Patent Publication Number: US-8968522-B2

Title: Recovery of butanol isomers from a mixture of butanol isomers, water, and an organic extractant

Description:
CROSS REFERENCE TO RELATED APPLICATIONS 
     This application claims the benefit of priority to U.S. Provisional Patent Application 61/225,659, filed Jul. 15, 2009, the entirety of which is herein incorporated by reference. 
    
    
     FIELD OF THE INVENTION 
     Processes for recovering butanol from a butanol-containing organic phase obtained from an extractive fermentation process are provided. Specifically, processes for separating butanol from a mixture comprising butanol, water, a water-immiscible organic extractant, and optionally a non-condensable gas, are provided. 
     BACKGROUND OF THE INVENTION 
     Butanol is an important industrial chemical with a variety of applications, such as use as a fuel additive, as a blend component to diesel fuel, as a feedstock chemical in the plastics industry, and as a foodgrade extractant in the food and flavor industry. Each year 10 to 12 billion pounds of butanol are produced by petrochemical means. As the projected demand for butanol increases, interest in producing butanol from renewable resources such as corn, sugar cane, or cellulosic feeds by fermentation is expanding. 
     In a fermentative process to produce butanol, in situ product removal advantageously reduces butanol inhibition of the microorganism and improves fermentation rates by controlling butanol concentrations in the fermentation broth. Technologies for in situ product removal include stripping, adsorption, pervaporation, membrane solvent extraction, and liquid-liquid extraction. In liquid-liquid extraction, an extractant is contacted with the fermentation broth to partition the butanol between the fermentation broth and the extractant phase. The butanol and the extractant are recovered by a separation process, for example by distillation. In the recovery process, the butanol can also be separated from any water, non-condensable gas, and/or fermentation by-products which may have been removed from the fermentation broth through use of the extractant. 
     Processes for recovering butanol from the butanol-containing extractant phase obtained by in situ product removal from a fermentation broth are sought. Economical processes for recovering butanol substantially free of water and of the extractant are desired. Also desired are separation processes which are energy efficient and provide high purity butanol product having little color. Butanol recovery processes which can be run for extended periods without equipment fouling or repeated shutdowns are also sought. 
     SUMMARY OF THE INVENTION 
     The present invention provides a process for separating a butanol selected from the group consisting of 1-butanol, isobutanol, and mixtures thereof, from a feed comprising a water-immiscible organic extractant, water, the butanol, and optionally a non-condensable gas. 
     In one aspect, the present invention is a process comprising the steps:
         a) introducing a feed comprising:
           (i) a water-immiscible organic extractant,   (ii) water,   (iii) at least one isomer of butanol, and   (iv) optionally a non-condensable gas   
               

     into a first distillation column, wherein the first distillation column comprises a stripping section and optionally a rectifying section at an introduction point above the stripping section, the first distillation column having an operating temperature, T 1  and an operating pressure P 1  at a predetermined point in the stripping section, wherein T 1  and P 1  are selected to produce a first bottoms stream and a first vaporous overhead stream, the first bottoms stream comprising the water-immiscible organic extractant and butanol and being substantially free of water, and the first vaporous overhead stream comprising water, butanol, and the optional non-condensable gas;
         b) condensing the first vaporous overhead stream to produce a gas phase and recover a first mixed condensate, wherein the first mixed condensate comprises
           (i) a butanol phase comprising butanol, less than about 30 wt % water; and   (ii) an aqueous phase comprising water and less than about 10 wt % of butanol;   
           c) introducing at least a portion of the aqueous phase to the first distillation column;   d) introducing a first portion of the butanol phase into a second distillation column having at least a stripping section; and   e) introducing a first portion of the first bottoms stream into a second distillation column having at least a stripping section and optionally a rectifying section and operating the second distillation column to produce a second bottoms stream comprising the extractant and being substantially free of butanol, and a second vaporous overhead stream comprising butanol;
 
wherein the extractant preferentially dissolves butanol over water and is separable from butanol by distillation.
       

    
    
     
       BRIEF DESCRIPTION OF THE FIGURES 
         FIG. 1  illustrates one embodiment of a system useful for practicing the process of the invention. 
         FIG. 2  illustrates a process schematic diagram used in modeling the process of the invention. 
     
