-based models, which use multicomponent mass transfer
	rates rather than empirical eficiency factors, so as to incorporate
	nonequilibrium e!ects."
	
	"The NEQ stage is a lumped variable model, where conservation equations
	are written separately for each phase and the interface as a whole,
	and then solved together with constitutive transport equations. Mixing
	and flow e!ects are considered empirically in the calculation of
	the driving force for mass transfer, where bulk concentrations are
	averaged between inlet and outlet conditions using arbitrary mixing
	parameters. This approach is rigorous only for completely mixed liquid
	and vapour phases, being fundamentally wrong and inadequate for industrial-scale
	trays, as pointed out by Kooijman and Taylor (1995)."},
  timestamp = {2006.08.21}
}

@BOOK{Shankar:1999,
  title = {Data Reconciliation and Gross Error Detection: An Intelligent Use
	of Process Data},
  publisher = {Gulf Professional Publishing},
  year = {1999},
  author = {Narasimhan, Shankar and Jordache, Cornelius},
  month = {November},
  isbn = {0884152553}
}

@ARTICLE{Olsen:1997,
  author = {I. Olsen and G. O. Endrestol and T. Sira},
  title = {A Rigorous and Efficient Distillation Column Model for Engineering
	and Training Simulators},
  journal = CCE,
  year = {1997},
  volume = {21},
  pages = {S193--S198},
  number = {Suppl},
  abstract = {A comprehensive dynamic distillation column model has been developed
	and implemented in the commercial simulator package ProSim. The effectiveness
	and robustness of the model has been proven through several deliveries
	of operator training simulators as well as engineering simulators
	to the process industry. The present paper describes the main model
	equations and the applied solution method. The implemented algorithm
	allows the column model to be combined with a large number of other
	process and instrumentation models in simulators running in real-time
	or faster, with a time step of typically one second. Rigorous equations
	are used for material and energy balances on each tray, together
	with hydraulic correlations describing internal liquid and vapour
	flows. Liquid flows along the column are determined by a single pass
	semi-implicit method where flow influences on liquid levels at the
	tray below are approximately taken into account. Internal vapour
	flows are calculated simultaneously with the solution of mass and
	energy balance equations. The method used is a multi pass shooting
	algorithm where the bottom pressure is adjusted to obtain a given
	overhead vapour flow.},
  comment = {Versão impressa.},
  owner = {Paula},
  pdf = {distillationColumn/Olsen:1997.pdf},
  review = {O artigo apresenta uma modelagem rigorosa, mas com o balanço de energia
	em função da entalpia e não da energia interna. O autor diz que essa
	simplificação não leva a grandes erros desde que o sistema não opere
	em pressões muito elevadas.
	
	Como exemplo, é simulado uma unidade com duas colunas de destilação
	e outros acessórios resultado em um sistema com 226.000 variáveis,
	97.000 parâmetros e 2.200 especificações. Utilizando o método de
	resolução proposto (com a divisão das equações em grupos e resolvidas
	alternativamente), o sistema pode ser simulado em tempo real.}
}

@ARTICLE{Osorio:2004,
  author = {D. Osorio and R. Pérez-Correa and A. Belancic and E. Agosin},
  title = {Rigorous dynamic modeling and simulation of wine distillations},
  journal = FC,
  year = {2004},
  volume = {15},
  pages = {515--521},
  abstract = {A novel simulation strategy for dynamic distillation of complex mixtures,
	such as wine, is proposed and evaluated in terms of computing efficiency
	and accuracy. The model developed describes wine distillation as
	a multicomponent reactive batch distillation process. The simulation
	approach transforms the system of differential algebraic equations
	(DAE) into a set of ordinary differential equations, by pre-solving
	the algebraic equations and replacing them with artificial neural
	networks. This new simulation strategy for wine distillation is 40%
	faster than the rigorous solution of the DAE system, compared at
	the same level of accuracy. The model can be applied to the distillation
	of other spirits or complex mixtures, as well as in other separation
	processes in which the recovery of aromas is essential.},
  comment = {Versão impressa.},
  keywords = {Reactive-batch distillation; Terpenes; Pisco},
  owner = {Paula},
  pdf = {distillationColumn/Osorio:2004.pdf},
  review = {Neste artigo, o autor propõe o uso de redes neurais em combinação
	com o método DDD (direct dynamic derivatives) na resolução de sistemas
	DAE gerados na modelagem de colunas de destilação batelada.
	
	Na modelagem, é considerado um termo de reação que acontece somente
	na fase líquida.
	
	
	Resumindo, o modelo rigoroso é misturado a um modelo empírico, gerado
	pelas variáveis algébricas de VLE via rede neural, para evitar a
	resolução do sistema como um DAE.
	
	
	Os resultados de simulações com esta mescla de modelos é praticamente
	idêntico ao resultado de um modelo rigoroso resolvido normalmente
	com solver DAE.}
}

@MANUAL{Pelegrini:2006,
  title = {EMSO Manual},
  author = {Rafael de Pelegrini Soares},
  month = {September},
  year = {2006},
  comment = {Versão eletrônica.},
  owner = {Paula},
  timestamp = {2006.10.13}
}

@MASTERSTHESIS{Pelegrini:2003,
  author = {Rafael de Pelegrini Soares},
  title = {Desenvolvimento de um Simulador Genérico de Processos Dinâmicos},
  school = {PPGEQ- UFRGS},
  year = {2003},
  comment = {Versão impressa.},
  owner = {Paula},
  timestamp = {2006.10.11}
}

