# $Id: rathore.in 2 2004-04-17 20:20:23Z ucecesf $
# 
# rathore.in
#
# Simple separation sequence synthesis example based on the problem
# described by Rathore et al, AIChE J, May 1974.
#
# Copyright (c) 2000-2001, Eric S Fraga, UCL, All rights reserved.
#
#
# --------------------------------------------
#
# Give the synthesis problem a name and a description. These are used
# for report generation. All output will appear in a subdirectory
# named after the project name.
#
project Rathore
title "Separation sequence synthesis [Rathore et al., 1974]"
#
# tell the system where to find the classes referenced below. The
# second of these is particularly important as it enables us to use
# single line definitions of unit variables.
#
use uk.ac.ucl.che.esf.fish.ps		# for base stream and component classes
use uk.ac.ucl.che.esf.fish.units	# for the unit models and unit variables
#
# Define the constants used by the rest of the input file, specifically
# for definining the component discretizations.
#
variables
	constant Base 10 "Percentage component flow discretization"
	# define the flows of the components in the feed
	constant Fpropane  " 45.36 *kmol/hr"
	constant Fibutane  "136.08 *kmol/hr"
	constant Fnbutane  "226.8  *kmol/hr"
	constant Fipentane "181.44 *kmol/hr"
	constant Fnpentane  "317.52 *kmol/hr"
	constant FeedFlow "Fpropane+Fibutane+Fnbutane+Fipentane+Fnpentane"
end
#
# The feed stream consists of five hydrocarbon components. The base
# flow for each component is 10% of the total initial flow for that
# component. In other words, component flows will map to the nearest
# 10% of the initial flow. This is sufficient for the level of detail
# desired for this type of problem.  The main effect it has is on the
# purity specification of the final product streams.
#
KistaComponent propane
	base "Fpropane/Base"
	bp 230.8
	cpv -4.224 3.062e-1 -1.586e-4 3.214e-8
	lhtc "0.583 *kW/m^2/K"
	vhtc "5.0 *kW/m^2/K"
end
KistaComponent ibutane
	base "Fibutane/Base"
	bp 263.0
	cpv -1.390 3.847e-1 -1.846e-4 2.895e-8
	lhtc "0.583 *kW/m^2/K"
	vhtc "5.0 *kW/m^2/K"
end
KistaComponent nbutane
	base "Fnbutane/Base"
	bp 272.4
	cpv 9.487 3.313e-1 -1.108e-4 -2.821e-9
	lhtc "0.583 *kW/m^2/K"
	vhtc "5.0 *kW/m^2/K"
end
KistaComponent ipentane
	base "Fipentane/Base"
	bp 301.0
	cpv -9.525 5.066e-1 -2.729e-4 5.723e-8
	lhtc "0.583 *kW/m^2/K"
	vhtc "5.0 *kW/m^2/K"
end
KistaComponent npentane
	base "Fnpentane/Base"
	bp 309.3
	cpv -3.626 4.873e-1 -2.580e-4 5.304e-8
	lhtc "0.583 *kW/m^2/K"
	vhtc "5.0 *kW/m^2/K"
end
# 
# The feed consists of a single liquid phase made up of the components
# listed above.
#
Phase feedphase
	comps propane ibutane nbutane ipentane npentane
	x 0.05 0.15 0.25 0.2 0.35
	flow "FeedFlow"
	phase liquid
end
#
# Define the actual feed stream. There is only one pressure level
# defined.
#
PStream feed
	# the stream has one phase
	add feedphase
	# define the valid pressure range and number of values in that
	# range 
	prange "6.8 *atm" "6.8 *atm"
	nstates 1
	# and set the actual pressure
	P "6.8 *atm"
	# map to discrete space. this is not strictly necessary but is
	# useful to ensure that the feed definition starts at a point
	# in discrete space
	map	
end
#
# Discrete utilities are available for both heating and cooling. The
# format of each line is:
# 
# type  description  Tin  Tout  TransferCoefficient  Cost in $/J
#
# we define four hot utilities (stream at a variety of pressures) and
# four cold utilities (cold water and ammonia at different
# temperatures). Note that the cost of cooling water is significantly
# lower than any of the other cold utilities and it is therefore
# unlikely that Ammonia will ever be used. However, the option is
# there and it is up to the optimization procedures to choose the
# correct utilities in order to minimize the objective function
# criteria specified (see below)
#
DiscreteUtilities utils
    hot  "Steam @ 28.23 atm"	503.5 503.5 "5000 *W/m^2/K" "1.0246 / GJ"
    hot  "Steam@11.22atm"	457.6 457.6 "5000 *W/m^2/K" "0.773824 / GJ"
    hot  "Steam@4.08atm"	417.0 417.0 "5000 *W/m^2/K" "0.573203 / GJ"
    hot  "Steam@1.70atm"	388.2 388.2 "5000 *W/m^2/K" "0.41796 / GJ"
    cold  "CooldWater@32.2degC" 305.2 305.2 "500 *W/m^2/K" "0.0668737 / GJ"
    cold  "Ammonia@1degC"	274.00 274.00 "500 *W/m^2/K" "1.65035 / GJ"
    cold  "Ammonia@-17.68degC" 	255.32 255.32 "500 *W/m^2/K" "2.96871 / GJ"
    cold  "Ammonia@-21.67degC"	251.33 251.33 "500 *W/m^2/K" "3.96226 / GJ"