    
    
     DETAILED DESCRIPTION OF THE INVENTION 
     Applicants specifically incorporate the entire contents of all cited references in this disclosure. Further, when an amount, concentration, or other value or parameter is given as either a range, preferred range, or a list of upper preferable values and lower preferable values, this is to be understood as specifically disclosing all ranges formed from any pair of any upper range limit or preferred value and any lower range limit or preferred value, regardless of whether ranges are separately disclosed. Where a range of numerical values is recited herein, unless otherwise stated, the range is intended to include the endpoints thereof, and all integers and fractions within the range. It is not intended that the scope of the invention be limited to the specific values recited when defining a range. 
     Definitions 
     The following definitions are used in this disclosure: 
     “Butanol” as used herein refers with specificity to the butanol isomers 1-butanol (1-BuOH) and/or isobutanol (iBuOH or I-BUOH), either individually or as mixtures thereof. 2-Butanol and tert-butanol (1,1-dimethyl ethanol) are specifically excluded from the present use of the term. 
     “In Situ Product Removal” as used herein means the selective removal of a specific fermentation product from a biological process such as fermentation to control the product concentration in the biological process. 
     “Fermentation broth” as used herein means the mixture of water, sugars, dissolved solids, suspended solids, microorganisms producing butanol, product butanol and all other constituents of the material held in the fermentation vessel in which product butanol is being made by the reaction of sugars to butanol, water and carbon dioxide (CO 2 ) by the microorganisms present. The fermentation broth is the aqueous phase in biphasic fermentative extraction. From time to time, as used herein the term “fermentation medium” may be used synonymously with “fermentation broth”. 
     “Fermentation vessel” as used herein means the vessel in which the fermentation reaction by which product butanol is made from sugars is carried out. The term “fermentor” may be used synonymously herein with “fermentation vessel”. 
     The term “effective titer” as used herein, refers to the total amount of butanol produced by fermentation per liter of fermentation medium. The total amount of butanol includes: (i) the amount of butanol in the fermentation medium; (ii) the amount of butanol recovered from the organic extractant; and (iii) the amount of butanol recovered from the gas phase, if gas stripping is used. 
     The term “aqueous phase titer” as used herein, refers to the concentration of butanol in the fermentation broth. 
     “Stripping” as used herein means the action of transferring all or part of a volatile component from a liquid stream into a gaseous stream. 
     “Stripping section” as used herein means that part of the contacting device in which the stripping operation takes place. 
     “Rectifying” as used herein means the action of transferring all or part of a condensable component from a gaseous stream into a liquid stream in order to separate and purify lower boiling point components from higher boiling point components. 
     “Rectifying section” as used herein means the section of the distillation column above the feed point, i.e. the trays or packing material located above the point in the column where the feed stream enters, where the rectifying operation takes place. 
     The term “separation” as used herein is synonymous with “recovery” and refers to removing a chemical compound from an initial mixture to obtain the compound in greater purity or at a higher concentration than the purity or concentration of the compound in the initial mixture. 
     The term “water-immiscible” refers to a chemical component, such as an extractant or solvent, which is incapable of mixing with an aqueous solution, such as a fermentation broth, in such a manner as to form one liquid phase. 
     The term “extractant” as used herein refers to one or more organic solvents which are used to extract butanol from a fermentation broth. 
     The term “organic phase”, as used herein, refers to the non-aqueous phase of a biphasic mixture obtained by contacting a fermentation broth with a water-immiscible organic extractant. 
     The term “fatty acid” as used herein refers to a carboxylic acid having a long, aliphatic chain of C 7  to C 22  carbon atoms, which is either saturated or unsaturated. 
     The term “fatty alcohol” as used herein refers to an alcohol having a long, aliphatic chain of C 7  to C 22  carbon atoms, which is either saturated or unsaturated. 
     The term “fatty aldehyde” as used herein refers to an aldehyde having a long, aliphatic chain of C 7  to C 22  carbon atoms, which is either saturated or unsaturated. 
     Non-condensable gas means a gas that is not condensed at an operating temperature of the process described herein. 
     Butanol-containing extractant streams useful as a feed in the processes of the invention include any organic phase obtained from an extractive fermentation wherein butanol is produced as a fermentation product. Typical butanol-containing extractant streams include those produced in “dry grind” or “wet mill” fermentation processes in which in situ product removal is practiced using liquid-liquid extraction of the fermentation broth with an organic extractant. After extraction, the extractant stream typically comprises butanol, water, and the extractant. The extractant stream may optionally comprise a non-condensable gas, which can be a gas that is inert or otherwise non-reactive with other feed components under the operating conditions of the present invention. Such gases can be selected from gases in the group consisting of, for example, carbon dioxide, nitrogen, hydrogen, Noble gases such as argon, or mixtures of any of these. The extractant stream may optionally further comprise fermentation by-products having sufficient solubility to partition into the extractant phase. Butanol-containing extractant streams useful as a feed in the processes of the invention include streams characterized by a butanol concentration in the feed from about 0.1 weight percent to about 40 weight percent, for example from about 2 weight percent to about 40 weight percent, for example from about 5 weight percent to about 35 weight percent, based on the weight of the feed. Depending on the efficiency of the extraction, the aqueous phase titer of butanol in the fermentation broth can be, for example, from about 5 g/L to about 85 g/L, or from about 10 g/L to about 40 g/L. 
     The extractant is a water-immiscible organic solvent or solvent mixture having characteristics which render it useful for the extraction of butanol from a fermentation broth. The extractant preferentially partitions butanol from the aqueous phase, for example by at least a 1.1:1 concentration ratio, such that the concentration of butanol in the extractant phase is at least 1.1 times that in the aqueous phase when evaluated in a room-temperature extraction of an aqueous solution of butanol. Preferably, the extractant preferentially partitions butanol from the aqueous phase by at least a 2:1 concentration ratio, such that the concentration of butanol in the extractant phase is at least two times that in the aqueous phase when evaluated in a room-temperature extraction of an aqueous solution of butanol. To be of practical use in the butanol recovery process, the extractant is separable from butanol by distillation, having a boiling point at atmospheric pressure which is at least about 30 degrees Celsius higher than that of the butanol to be recovered, or for example at least about 40 degrees higher, or for example at least about 50 degrees higher. 