@ARTICLE{Peng:2003,
  author = {Jianjun Peng and Thomas F. Edgar and R. Bruce Eldridge},
  title = {Dynamic rate-based and equilibrium models for a packed reactive distillation
	column},
  journal = {Chemical Engineering Science},
  year = {2003},
  volume = {58},
  pages = {2671--2680},
  abstract = {Dynamic rate-based and equilibrium models were developed for a packed
	reactive distillation column for the production of tert-amyl methyl
	ether (TAME). The two types of models, consisting of diferential
	algebraic equations, were implemented in gPROMS and dynamic simulations
	were carried out to study the dynamic behaviour of reactive distillation
	of the TAME system. The dynamic responses predicted by the two types
	of models are similar in general, with some diferences in steady-state
	values. The influence of manipulated variables, such as distillate
	flow rate, reflux ratio, and reboiler duty, on the dynamic responses
	of the controlled variables (reactant conversion and product purity)
	was studied. The dynamic response of reactant conversion is very
	nonlinear and unconventional, but the response of product purity
	is well approximated by a linear first-order diferential equation.
	The CPU time required to complete a dynamic simulation of the rate-based
	model is at least an order of magnitude higher than that for the
	equilibrium model. Therefore, the dynamic rate-based model is much
	more complicated than the equilibrium model, and simplification of
	the rate-based model is necessary for the implementation of model-based
	control. A new approach was proposed to simplify the dynamic rate-based
	model by assuming that the mass transfer coeficients are time invariant.
	This approach was demonstrated to be superior to the conventional
	simplification methods. It can reduce the number of equations by
	up to two-thirds and still accurately predicts the dynamic behaviour.},
  comment = {apenas versão eletrônica.},
  keywords = {Reactive distillation; Dynamic simulation; Modelling; Process control;
	Rate-based model; Nonlinear dynamics},
  owner = {Paula},
  pdf = {reactivedistillation/Peng:2003.pdf},
  timestamp = {2006.09.22}
}

@ARTICLE{Pinto:1988,
  author = {J. C. Pinto and E. C. {Biscaia Jr.}},
  title = {Order Reduction Strategies for Models of Staged Separation Systems},
  journal = {CCE},
  year = {1988},
  volume = {12},
  pages = {821--8318},
  number = {3},
  comment = {artigo impresso.},
  owner = {Paula},
  timestamp = {2007.08.12}
}

@MANUAL{Ltd.:2004,
  title = {PML: Separation Library},
  author = {{PROCESS S. E. Ltd.}},
  organization = {Bridge Studios},
  address = {107a Hammersmith Bridge Road, London W6 9DA},
  month = {May},
  year = {2004},
  owner = {Paula},
  timestamp = {2006.11.01}
}

@ARTICLE{Ramaswamy:2002,
  author = {R. C. Ramaswamy and D. N. Saraf},
  title = {Reduced Order Modeling of a Crude Distillation Unit for Online Applications},
  journal = {Journal of Chemical Engineering of Japan},
  year = {2002},
  volume = {35},
  pages = {714--728},
  number = {8},
  abstract = {A transport phenomena based process model is a prerequisite for supervisory
	level online process optimization. For real time applications it
	is necessary to have an efficient and robust solution procedure for
	the model equations. A method for the reduction in the number of
	model equations for a crude petroleum distillation unit is reported
	here. The predictions from the rigorous, and several reduced order
	models were compared with the experimental data from an operating
	refinery. The results of the reduced order model not only compared
	favorably with those of the rigorous model but the former was also
	found to be more flexible to tuning with the plant data and showed
	greater tolerance to noisy measurements as compared to the latter.
	Use of empirical thermodynamic relations for VLE (vapor-liquid equilibrium)
	data, and analytical derivatives, choice of independent variables
	and numbering of stages were found to further reduce computation
	time significantly.},
  comment = {Apenas versão eletrônica.},
  keywords = {Distillation; Modeling; Reduced Order Modeling; Online Applications},
  owner = {Paula},
  pdf = {distillationColumn/Ramaswamy:2002.pdf},
  timestamp = {2006.08.28}
}

@ARTICLE{Ramchandran:1995,
  author = {Soundar Ramchandran and R. Russell Rhinehartt},
  title = {A very simple structure for neural network control of distillation},
  journal = {Journal of Process Control},
  year = {1995},
  volume = {5},
  pages = {115--128},
  number = {2},
  abstract = {This paper presents a novel approach for process control that uses
	neural networks to model the steadystate inverse of a process which
	is then coupled with a simple reference system synthesis to generate
	a
	
	multivariable controller. The control strategy is applied to dynamic
	simulations of two methanol-water distillation columns that express
	distinctly different behaviour from each other (one simulates a lab
	
	column, while the second simulates an industrial-scale high-purity
	column). A steady-state process simulation package was used to generate
	all the neural network training data. An efficient training algorithm
	
	based on a nonlinear least-squares technique was used to train the
	networks. The neural network modelbased controllers show robust performance
	for both setpoints and disturbances, and performed better
	
	than conventional feedback proportional-integral (PI) controllers
	with feedforward features.},
  comment = {Apenas versão eletrônica.},
  keywords = {neural networks; distillation; dynamic simulations},
  owner = {Paula},
  pdf = {distillationColumn/Ramchandran:1995.pdf},
  timestamp = {2006.08.24}
}

@ARTICLE{Rao:2001,
  author = {D.P. Rao and C.V. Goutami and S. Jain},
  title = {A direct method for incorporation of tray-efficiency matrix in simulation
	of multicomponent separation processes},
  journal = {Computers and Chemical Engineering},
  year = {2001},
  volume = {25},
  pages = {1141--1152},
  abstract = {Both experimental and estimated multicomponent tray efficiencies are
	known to become unbounded and exhibit bizarre variation from tray
	to tray in a distillation column even for ideal systems. Besides
	lacking the physical significance, they pose numerical difficulties
	in computation of the component tray efficiencies from the point
	efficiencies whenever the latter assume negative values (Lockett,
	M. J. (1986). Distillation tray fundamentals. Cambridge: Cambridge
	University Press). The use of the Stefan-Maxwell approach for estimation
	of point efficiency leads to a matrix form. Recently, the tray-efficiency
	matrix for well-mixed, dispersed and plug flow of liquid has been
	obtained in terms of point-efficiency matrix similar to binary systems.
	However, there are no method to use directly the tray-efficiency
	matrix in simulation. Here, we present a method for direct incorporation
	of the efficiency matrix in the well-known Naphtali-Sandholm method.
	We have studied the convergence characteristics of the modified and
	the original methods for distillation, absorption and extraction
	columns. The results show the modified one is superior to the original
	method.},
  comment = {Apenas versão eletrônica.},
  keywords = {Simulation; Distillation; Absorption; Extraction; Separations; Tray-efficiency},
  owner = {Paula},
  pdf = {distillationColumn/Rao:2001.pdf},
  review = {"..., the multicomponent mass transfer theory suggests that the natural
	extension of the Murphree tray efficiency from binary to multicomponent
	system would take a matrix form (Taylor and Krishna, 1993). The diagonal
	elements reflect the contacting efficiency of the phases on the tray
	and the off-diagonal elements the multicomponent interaction effects."},
  timestamp = {2006.08.22}
}