end
#
# the only processing technology is a distillation unit for which we
# specify a single pressure level which happens to match the the same
# pressure range specified for the feed stream, and hence all other
# streams created by Jacaranda. It is advisable that the pressure
# ranges and number of discrete values used by units (such as
# Distillation) be consistent with the pressure levels that can be
# represented in the stream objects.
#
Distillation dist
  Real P "6.8 *atm" "6.8 *atm" 1
end
#
# and we define a product tank which accepts any stream which has one
# component with greater than 90% purity.
#
ProductTank pure
  # The specification for the product streams is uses the variable 'x'
  # which is a vector made up of the mole fractions of the components
  # in the feed to this unit. The expression 'x>0.90' creates a vector
  # of the same size with values 1 or 0 depending on whether the
  # individual mole fraction is greater than 0.90 or not (1=true,
  # 0=false). The '$' operator takes the sum of the values in the
  # vector so this full expression will return a value of 1 if one
  # component matches the spefication and 0 otherwise.  Note that it
  # is impossible for more than one component to match the
  # specification within any given stream as the mole fractions must
  # add up to 1.
  Expression spec "$(x>0.90)"
  # The unit must be marked as interesting to indicate that any
  # path in the search graph which terminates at one of these
  # nodes is an interesting path, i.e. one that leads to a
  # desired product. this is used by the synthesis procedure to enable
  # us to generate different solutions when the user wishes to have
  # more than one solution generated. the variable 'nbest' in the
  # synthesis problem class (defined below) can be set to request any
  # number of solutions.
  interesting		# interesting leaf node for n-best diversity
end
#
# we also need at least one feed tank for the raw material. the feed
# stream defined above is associated with this feed tank.
#
FeedTank feedTank
  Stream feed feed
end
#
# we will ask for solutions to be ranked in three separate lists, the
# first according to capital cost, the second according to operating
# cost, and the third a combination of the two yielding a form of
# annualized cost. Each criterion is given a name, the type of
# operation required to combine criteria values from different sources
# (options are sum or max), and the actual expression for evaluating
# the criterion. The variables "opercost" and "capcost" are used for
# operating and capital costs respectively by all the standard unit
# models (and heat exchangers) in the FiSH distribution.
#
Criteria criteria
  # 
  # We define each criterion separately. The last three arguments in
  # each criterion expression are optional and describe the units for
  # the values generated, the lower bound on the particular criterion,
  # and the format to use for output.
  #
  criterion Capital sum capcost "$" 0.0 "#,##0"
  criterion Operating sum opercost "$/yr" 0.0 "#,##0"
  criterion Annualized sum "capcost/2.0 + opercost" "$/yr" 0.0 "#,##0"
end
#
# before attempting a synthesis problem, we tell the system the
# objects to use for all the global settings which affect the
# synthesis procedures. these consist of the set of utilities, the
# objective function criteria, and the unit models that are available
# for building up process flowsheets.
#
Data
  utils utils		# which utilities object to use
  criteria criteria	# the ranking criteria
  # we now specify the list of units which are allowed for
  # processing
  unit dist		# distillation
  unit pure		# and pure product tanks
  unit feedTank		# and the feed tank
  print			# output all global settings
end
#
# now we actually define the synthesis problem based on the stream and
# units defined above. The number of best solutions to generate can be
# specified in the command line. For example,
#
#   java esf.Main -n 3 rathore.in
#
# would ask for the best three solutions to be generated for each
# criterion specified above. Alternatively, the input file can have
# this value specified directly by adding the line
#
#    nbest 3
#
# within the PS_Problem object definition below.
#
PS_Problem rathore
  representation units	# include unit info in n-best diversity
  # solve the problem ...
  solve
  print			# and show the best solutions found
  print short		# showing the basic structure as well
  stats			# display some statistics about the search
  export		# generate the flowsheets
end
# and that's all!  if one wants to save all objects created by
# Jacaranda in this input file, the option "-s" can be given:
#
#   java esf.Main -s rathore.in
#
# In this case, objects will be saved in the user's esfobjects
# sub-directory off the user's home directory, if it
# exists. Otherwise, the objects will be saved in the current
# directory. If objects have been saved, one can browse them using the
# command:
#
#   java esf.ui.Manager
#