     The extractant comprises at least one solvent selected from the group consisting of C 7  to C 22  fatty alcohols, C 7  to C 22  fatty acids, esters of C 7  to C 22  fatty acids, C 7  to C 22  fatty aldehydes, C 7  to C 22  fatty amides and mixtures thereof. Suitable organic extractants are further selected from the group consisting of oleyl alcohol (CAS No. 143-28-2), behenyl alcohol (CAS No. 661-19-8), cetyl alcohol (CAS No. 36653-82-4), lauryl alcohol, also referred to as 1-dodecanol (CAS No. 112-53-8), myristyl alcohol (112-72-1), stearyl alcohol (CAS No. 112-92-5), 1-undecanol (CAS No. 112-42-5), oleic acid (CAS No. 112-80-1), lauric acid (CAS No. 143-07-7), myristic acid (CAS No. 544-63-8), stearic acid (CAS No. 57-11-4), methyl myristate CAS No. 124-10-7), methyl oleate (CAS No. 112-62-9), undecanal (CAS No. 112-44-7), lauric aldehyde (CAS No. 112-54-9), 2-methylundecanal (CAS No. 110-41-8), oleamide (CAS No. 301-02-0), linoleamide (CAS No. 3999-01-7), palmitamide (CAS No. 629-54-9) and stearylamide (CAS No. 124-26-5) and mixtures thereof. In some aspects, the extractant comprises oleyl alcohol. Suitable solvents are described in U.S. Patent Application Publication No. 2009030537 and also in U.S. application Ser. Nos. 12/759,283 and 12/758,870 (both filed Apr. 13, 2010), all of which are incorporated herein by reference. 
     These organic extractants are available commercially from various sources, such as Sigma-Aldrich (St. Louis, Mo.), in various grades, many of which may be suitable for use in extractive fermentation to produce or recover butanol. Technical grades contain a mixture of compounds, including the desired component and higher and lower fatty components. For example, one commercially available technical grade oleyl alcohol contains about 65% oleyl alcohol and a mixture of higher and lower fatty alcohols. 
     The invention provides processes for separating or recovering butanol from a feed comprising a water-immiscible organic extractant, water, the butanol, and optionally a non-condensable gas. Separation of the butanol from the feed is achieved through a combination of distillation and decantation. The distillation involves the use of at least two distillation columns. The first column, in combination with decantation, effects a separation of water from butanol and the extractant. The cooled overhead stream from the first column is decanted into two liquid phases. The organic phase is returned to the first column. The second column effects a separation of butanol from the extractant under vacuum conditions and provides a butanol stream which is substantially free of extractant. The second column also provides an extractant stream which is substantially free of water and has a reduced butanol content. 
     The processes of the invention can be understood by reference to  FIG. 1 , which illustrates one embodiment of a system useful for practicing the process of the invention. The feed stream  100 , obtained from a fermentation vessel (not shown) or an extractor (not shown) in a process for fermentative extraction, is introduced into a first distillation column  500 , which has a stripping section and optionally a rectifying section, at a feed point above the stripping section. The feed stream  100  is distilled to provide a first bottoms stream  110  and a first vaporous overhead stream  300  comprising water, butanol, and any non-condensable gas present in the feed. An operating temperature T 1  and an operating pressure P 1  at a predetermined point in the stripping section of column  500  are selected so as to provide the first bottoms stream  110  comprising the extractant and butanol and being substantially free of water. The distillation column  500  can be any conventional column having at least a feed inlet, an overhead vapor outlet, a bottoms stream outlet, a heating means, and a sufficient number of stages to effect the separation of the water from the extractant. In the case where the extractant comprises oleyl alcohol, distillation column  500  should have at least 5 stages including a re-boiler. 
     The first bottoms stream  110  can comprise from about 0.1 to about 40 weight percent butanol, and can be substantially free of water. By “substantially free”, it is meant that the bottoms stream can comprise less than about 0.1 weight percent water. For example, the bottoms stream  110  can comprise less than about 0.01 weight percent water. To ensure that the bottom stream  110  is substantially free of water, the amount of organic phase reflux and the reboiler boil-up rate can be varied. Stream  300  is condensed in a condenser  550  to produce a first mixed condensate stream  310  comprising a liquid. The mixed stream  310  can further comprise a non-condensable gas component if the gas was present in the feed. The condenser  550  may be of any conventional design. 
     The mixed condensate stream  310  is introduced into a decanter  700  and allowed to separate into a gas phase optionally comprising the non-condensable gas, a liquid butanol phase, and a liquid aqueous phase. The temperature of the decanter is preferably maintained at or below about 40° C. to reduce the amount of butanol and water being stripped out by the non-condensable gas. The liquid butanol phase, the lighter liquid phase (the top liquid phase), can include about 16 to about 30 weight percent water and may further comprise any extractant which comes overhead in column  500 . The fraction of extractant in the butanol phase can be minimized by use of an optional rectification section in column  500 . The liquid aqueous phase includes about 3 to about 10 weight percent butanol. The decanter may be of any conventional design. 
     When a non-condensable gas such as carbon dioxide is present in the feed, the non-condensable gas is present in stream  300  and in stream  310 . At least a portion of the gas phase comprising the non-condensable gas can be purged from the process, as shown in  FIG. 1 , in which purge stream  460  comprising the non-condensable gas is shown leaving the decanter  700 . 
     From the decanter  700 , the aqueous phase  480  can be purged from the process, as shown in  FIG. 1 , in which the purge stream comprising the aqueous phase  480  is shown leaving the decanter  700 . Alternatively, at least a portion of the aqueous phase can be introduced to a fermentation vessel (not shown). This can provide a means to recycle some of the water from the butanol recovery process back to the extractive fermentation process. In one embodiment, at least a portion of the aqueous phase can be combined with at least a portion of the bottoms stream from the second distillation column and then introduced to a fermentation vessel, as shown in  FIG. 2  wherein the aqueous phase  48  from the decanter  70  is combined in a mixer  75  with the bottoms stream  44  from the second distillation column to provide combined stream  45 . 