@ARTICLE{Rao:1995,
  author = {D. P. Rao and R. S. Prem Kumar and P. Pandit and T. C. T. Das},
  title = {Multicomponent tray efficiencies accounting for entrainment},
  journal = {The Chemical Engineering Journal},
  year = {1995},
  volume = {57},
  pages = {237--246},
  abstract = {In multicomponent distillation, the component point efficiencies are
	highly sensitive to the composition profiles and are known to exhibit
	bizarre behavior. A major limitation of these efficiencies is the
	fact that cannot be related to tray efficiencies for dispersed and
	plug-flow of liquid, unless multicomponent effects are ignored -
	these would still pose a problem if the component point efficiencies
	assume large negative values. The Maxwell-Stephan approach to diffusion
	on multicomponent mixtures leads to a component point efficiency
	matrix from a point efficiency matrix for dispersed flow and plug
	flow or a liquid phase, and accounting for entrainment. The results
	of the simulation of the fractionation of two ideal and two non-ideal
	mixtures indicated the superiority of the matrix approach over the
	use of component efficiencies.},
  comment = {Apenas versão eletrônica.},
  keywords = {Multicomponent; Distillation; Entrainment; Composition profiles},
  owner = {Paula},
  pdf = {distillationColumn/Rao:1995.pdf},
  review = {Apresenta uma introdução muito boa.
	
	os "rated based models" são os modelos que não dependem de uma eficiência
	a ser setada ou calculada. São os modelos reais.
	
	
	O artigo trata da estimação da eficiência de prato através da eficiência
	de ponto para modelos de pratos reais levando em conta o arraste
	de líquido.
	
	O equacionamento é apresentado.},
  timestamp = {2006.08.21}
}

@ARTICLE{Ray:1996,
  author = {S. Ray and S. P. Sengupta},
  title = {Irreversibility analysis of a sieve tray in a distillation column},
  journal = {Int. J. Heat Mass Transfer},
  year = {1996},
  volume = {39},
  pages = {1535--1542},
  number = {7},
  abstract = {A second Law analysis has been developed for a vapor-liquid contacting
	device as in the sieve tray of a distillation column. Using a discrete
	bubble dynamics model, an equation for entropy balance has been formulated
	to numerically evaluate the entropy generation rate associated with
	heat, mass and momentum transfer for bubble movement through a moving
	liquid pool. The entropy generation rates per unit bubble mass have
	been evaluated for variations in sieve tray parameters like orifice
	diameter and weir height for fixed separation characteristics of
	components constituting the two pfiases. It has been found that among
	the tray parameters, weir height plays a dominant role compared to
	sieve hole diameter on entropy generation.},
  comment = {Apenas versão eletrônica.},
  owner = {Paula},
  pdf = {distillationColumn/Ray:1996.pdf},
  review = {Artigo que analisa a irreversibilidade na formação das bolhas de vapor
	no líquido.},
  timestamp = {2006.08.22}
}

@ARTICLE{Reepmeyer:2004,
  author = {Frauke Reepmeyer and Jens-Uwe Repke and Günter Wozny},
  title = {Time optimal start-up strategies for reactive distillation columns},
  journal = {Chemical Engineering Science},
  year = {2004},
  volume = {59},
  pages = {4339 --4347},
  abstract = {In this contribution, a rigorous process model to simulate the start-up
	of a cold and empty reactive distillation (RD) column is developed
	and experimentally validated with a transesterification process.
	Strategies for time optimal start-up of an RD column are presented.
	The mostly used strategy for conventional distillation of total reflux
	for RD is only recommendable with limitations. New, alternative strategies,
	like the recycling of the off-spec bottom and top product or the
	initial charging with product, to minimize the necessary start-up
	time are presented. Suitable strategies can save up to 82% of the
	needed time for the column start-up.},
  comment = {Versão Impressa.},
  keywords = {Reactive distillation; Start-up; Dynamic simulation; Ethyl acetate;
	Transesterification},
  owner = {Paula},
  pdf = {reactivedistillation/Reepmeyer:2004.pdf},
  timestamp = {2006.08.25}
}

@ARTICLE{Reepmeyer:2003,
  author = {Frauke Reepmeyer and Jens-Uwe Repke and Günter Wozny},
  title = {Analysis of the Start-up Process for Reactive Distillation},
  journal = {Chemical Engineering Technology},
  year = {2003},
  volume = {26},
  pages = {81--86},
  comment = {Versão impressa.},
  owner = {Paula},
  pdf = {reactivedistillation/Reepmeyer:2003.pdf},
  timestamp = {2006.08.25}
}