     The butanol phase  470  from the decanter is returned to the first distillation column  500 . Stream  470  would normally be introduced as reflux to the column. Introducing stream  470  as liquid reflux will suppress extractant loss in vaporous stream  300  of column  500 . The butanol phase  470  may further comprise volatile fermentation byproducts such as acetaldehyde. Optionally, at least a portion of stream  470  may be purged from the process (not shown) to remove volatile fermentation byproducts from the butanol recovery process. 
     The first bottoms stream  110  is withdrawn from column  500  and introduced into a second distillation column  800 , which has a stripping section and optionally a rectifying section, at a feed point above the stripping section. The stream  110  is distilled to provide a second bottoms stream  420  comprising the extractant and a second vaporous overhead stream  400  comprising butanol. The second distillation column is operated so as to provide the bottoms stream  420  substantially free of butanol. By “substantially free of butanol” it is meant that the bottom  420  comprises less than about one weight percent butanol. The second vaporous overhead stream  400  is substantially free of the extractant. By “substantially free of extractant” it is meant that the overhead stream  400  comprises less than about 0.01 weight percent extractant. The distillation column  800  can be any conventional column having at least a feed inlet, an overhead vapor outlet, a bottoms stream outlet, a heating means, a stripping section, and a sufficient number of stages to effect the desired separation. Column  800  should have at least 6 stages a including re-boiler. Preferably, column  800  is operated at a pressure less than atmospheric to minimize the temperature of the extractant in the base of the column while enabling economical and convenient condensation of the butanol overheads. 
     The process may further comprise introducing bottoms stream  420  from the second distillation column into a fermentation vessel (not shown). In one embodiment, bottoms stream  420  may be combined with at least a portion of the aqueous phase  480  from the decanter before introduction into a fermentation vessel, as shown in  FIG. 2  wherein analogous streams  44  and  48  are combined in mixer  75  to provide the combined stream  45 . 
     A mixture of higher boiling extractants is expected to behave in a fundamentally similar way to a single extractant provided that the boiling point of the mixture, or the boiling point of the lowest boiling solvent of the mixture, is significantly higher than the boiling points of water and butanol, for example at least about 30 degrees higher. 
     The present processes for separating or recovering butanol provide butanol known to have an energy content similar to that of gasoline and which can be blended with any fossil fuel. Butanol is favored as a fuel or fuel additive as it yields only CO 2  and little or no SC X  or NC X  when burned in the standard internal combustion engine. Additionally, butanol is less corrosive than ethanol, the most preferred fuel additive to date. 
     In addition to its utility as a biofuel or fuel additive, the butanol recovered according to the present processes has the potential of impacting hydrogen distribution problems in the emerging fuel cell industry. Fuel cells today are plagued by safety concerns associated with hydrogen transport and distribution. Butanol can be easily reformed for its hydrogen content and can be distributed through existing gas stations in the purity required for either fuel cells or vehicles. Furthermore, the present processes recover butanol obtained from plant derived carbon sources, avoiding the negative environmental impact associated with standard petrochemical processes for butanol production. 
     One advantage of the present processes for separation or recovery of butanol is energy integration of the distillation columns, which provides energy efficiency. Relative to a distillation scheme in which the separation of butanol and extractant is made prior to the final separation of butanol and water, the present processes require less energy per unit weight of butanol obtained. 
     Another advantage is that the present processes provide high purity butanol having little or no color. 
     A further advantage is that the second bottoms stream comprising the extractant is substantially free of the butanol product, which contributes to high yield in the recovery process. Being substantially free of butanol also enables optional recycling of the second bottoms stream comprising the extractant to the fermentative process. Being substantially free of butanol also simplifies the stream&#39;s disposition, should it not be recycled. 
     Yet another advantage is that the present processes allow for extended operation without equipment fouling or repeated shutdowns. 
     Although particular embodiments of the present invention have been described in the foregoing description, it will be understood by those skilled in the art that the invention is capable of numerous modifications, substitutions, and rearrangements without departing from the spirit of essential attributes of the invention. Reference should be made to the appended claims, rather than to the foregoing specification, as indicating the scope of the invention. 
     The process of the invention can be demonstrated using a computational model of the process. Process modeling is an established methodology used by engineers to simulate complex chemical processes. Process modeling software performs many fundamental engineering calculations, for example mass and energy balances, vapor/liquid equilibrium and reaction rate computations. The modeling of distillation columns is particularity well established. Calculations based on experimentally determined binary vapor/liquid equilibrium and liquid/liquid equilibrium data can predict reliably the behavior of multi-component mixtures. This capability has been expanded to allow modeling of complex multi-stage, multi-component distillation columns using rigorous algorithms like the “inside-out” algorithm developed by Joseph Boston of Aspentech, Inc. of Burlington, Mass. Commercial modeling software, such as Aspen Plus® from Aspentech, can be used in conjunction with physical property databases, such as DIPPR, available from the American Institute of Chemical Engineers, Inc., of New York, N.Y., to develop accurate models and assessments of processes. 
     EXAMPLES 
     The Examples were obtained through process modeling using isobutanol as the butanol isomer and oleyl alcohol as the extractant. 
     Similar results would be expected for the analogous cases where 1-butanol or a mixture of 1-butanol and isobutanol was selected as the butanol isomer, due to the similarity of the physical property data for isobutanol and 1-butanol and the heterogeneous nature of the azeotrope between water and these butanol isomers. 
     Table 1 lists typical feed compositions of the rich solvent stream, obtained from extractive fermentation, entering the isobutanol product recovery area. These compositions were used in modeling the processes of the invention. In the Examples, the term “rich solvent stream” is synonymous with the term “feed stream” used above. 
     