@ARTICLE{Resjorde:2005,
  author = {A. Resjorde and S. Kjelstrup},
  title = {The second lawoptimal state of a diabatic binary tray distillation
	column},
  journal = {Chemical Engineering Science},
  year = {2005},
  volume = {60},
  pages = {1199--1210},
  abstract = {A new numerical procedure to minimize the entropy production in diabatic
	tray distillation columns has been developed. The method was based
	on a least square regression of the entropy production at each tray.
	A diabatic column is a column with heat exchangers on all trays.
	The method was demonstrated on a distillation column separating propylene
	from propane. The entropy production included contributions from
	the heat transfer in the heat exchangers and the mass and heat transfer
	between liquid and vapor inside the distillation column. It was minimized
	for a number of binary tray distillation columns with fixed heat
	transfer area, number of trays, and feed stream temperature and composition.
	For the first time, the areas of heat exchange were used as variables
	in the optimization. An analytical result is that the entropy production
	due to heat transfer is proportional to the area of each heat exchanger
	in the optimal state. For many distillation columns, this is equivalent
	to a constant driving force for heat transfer. The entropy production
	was reduced with up to 30% in the cases with large heat transfer
	area and many trays. In large process facilities, this reduction
	would ideally lead to 1-2GWh of saved exergy per year. The most important
	variable in obtaining these reductions is the total heat transfer
	area. The investigation was done with a perspective to later include
	the column as a part in an optimization of a larger process. We found
	that the entropy production of the column behaved almost as a quadratic
	function when the composition of the feed stream changed. This means
	that the feed composition is a natural, easy variable for a second
	law optimization when the distillation column is a part of a process.
	The entropy production was insensitive to variations in the feed
	temperature.},
  comment = {Apenas versão eletrônica.},
  keywords = {Distillation; Energy; Entropy production; Mathematical; Second law;
	Optimization},
  owner = {Paula},
  pdf = {distillationColumn/Resjorde:2005.pdf},
  review = {"The aim of this work is to contribute to a better energy economy
	of distillation by increasing the energy efficiency. Maximum efficiency
	is found by minimizing the entropy production in diabatic columns.
	We continue the work by De Koeijer et al. (2004), who minimized the
	entropy production in diabatic distillation columns. We shall add
	to earlier work and show how we can determine, by theory and calculation,
	the optimal area of heat exchange at each tray. A new numerical solution
	procedure shall also be reported.We will not yet include aspects
	related to the practical implementation (like controllability and
	cost) in this study."
	
	
	O artigo mostra o equacionamento de uma forma clara.
	
	
	"We observed that the entropy production of the column behaved almost
	as a quadratic function when the composition of the feed stream changed.
	This means that the feed composition easily can be used as variable
	when a distillation column is part of a process optimization. Surprisingly,
	the entropy production was almost independent of the feed temperature."},
  timestamp = {2006.08.22}
}

@ARTICLE{Roffel:2000,
  author = {B. Roffel and B.H.L. Betlem and J.A.F. de Ruijter},
  title = {First principles dynamic modeling and multivariable control of a
	cryogenic distillation column process},
  journal = CCE,
  year = {2000},
  volume = {24},
  pages = {111--123},
  abstract = {In order to investigate the feasibility of constrained multivariable
	control of a heat-integrated cryogenic distillation process, a rigorous
	first principles dynamic model was developed and tested against a
	limited number of experiments. It was found that the process variables
	showed a large amount of interaction, which is responsible for the
	difficulties with the presently used, PID-based, control scheme,
	especially in load-following situations, which are common in air
	separation plants such as for instance integrated coal gasification
	combined cycle plants. Contrary to what is suggested in the literature,
	it was found that vapor hold-up in low-temperature, high-pressure
	columns does not play a significant role in the process dynamics.
	Despite large throughput changes and non-linear process behavior,
	multivariable model predictive control using a linearized model for
	average operating conditions, could work well provided all process
	flows have sufficient range. Due to the strong interactive nature
	of the process variables, process changes have to be made slowly,
	since otherwise manipulated variables easily saturate and process
	output targets cannot be maintained.},
  comment = {Versão impressa.},
  keywords = {Dynamic modeling; Multivariable control; Cryogenic distillation},
  owner = {Paula},
  pdf = {distillationColumn/Roffel:2000.pdf},
  review = {Destilação criogênica é semelhante à destilação convencional, mas
	acontece em baixíssimas temperaturas. Ela é necessária quando se
	quer separar ar, por exemplo, em oxigênio e nitrogênio. Apenas em
	temperaturas na ordem de 100K (-173°C) estes componentes se tornam
	líquidos e podem ser separados.
	
	
	A coluna de destilação criogênica apresenta uma configuração diferente.
	O condensador e o refervedor são integrados e se encontram no meio
	da coluna dividindo a mesma em duas. Estas "duas colunas" têm a sua
	operação em diferentes pressões, sendo a parte inferior com maior
	pressão e a parte superior com nemor pressão.
	
	A modelagem do condensador/refervedor é apresentada.
	
	Testes são feitos para provar que o efeito da desconsideração do acúmulo
	de vapor no prato é insignificante, ao contrário do que diz a literatura
	para colunas que operam em altas pressões.
	
	
	É feito também um estudo a cerca do controle do sistema.
	
	
	ESTE ARTIGO APRESENTA UMA SÉRIE DE EQUAÇÕES DE HIDRÁULICA MUITO INTERESSANTE!!}
}

@ARTICLE{Ruiz:1988,
  author = {C. A. Ruiz and I. T. Cameron and R. Gani},
  title = {A Generalized Model for Distillation Columns - III - Study of Start-up
	Operations},
  journal = CCE,
  year = {1988},
  volume = {12},
  pages = {1--14},
  number = {1},
  abstract = {The dynamic behavior of distillation columns during startup operations
	have been studied and analyzed. A procedure is proposed for determining
	appropriate startup policies for distillation column operations based
	on the analysis of the dynamic behavior. The final startup policy
	consists of three strategies corresponding to the three characteristic
	stages of the stratup operation. The proposed procedure has been
	successfully applied to a test problem. Numerical results of the
	dynamic behavior and the test problem are presented.},
  comment = {Foi adquirido na CIENTEC. Apenas cópia impressa.},
  owner = {Paula},
  review = {Neste artigo, todos os valores das variáveis básicas (de vazão, pressão,
	etc...) são analisadas através de gráficos de simulações de partidas.
	
	
	O autor divide a partida de uma coluna de destilação em três estágios.
	São eles:
	
	- Estágio Discontínuo: caracterizado pelo curto período de tempo de
	duração e pela natureza de discontinuidade de praticamente todas
	as variáveis (principalmente as relacionadas à hidráulica)
	
	- Estágio Semi-Contínuo: é caracterizado pela variação não linear
	das variáveis, mas sem descontinuidades, e pela aproximação do valor
	estacionário das variáveis hidráulicas. Este período tem uma maior
	duração de tempo.
	
	- Estágio Contínuo: é caracterizado pelo transiente linear das variáveis.
	No final desta etapa todas as variáveis atingem o estado estacionário.
	