       
         
           
               
             
               
                 TABLE 1 
               
             
            
               
                   
               
               
                 Feed Compositions (in Weight Percent) of the 
               
               
                 Rich Solvent Stream from the Extractor 
               
            
           
           
               
               
               
               
            
               
                   
                 Feed Compositions 
                 Example 1 
                 Example 2 
               
               
                   
                   
               
            
           
           
               
               
               
               
            
               
                   
                 Isobutanol 
                 11.44% 
                 25.10% 
               
               
                   
                 Water 
                 6.47% 
                 8.23% 
               
               
                   
                 Carbon dioxide 
                 0.88% 
                 0.94% 
               
               
                   
                 Oleyl alcohol 
                 81.21% 
                 65.73% 
               
               
                   
                   
               
            
           
         
       
     
     These composition values for the rich solvent stream were established by a simulation of a dry grind facility using extractive in situ product removal technology producing 50 mM gal/year of isobutanol, and fermenter broth aqueous phase titers of 20 and 40 g/L respectively. It was assumed that the rich solvent stream was at equilibrium with the fermentation broth and that the solvent flow rate was sufficient to meet the specified annual capacity. 
     The parameters inputted for the simulations of the embodiments of the processes of the invention are listed in Table 2 and follow a process schematic diagram as shown in  FIG. 2 . In  FIG. 2 , “QED 06 ” refers to a heat stream representing process to process heat exchange via heat exchangers  65  and  85 . Block  60  represents an optional mixer. Block  75  represents a mixer combining streams  48  and  44  to provide stream  45 . Certain dimensions and duty results calculated from the process model are also listed in Table 2. These parameters do not include physical property parameters, and those related to convergence and other computational options or diagnostics. 
     