	
	Baseado na análise dinâmica da partida, o procedimento de partida
	de uma coluna é partido em três etapas que coincidem com os estágios
	descritos acima. Na primeira etapa, o procedimento mais adequado
	é o que causa o mímino de problemas de operação, garantindo que não
	haverão descontinuidades no final deste período. Na segunda etapa
	o sistema de controle entra em ação para que este estágio seja ultrapassado
	com o mínimo custo de operação. No início da terceira etapa o sistema
	de controle é ligado e o sistema é mantido em torno do estado estacionário
	desejado.
	
	
	Para obter o melhor procedimento para a partida de uma coluna, é utilizada
	otimização.
	
	Aspectos numéricos são relatados.}
}

@ARTICLE{Sage:1940,
  author = {Sage,B.H. and W.N.Lacey},
  journal = {Industrial \& Engineering Chemistry Research},
  year = {1940},
  volume = {32},
  pages = {992},
  owner = {Paula},
  timestamp = {2007.09.10}
}

@INPROCEEDINGS{Soares:2003,
  author = {R. P. Soares and A. R. Secchi},
  title = {EMSO: A New Environment for Modelling, Simulation, and Optimisation},
  booktitle = {ESCAPE 13th},
  year = {2003},
  volume = {1},
  pages = {947--952},
  publisher = {Elsevier Science Publishers},
  comment = {Pegar versão com o Rafael.},
  owner = {Paula}
}

@ARTICLE{Soave:2002,
  author = {Giorgio Soave and Josep A. Feliu},
  title = {Saving energy in distillation towers by feed splitting},
  journal = {Applied Thermal Engineering},
  year = {2002},
  volume = {22},
  pages = {889--896},
  abstract = {It is a common procedure to save energy in industrial distillation
	towers by preheating the feed with heat recovered from the bottom
	product. It will be demonstrated theoretically, and shown by simulation
	means,
	
	that if, before entering the unit, the feed is split into two streams,
	and only one of them is preheated, further savings of energy (up
	to 50%) can be achieved. The use of a steady state process simulator
	like Hysys is precious for a fast and reliable determination of the
	optimum split ratio and feed tray. A typical example of application
	is given and the use of Hysys shown. The results for the optimization
	of the split ratio are provided showing the economical impact of
	the proposed solution.},
  comment = {Apenas versão eletrônica.},
  keywords = {Energy savings; Feed splitting; Process simulation},
  owner = {Paula},
  pdf = {distillationColumn/Soave:2002.pdf},
  timestamp = {2006.08.22}
}

@ARTICLE{Srivastava:1987,
  author = {R. K. Srivastava and B. Joseph},
  title = {Reduced-order Models for separation columns - VI. Columns with steep
	and flat composition profiles},
  journal = {Computers and Chemical Engineering},
  year = {1987},
  volume = {11},
  pages = {165--176},
  number = {2},
  comment = {Apenas versão impressa. Retirado da CIENTEC.},
  owner = {Paula},
  timestamp = {2006.09.15}
}

@ARTICLE{Srivastava:1985,
  author = {R. K. Srivastava and B. Joseph},
  title = {Reduced-order Models for separation columns - V. Selections of collocation
	points},
  journal = {Computers and Chemical Engineering},
  year = {1985},
  volume = {9},
  pages = {601--613},
  number = {6},
  comment = {Apenas versão impressa. Retirado da CIENTEC.},
  owner = {Paula},
  timestamp = {2006.09.15}
}

@ARTICLE{Stewart:1985,
  author = {Warren E. Stewart and Keith L. Levien and Manfred Morari},
  title = {Simulation of fractionation by orthogonal collocation},
  journal = CES,
  year = {1985},
  volume = {40},
  pages = {409--421},
  number = {3},
  abstract = {An orthogonal collocation method is given for rapid simulation of
	multistage separation schemes. The grid points for each multistage
	module are selected by a stage wise least squares ctiterion. Refinement
	of the grid yields rapid convergence to the full stagewise solution.
	Calculations show that the method is remarkably efficient, both for
	steady and dynamic simulations of distillation columns.},
  comment = {Apenas versão impressa. Retirado da CIENTEC.},
  owner = {Paula},
  timestamp = {2006.08.24}
}

@BOOK{Sundmacher:2003,
  title = {Reactive Distillation - Status and Future Directions},
  publisher = {Wiley - VCH Verlag GmbH \& Co. KGaA},
  year = {2003},
  editor = {Kai Sundmacher and Achim Kienle},
  author = {Kai Sundmacher and Achim Kienle},
  comment = {versão eletrônica.},
  owner = {Paula},
  pdf = {reactivedistillation/Sundmacher:2003.pdf},
  timestamp = {2006.09.22}
}

@TECHREPORT{Suppes:2002,
  author = {Galen J. Suppes},
  title = {Selecting Thermodynamic Models for Process Simulation of Organic
	VLE and LLE Systems},
  institution = {Department of Chemical Engineering The University of Missouri-Columbia},
  year = {2002},
  month = {September},
  comment = {Versão impressa.},
  owner = {Paula},
  pdf = {thermodynamic/Suppes:2002.pdf},
  review = {O texto propõe que sejam utilizadas as propriedades críticas dos componentes
	da mistura para ajudar na seleção do método de cálculo mais adequado
	através da regra de Kay.},
  timestamp = {2006.08.22}
}

@ARTICLE{Taylor:2000,
  author = {R. Taylor and R. Krishna},
  title = {Modelling reactive distillation},
  journal = {Chemical Engineering Science},
  year = {2000},
  volume = {55},
  pages = {5183--5229},
  abstract = {The design and operation issues for reactive distillation systems
	are considerably more complex than those involved for either conventional
	reactors or conventional distillation columns. The introduction of
	an in situ separation function within the reaction zone leads to
	complex interactions between vapor-liquid equilibrium, vapor-liquid
	mass transfer, intra-catalyst di!usion (for heterogeneously catalysed
	processes) and chemical kinetics. Such interactions have been shown
	to lead to the phenomenon of multiple steady-states and complex dynamics,
	which have been verified in experimental laboratory and pilot plant
	units. We trace the development of models that have been used for
	design of reactive distillation columns and suggest future research
	directions.},
  comment = {versão impressa.},
  keywords = {Reactive distillation; Equilibrium stage model; Non-equilibrium stage
	model; Multiple steady-states; Maxwell-Stefan equations},
  owner = {Paula},
  pdf = {reactivedistillation/Taylor:2000.pdf},
  timestamp = {2006.09.22}
}

@ARTICLE{Trotta:1995,
  author = {Antonio Trotta and Massimiliano Barolo},
  title = {Nonlinear Model-Based Control of a Binary Distillation Column},
  journal = {Computers and Chemical Engineering},
  year = {1995},
  volume = {19},
  pages = {S519--S524},
  abstract = {This paper concerns the control of both product purities of a binary
	distillation column. Refiux and boilup flow rates are chosen as manipulated
	variables, and the corresponding control laws are derived within
	the Globally Linearizing Control framework. Reduced order models
	of the column are developed that allow the controller synthesis to
	be carried out easily. Simulation results indicate that the proposed
	control strategy outperforms a conventional PI control strategy by
	a significant amount.},
  comment = {Apenas versão eletrônica.},
  keywords = {Distillation; nonlinear control; model-based control; globally linearizing
	control},
  owner = {Paula},
  pdf = {distillationColumn/Trotta:1995.pdf},
  timestamp = {2006.08.28}
}

@ARTICLE{Traenkle:1997,
  author = {F. Tränkle and A. Gerstlauer and M. Zeitz and E.D. Giiles},
  title = {Application of the Modeling and Simulation Environment PROMOT/DIVA
	to the Modeling of Distillation Processes},
  journal = {Computers chem. Engng},
  year = {1997},
  volume = {21},
  pages = {S841--S846},
  number = {Suppl.},
  abstract = {In this contribution, the application of the computer-aided modeling
	and simulation environment PROMOT/DIVA to the modeling of (reactive)
	distillation processes is presented. The main focus is on the description
	of the underlying modeling concept, together with some implications
	of this concept for the modeling of distillation processes. One important
	point of the modeling concept and the subsequent design of the knowledge
	base of PROMOT is the decomposition of individual process units into
	physically meaningful, finer grained modeling entities on different
	hierarchical levels. The hierarchical levels considered thus far
	are the process unit level, the phase level, and the storage level.
	This contribution focuses mainly on the definition of the modeling
	entities on the phase level, which are important for the modeling
	of (reactive) distillation processes. Furthermore, the design of
	the object-oriented knowledge base of PRoMoT that contains these
	modeling entities is illustrated.},
  comment = {Versão impressa.},
  owner = {Paula},
  pdf = {distillationColumn/Traenkle:1997.pdf},
  review = {Ler com mais atenção.},
  timestamp = {2006.08.22}
}

@INPROCEEDINGS{Tummescheit:1997,
  author = {Hubertus Tummescheit and Matthias Klose and Thilo Ernst},
  title = {Modelica and Smile - a Case Study Applying Object-Oriented Concepts
	to Multi-Facet Modeling},
  booktitle = {9th European Simulation Symposium ESS97},
  year = {1997},
  month = {October},
  abstract = {A new language called Modelica for hierarchical physical modeling
	is developed in an international effort. The main objectives are
	to make it easy to exchange models and
	
	model libraries between tools and to use object-oriented constructs
	to facilitate the reuse of modeling knowledge. The design approach
	joins the concepts of non-causal modeling with ordinary differential
	and algebraic equations with object-oriented model structuring facilities.
	Modelica's language features are compared to the features of Smile,
	one of the existing object-oriented modeling languages available
	from the TU of Berlin and GMD FIRST. The Smile environment is used
	at DLR Cologne for the modeling of solar thermal power plants, but
	the Smile development team plans to extend the environment with theModelica
	language (Ernst, T.,S. Jähnichen, M. Klose 1997). The example of
	a simple stove with electrical plates is used to point out the new
	model structuring possibilities. A tank system with a centrifugal
	pump is used to demonstrate new possibilities of modeling using genericity
	and inheritance.},
  comment = {Versão impressa.},
  owner = {Paula},
  pdf = {softwares/Tummescheit:1997.pdf},
  timestamp = {2006.09.15}
}

@ARTICLE{Vogelpohl:1999,
  author = {Alfons Vogelpohl},
  title = {A unified description of the distillation of ideal mixtures},
  journal = {Chemical Engineering and Processing},
  year = {1999},
  volume = {38},
  pages = {631--634},
  abstract = {It is shown that the distillation of multicomponent ideal mixtures
	may be regarded as a superposition of the distillation of ternary
	mixtures and that the equation describing the distillation of ternary
	mixtures may be reduced to one single fundamental equation. This
	fundamental equation contains the lightest, the heaviest and one
	intermediate boiling component and is equally valid for distillation
	based on theoretical trays as well as packings. It applies to the
	distillation at total and finite reflux and also includes the limiting
	cases of reversible distillation or distillation with a mass transfer
	resistance either on the gas or on the liquid
	
	side. This reduction of the distillation of multicomponent mixtures
	to the distillation of a ternary mixture and to one single equation
	greatly simplifies the understanding of the complexities of multicomponent
	distillation.},
  comment = {Apenas versão eletrônica.},
  keywords = {Distillation; Multicomponent ideal mixtures},
  owner = {Paula},
  pdf = {distillationColumn/Vogelpohl:1999.pdf},
  review = {Artigo que trata de uma modelagem gráfica baseada em diagramas ternários
	e em relações de equilíbrio simples.},
  timestamp = {2006.08.22}
}

@UNPUBLISHED{VRTech:2005,
  author = {VRTech},
  title = {VRTherm, a software to predict thermodynamic and physical properties
	of complex mixtures and pure substances},
  note = {www.vrtech.com.br},
  year = {2005},
  owner = {Paula},
  timestamp = {2006.08.25}
}