       
         
           
               
             
               
                 TABLE 2 
               
             
            
               
                   
               
               
                 Conditions Used for Modeling Processes of the Invention 
               
            
           
           
               
               
               
               
               
            
               
                 Equipment blocks 
                 Inputs 
                 Example 1 
                 Example 2 
                 Units 
               
               
                   
               
            
           
           
               
               
               
               
               
            
               
                 Solvent Column 
                 Number of theoretical stages 
                 15 
                 15 
                 stages 
               
               
                 (50) 
                 including re-boiler 
               
               
                   
                 Column top pressure 
                 1 
                 1 
                 bar 
               
               
                   
                 Column bottom pressure 
                 1.1 
                 1.1 
                 bar 
               
               
                   
                 Column internal diameter 
                 3.71 
                 2.91 
                 m 
               
               
                   
                 Column re-boiler duty 
                 59612 
                 38116 
                 MJ/hr 
               
               
                   
                 Preheated rich solvent feed (10) 
                 1 
                 1 
                 stage 
               
               
                   
                 location 
               
               
                   
                 Organic reflux from decanter (47) 
                 1 
                 1 
                 stage 
               
               
                   
                 location 
               
               
                   
                 Mass fraction water in bottom 
                 1 
                 1 
                 ppm 
               
               
                   
                 stream (11) 
               
               
                   
                 Reflux stream temperature 
                 40 
                 40 
                 deg C. 
               
               
                   
                 Preheated rich solvent stream (10) 
                 177671 
                 75171 
                 kg/hr 
               
               
                   
                 flow rate 
               
               
                   
                 Preheated rich solvent stream (10) 
                 91.7 
                 84.9 
                 deg C. 
               
               
                   
                 temperature 
               
               
                   
                 Condenser duty 
                 −48810 
                 −33831 
                 MJ/hr 
               
               
                 BuOHCOL Column 
                 Number of theoretical stages 
                 15 
                 15 
                 stages 
               
               
                 (80) 
                 including re-boiler 
               
               
                   
                 Column top pressure 
                 0.1 
                 0.1 
                 bar 
               
               
                   
                 Column bottom pressure 
                 0.105 
                 0.105 
                 bar 
               
               
                   
                 Column internal diameter 
                 2.58 
                 2.46 
                 m 
               
               
                   
                 Column re-boiler duty 
                 9045 
                 10951 
                 MJ/hr 
               
               
                   
                 Organic feed from solvent column 
                 7 
                 7 
                 stage 
               
               
                   
                 (11) location 
               
               
                   
                 Organic feed from solvent column 
                 145.6 
                 125.1 
                 deg C. 
               
               
                   
                 (11) temperature 
               
               
                   
                 Column bottom temperature 
                 147 
                 147 
                 deg C. 
               
               
                   
                 Oleyl alcohol mass fraction in top 
                 100 
                 100 
                 ppm 
               
               
                   
                 product (40) 
               
               
                   
                 Isobutanol mass fraction in 
                 9000 
                 9000 
                 ppm 
               
               
                   
                 bottom lean solvent (42) 
               
               
                   
                 Condenser duty 
                 −13844 
                 −12278 
                 MJ/hr 
               
               
                 Decanter (70) 
                 Decanter pressure 
                 1 
                 1 
                 atm 
               
               
                   
                 Decanter temperature 
                 40 
                 40 
                 deg C. 
               
               
                   
               
            
           
         
       
     
     Two cases were run to demonstrate the operating requirements of the processes of the invention. For each case, a particular modification was made to the rich solvent feed flow and compositions from the extractive fermentation process where two different aqueous phase titers were maintained. In each of the independent simulations, column traffic and heat exchanger duties will change because of the feed composition change. By comparing the resulting capital investment and operating costs between different cases, the impact of the rich solvent feed flow and composition on product recovery area performance was quantified. These two examples, however, should not be regarded as process operating limits of this invention. 
     In the Tables, the term “Solvent Column” is synonymous with the term “first distillation column” used above. The term “BUOHCOL” is synonymous with the term “second distillation column” used above. The abbreviation “OLEYLOH” refers to oleyl alcohol. 
     Stream results for Example 1 are listed in Table 3. BUOHCOL column traffic and liquid mass composition profiles are listed in Table 4. Solvent column traffic and liquid mass composition profiles are listed in Table 5. 
     Stream results for Example 2 are listed in Table 6. BUOHCOL column traffic and liquid mass composition profiles are listed in Table 7. Solvent column traffic and liquid mass composition profiles are listed in Table 8. 
     Other key process parameters include the following: 1) the total number of theoretical stages and the bottom stream water content in the solvent column; 2) the BUOHCOL column bottom temperature; and 3) the degree of preheating of the rich solvent stream before feeding it to the solvent column. These parameters can be manipulated to achieve optimum separation performance. 
     Example 1 
     In this Example, 177,671 kg/hr rich solvent feed ( 9 ) containing 11.44 weight percent isobutanol is heated from 32.2 to 91.7° C. by a process to process heat exchanger and the resulting stream ( 10 ) is fed to the solvent column ( 50 ) at stage  1 . This rich solvent feed condition corresponds to 20 g/liter aqueous phase titer in the fermentor which is maintained during the extractive fermentation process. The separation is realized by a larger diameter solvent column, higher solvent column bottom temperature, and higher solvent column re-boiler and condenser duties. Stream ( 40 ) is essentially 100 weight percent isobutanol. Stream ( 42 ) contains 0.9 weight percent isobutanol and 99.1 weight percent oleyl alcohol. 
     Example 2 
     In this Example, 75,171 kg/hr rich solvent feed ( 9 ) is heated from 32.2 to 84.9° C. by a process to process heat exchanger and the resulting stream ( 10 ) is fed to the solvent column ( 50 ) at stage  1 . This rich solvent feed condition corresponds to 40 g/liter aqueous phase titer in the fermenter which is maintained during the extractive fermentation process. The separation is realized by a smaller diameter solvent column, lower solvent column bottom temperature, and lower solvent column re-boiler and condenser duties. Stream ( 40 ) is essentially 100 weight percent isobutanol. Stream ( 42 ) contains 0.9 weight percent isobutanol and 99.1 weight percent oleyl alcohol. 
     