@ARTICLE{Wang:2003,
  author = {Lin Wang and Pu Li and Günter Wozny and Shuqing Wang},
  title = {A start-up model for simulation of batch distillation starting from
	a cold state},
  journal = {Computers and Chemical Engineering},
  year = {2003},
  volume = {27},
  pages = {1485--1497},
  abstract = {Batch distillation columns are frequently started up with a different
	initial reboiler charge. A proper initial state is required for simulation
	and optimization of such processes, but it has been a non-trivial
	task to obtain it. In this work, a model to express startup behaviors
	of batch columns starting from an empty cold state is proposed to
	address this issue. Each tray is described beginning with a non-equilibrium
	phase in which only mass and energy transfer is taking place, to
	an equilibrium phase in which the vapor-liquid equilibrium is being
	held. The switching point between these two phases is determined
	by the bubble-point temperature at the operating pressure. The equilibrium
	state is reached tray by tray from bottom to top of the column, while
	the liquid holdup on the trays is mainly filled in the opposite direction.
	A difficulty in solving the model equations is that the number of
	variables of the trays is not the same when their state switches
	from a phase to another. Trivial equations are introduced to deal
	with this problem gPROMS is used as the simulation platform. The
	startup of a three-component batch distillation column is simulated
	with this model and the results are compared with those from an equilibrium
	model. The model proposed is verified through experiment on a pilot
	batch plant with a bubble-cap tray column to separate a methanol/water
	mixture.},
  comment = {Apenas versão eletrônica.},
  keywords = {Batch distillation; Startup; Cold state; Non-equilibrium; Phase transition;
	Modeling; Simulation; gPROMS; Experimental verification},
  owner = {Paula},
  pdf = {distillationColumn/Wang:2003.pdf},
  timestamp = {2006.08.22}
}

@ARTICLE{Wijn:1998,
  author = {E.F. Wijn},
  title = {On the lower operating range of sieve and valve trays},
  journal = {Chemical Engineering Journal},
  year = {1998},
  volume = {70},
  pages = {143--155},
  abstract = {A model of the lower operating Iimits of distillation and absorption
	trays is described in this paper. The model requires the simultaneous
	solution of two equations describing ( 1) liquid flow across the
	tray and over the outlet weir, and (2) countercurrent liquid flow
	through the free hole area of the tray. The second equation stems
	from models of a tray without downcomers; this equation was validated
	by means of available test data. The model gives liquid height and
	weep fraction as a function of gas and liquid flow rates, for a given
	tray layout. As shown, it permits calculation of the gas flow rate
	at weep and seal point, in a coherent way. Examples illustrate the
	use of the method in calculating the position of the weeping range
	of a tray and its relation to tray efficiency.},
  comment = {Apenas versão eletrônica.},
  keywords = {Absorption; Distillation; Dumping; Seal point; Sieve tray; Valve tray;
	Weeping; Weep point},
  owner = {Paula},
  pdf = {distillationColumn/Wijn:1998.pdf},
  review = {Não li o artigo.},
  timestamp = {2006.08.22}
}

@ARTICLE{Wijn:1999,
  author = {E. F. Wijn},
  title = {Weir flow and liquid height on sieve and valve trays},
  journal = CEJ,
  year = {1999},
  volume = {73},
  pages = {191--204},
  abstract = {Mechanisms for the flow of liquid over outlet weirs of distillation
	and absorption trays are described in this paper. Weir flow contributes
	to the liquid height on a tray, and this height is important for
	the design and operation of trayed columns. Comparisons of available
	experimental data with Francis' weir equation and with new stochastic
	liquid flow models showed that the traditionally used Francis' equation
	needs modifcation. The stochastic flow models link the weir flow
	to the flow mechanisms upstream of the tray outlet. These upstream
	mechanisms provide the input needed for a new weir crest equation.
	The existence of a so-called 'edge-vortex' (a horizontal roll cell
	at the boundary of the gassed and the ungassed region) is shown to
	play an important role, when a calming zone is present upstream of
	the outlet weir.},
  comment = {Versão impressa.},
  keywords = {Calming zone; Distillation; Liquid height; Regime; Sieve tray; Spray;
	Valve tray; Weir},
  owner = {Paula},
  pdf = {distillationColumn/Wijn:1999.pdf},
  review = {Não li o artigo.}
}

@ARTICLE{Wijn:1996,
  author = {E. F. Wijn},
  title = {The effect of downcomer layout pattern on tray efficiency},
  journal = {The Chemical Engineering Journal},
  year = {1996},
  volume = {63},
  pages = {167--180},
  abstract = {A multi-branch/multi-cell model has been developed and used to evaluate
	the tray efficiency for examples of distillation trays with different
	layouts of the downcomer areas. The multi-branch/multi-cell model
	predicts that the trays with different downcomer area distribution
	patterns do have a different tray efficiency. Hence, it can help
	in the identification of the most efficient downcomer layout pattern
	and in the quantification of the expected efficiencies differences.},
  comment = {Apenas versão eletrônica.},
  keywords = {Downcomer layout pattern; Tray efficiency; Distillation columns},
  owner = {Paula},
  pdf = {distillationColumn/Wijn:1996.pdf},
  review = {Não li o artigo.},
  timestamp = {2006.08.22}
}

@ARTICLE{Wozny:2004,
  author = {Günter Wozny and Pu Li},
  title = {Optimisation and experimental verification of start-up policies for
	distillation columns},
  journal = {Computers and Chemical Engineering},
  year = {2004},
  volume = {28},
  pages = {253--265},
  abstract = {Startup of distillation columns is one of the most difficult operations
	in the chemical industry. Since the startup often lasts a long period
	of time, leads to off-spec products, and costs much energy, optimisation
	of startup operating policies for distillation columns is of great
	interest. In the last few years, we have carried out both theoretical
	studies and experimental verifications with the purpose of minimising
	the startup time of distillation columns. Model-based optimisation
	as well as real plant implementation is the core of this work. The
	model is at first validated with experimental data and then used
	in the optimisation problem formulation. A rigorous column model
	and a sequential dynamic optimisation approach have been applied
	to several pilot distillation columns. Experimental results indicate
	that a significant reduction of the startup time can be achieved
	by implementing the developed optimal policies. These results demonstrate
	the applicability of the modelling and optimisation methodology.},
  comment = {Versão impressa.},
  keywords = {Startup; Distillation column; Modelling; Optimisation; Experimental
	verification},
  owner = {Paula},
  pdf = {reactivedistillation/Wozny:2004.pdf},
  timestamp = {2006.09.14}
}