       
         
           
               
             
               
                 TABLE 3 
               
               
                   
               
               
                 Simulated Stream Outputs for Example 1. 
               
               
                   
               
             
            
               
                   
               
            
           
           
               
               
               
               
               
               
               
               
            
               
                   
                 9 
                 10 
                 11 
                 30 
                 31 
                 40 
                 42 
               
               
                   
               
               
                 Temperature C. 
                 32.2 
                 91.7 
                 145.6 
                 92.6 
                 92.6 
                 56.5 
                 147 
               
               
                 Pressure atm 
                 1.09 
                 1.04 
                 1.09 
                 0.99 
                 0.99 
                 0.1 
                 0.11 
               
               
                 Vapor Frac 
                 0 
                 0.157 
                 0 
                 1 
                 1 
                 0 
                 0 
               
               
                 Mole Flow kmol/hr 
                 1485.305 
                 1485.305 
                 798.584 
                 1075.55 
                 1075.55 
                 243.483 
                 555.101 
               
               
                 Mass Flow kg/hr 
                 177671.064 
                 177671.1 
                 163638.7 
                 32370.384 
                 32370.384 
                 18047.763 
                 145590.98 
               
               
                 Volume Flow l/hr 
                 212216.149 
                 6.88E+06 
                 219236 
                 3.23E+07 
                 3.23E+07 
                 23409.954 
                 193029.09 
               
               
                 Enthalpy MMBtu/hr 
                 −546.773 
                 −515.113 
                 −315.653 
                 −256.916 
                 −256.916 
                 −75.628 
                 −244.574 
               
               
                 Mass Flow kg/hr 
                   
                   
                   
                   
                   
                   
                   
               
               
                 I—BUOH 
                 20332.4088 
                 20332.41 
                 19356.11 
                 15863.657 
                 15863.657 
                 18045.795 
                 1310.3189 
               
               
                 WATER 
                 11496.2539 
                 11496.25 
                 0.163639 
                 14842.689 
                 14842.689 
                 0.1636388 
                 2.67E−10 
               
               
                 CO2 
                 1559.93142 
                 1559.931 
                 3.18E−23 
                 1656.2064 
                 1656.2064 
                 0 
                 0 
               
               
                 OLEYLOH 
                 144282.47 
                 144282.5 
                 144282.5 
                 7.8319222 
                 7.8319222 
                 1.8047763 
                 144280.67 
               
               
                 Mass Frac 
                   
                   
                   
                   
                   
                   
                   
               
               
                 I—BUOH 
                 0.11443849 
                 0.114438 
                 0.118286 
                 0.490067 
                 0.490067 
                 0.9998909 
                 0.009 
               
               
                 WATER 
                 0.06470526 
                 0.064705 
                 1.00E−06 
                 0.4585268 
                 0.4585268 
                 9.07E−06 
                 1.83E−15 
               
               
                 CO2 
                 0.00877988 
                 0.00878 
                 1.94E−28 
                 0.0511643 
                 0.0511643 
                 0 
                 0 
               
               
                 OLEYLOH 
                 0.81207635 
                 0.812076 
                 0.881713 
                 0.0002419 
                 0.0002419 
                 0.0001 
                 0.991 
               
               
                   
               
            
           
           
               
               
               
               
               
               
               
               
            
               
                   
                   
                 44 
                 45 
                 46 
                 47 
                 48 
                 49 
               
               
                   
               
               
                   
                 Temperature C. 
                 45 
                 44.3 
                 40 
                 40 
                 40 
                 40 
               
               
                   
                 Pressure atm 
                 1.26 
                 1 
                 1 
                 1 
                 1 
                 0.1 
               
               
                   
                 Vapor Frac 
                 0 
                 0 
                 1 
                 0 
                 0 
                 0 
               
               
                   
                 Mole Flow kmol/hr 
                 555.101 
                 1203.014 
                 38.774 
                 388.863 
                 647.913 
                 243.483 
               
               
                   