@ARTICLE{Yang:1997,
  author = {Dae Ryook Yang and Kwang Soon Lee},
  title = {Monitoring of a Distillation Column Using Modified Extended Kalman
	Filter and a Reduced Order Model},
  journal = {Computers and Chemical Engineering},
  year = {1997},
  volume = {21},
  pages = {S565--S570},
  number = {Suppl.},
  abstract = {An efficient model reduction technique for the distillation columns
	is applied to account for the detail dynamics. This technique utilizes
	the orthogonal collocation and cubic spline method. Then the extended
	Kalman filter is applied to identify the model parameters and the
	feed composition from the measurements of the column. From the simulation,
	the model reduction technique can account for the detail dynamics
	of the rigorous distillation model and not only the model parameters,
	but also the feed composition can be identified by the recursive
	prediction error method.},
  comment = {Apenas versão eletrônica.},
  owner = {Paula},
  pdf = {distillationColumn/Yang:1997.pdf},
  timestamp = {2006.08.28}
}

@ARTICLE{Yasuoka:1982,
  author = {H. Yasuoka and E. Nakanishi},
  title = {A convenient algorithm for the online optimum start-up operation
	of binary distillation.},
  journal = {Memoirs of the Faculty of the Engineering, Kobe University},
  year = {1982},
  volume = {29},
  pages = {161--169},
  comment = {Apenas utilizado como apud.},
  owner = {Paula},
  timestamp = {2006.08.25}
}

@ARTICLE{Zhang:2004,
  author = {Libin Zhang and Andreas A. Linninger},
  title = {Temperature Collocation Algorithm for Fast and Robust Distillation
	Design},
  journal = {Ind. Eng. Chem. Res},
  year = {2004},
  volume = {43},
  pages = {3163--3182},
  abstract = {In this paper, we describe a new minimum bubble-point distance (MIDI)
	algorithm for assessing the feasibility of a desired distillation
	specification. The algorithm computes the rectifying and stripping
	temperature profiles by temperature collocation on finite elements
	with orthogonal polynomials. We discovered the beneficial use of
	a dimensionless equilibrium tray temperature as an independent variable.
	This novel choice is bounded between 0 and 1, improves the numerical
	quality of the design problem formulation, and is well-behaved even
	in the vicinity of pinch regions. It also employs the fixed points
	of column sections as collocation points. Adaptive-element boundary
	placement at saddle temperatures can effectively overcome problems
	with numerical instability near pinch regions. Extensions of our
	MIDI algorithm to the calculation of the minimum and maximum refluxes
	are also introduced. We show the application of this algorithm in
	the separation of quaternary mixtures and provide an outlook of the
	methodology for optimal column sequencing. Cases studies demonstrate
	the algorithm robustness and reliability.},
  comment = {Apenas versão eletrônica.},
  owner = {Paula},
  pdf = {distillationColumn/Zhang:2004.pdf},
  timestamp = {2006.08.28}
}

@comment{jabref-meta: groupsversion:3;}

@comment{jabref-meta: groupstree:
0 AllEntriesGroup:;
1 ExplicitGroup:Real Distillation\;0\;Baur:2000\;Baur:2000a\;Biardi:19
89\;Eckert:2001\;Higler:1999\;Higler:1999_dissertation\;Koeijer:2004\;
Kooijman:1995\;Kooijman:1995a\;Lee:1998\;Mehlhorn:1996\;Muller:2000\;P
eng:2003\;Rao:1995\;Rao:2001\;;
1 ExplicitGroup:Hidraulics\;0\;Betlem:1998\;Chang:1998\;Hongyan:2002\;
Lockett:1986\;Wijn:1996\;Wijn:1998\;Wijn:1999\;;
1 ExplicitGroup:Miscellaneous\;0\;Brooks:1993\;Gross:1998\;Grossmann:2
005\;Jobson:1997\;Kaeser:2006\;Kiva:1997\;Liu:2000\;Luyben:2006\;Morta
heb:2002\;Soave:2002\;Suppes:2002\;Traenkle:1997\;Vogelpohl:1999\;;
1 ExplicitGroup:Numerical Aspects\;0\;Cameron:1986\;Fletcher:2000\;;
1 ExplicitGroup:Azeotropic\;0\;Castillo:1998\;;
1 ExplicitGroup:Startup-shutdown\;0\;Chang:1998\;Elgue:2004\;Reepmeyer
:2003\;Reepmeyer:2004\;Ruiz:1988\;Wang:2003\;Wozny:2004\;Yasuoka:1982\
;;
1 ExplicitGroup:LLE\;0\;Eckert:1995\;Eckert:2001\;Gumus:1997\;;
1 ExplicitGroup:Batch Distillation\;0\;Elgue:2004\;Kim:1999\;Klingberg
:2000\;Mehlhorn:1996\;Wang:2003\;;
1 ExplicitGroup:Equilibrium Distillation\;0\;Elgue:2004\;Gani:1986\;Ga
ni:1989\;Kim:1999\;Klingberg:2000\;Olsen:1997\;Osorio:2004\;Roffel:200
0\;Wang:2003\;;
1 ExplicitGroup:SS simulation\;0\;Carta:1995\;Dave:2003\;Eiden:1997\;F
letcher:2000\;Gani:1989\;Kooijman:1995a\;McKay:1997\;Ramchandran:1995\
;Stewart:1985\;;
1 ExplicitGroup:Irreversible Thermodynamics\;0\;Koeijer:2004\;Ray:1996
\;Resjorde:2005\;;
1 ExplicitGroup:low-order model\;0\;Benallou:1986\;Betlem:2000\;Cho:19
84\;Diwekar:1987\;Huss:1996\;Kienle:2000\;Musch:1993\;Ramaswamy:2002\;
Stewart:1985\;Trotta:1995\;Zhang:2004\;;
1 ExplicitGroup:Reactive Distillation\;0\;Alejski:1996\;Alfradique:200
5\;Baur:2000\;Baur:2000_dissertation\;Baur:2000a\;Gumus:1997\;Higler:1
999\;Higler:1999_dissertation\;Lee:1998\;Peng:2003\;Reepmeyer:2003\;Re
epmeyer:2004\;Sundmacher:2003\;Yasuoka:1982\;;
}