                 Mass Flow kg/hr 
                 145591 
                 157963.271 
                 1659.511 
                 18338.586 
                 12372.288 
                 18047.76 
               
               
                   
                 Volume Flow l/hr 
                 175750.7 
                 1.88E+05 
                 9.91E+05 
                 2.25E+04 
                 12691.227 
                 22984.34 
               
               
                   
                 Enthalpy MMBtu/hr 
                 −276.233 
                 −451.502 
                 −13.946 
                 −113.965 
                 −175.268 
                 −76.401 
               
               
                   
                 Mass Flow kg/hr 
                   
                   
                   
                   
                   
                   
               
               
                   
                 I—BUOH 
                 1310.319 
                 2222.04846 
                 64.7054968 
                 14887.2216 
                 911.729612 
                 18045.79 
               
               
                   
                 WATER 
                 2.67E−10 
                 11444.7055 
                 50.7448995 
                 3347.23881 
                 11444.7055 
                 0.163639 
               
               
                   
                 CO2 
                 0 
                 15.8524187 
                 1544.06067 
                 96.2933369 
                 15.8524187 
                 0 
               
               
                   
                 OLEYLOH 
                 144280.7 
                 144280.665 
                 1.02E−06 
                 7.83188542 
                 3.58E−05 
                 1.804776 
               
               
                   
                 Mass Frac 
                   
                   
                   
                   
                   
                   
               
               
                   
                 I—BUOH 
                 0.009 
                 0.01406686 
                 0.03899069 
                 0.8117977 
                 0.07369127 
                 0.999891 
               
               
                   
                 WATER 
                 1.83E−15 
                 0.07245168 
                 0.03057822 
                 0.18252437 
                 0.92502744 
                 9.07E−06 
               
               
                   
                 CO2 
                 0 
                 0.00010035 
                 0.93043108 
                 0.00525085 
                 0.00128128 
                 0 
               
               
                   
                 OLEYLOH 
                 0.991 
                 0.91338109 
                 6.15E−10 
                 0.00042707 
                 2.89E−09 
                 0.0001 
               
               
                   
               
            
           
         
       
     
     
       
         
           
               
             
               
                 TABLE 4 
               
               
                   
               
               
                 Simulated BUOHCOL Column Traffic and Liquid Mass Composition Profile Outputs for Example 1. 
               
               
                   
               
             
            
               
                   
               
            
           
           
               
               
               
               
               
               
               
               
               
               
               
            
               
                   
                   
                   
                 Heat 
                 Liquid 
                 Vapor 
                 Liquid 
                 Vapor 
                 Mixed 
                 Liquid 
                 Vapor 
               
               
                   
                 Temperature 
                 Pressure 
                 duty 
                 flow 
                 flow 
                 feed 
                 feed 
                 feed 
                 product 
                 product 
               
               
                 Stage 
                 C. 
                 atm 
                 MJ/hr 
                 kg/hr 
                 kg/hr 
                 kg/hr 
                 kg/hr 
                 kg/hr 
                 kg/hr 
                 kg/hr 
               
               
                   
               
               
                 1 
                 56.5011602 
                 0.1 
                 −13844.4 
                 2793.2042 
                 0 
                 0 
                 0 
                 0 
                 18047.7632 
                 0 
               
               
                 2 
                 66.1270606 
                 0.100357 
                 0 
                 267.02946 
                 20840.967 
                 0 
                 0 
                 0 
                 0 
                 0 
               
               
                 3 
                 120.88619 
                 0.100714 
                 0 
                 229.71305 
                 18314.793 
                 0 
                 0 
                 0 
                 0 
                 0 
               
               
                 4 
                 122.750144 
                 0.101071 
                 0 
                 229.1764 
                 18277.476 
                 0 
                 0 
                 0 
                 0 
                 0 
               
               
                 5 
                 122.786979 
                 0.101429 
                 0 
                 228.44906 
                 18276.94 
                 0 
                 0 
                 0 
                 0 
                 0 
               
               
                 6 
                 122.794813 
                 0.101786 
                 0 
                 227.72417 
                 18276.212 
                 0 
                 17089.858 
                 0 
                 0 
                 0 
               
               
                 7 
                 122.802293 
                 0.102143 
                 0 
                 146776.65 
                 1185.6295 
                 146548.89 
                 0 
                 0 
                 0 
                 0 
               
               
                 8 
                 122.815489 
                 0.1025 
                 0 
                 146784.87 
                 1185.6706 
                 0 
                 0 
                 0 
                 0 
                 0 
               
               
                 9 
                 122.828661 
                 0.102857 
                 0 
                 146793.08 
                 1193.8891 
                 0 
                 0 
                 0 
                 0 
                 0 
               
               
                 10 
                 122.841823 
                 0.103214 
                 0 
                 146801.28 
                 1202.0929 
                 0 
                 0 
                 0 
                 0 
                 0 
               
               
                 11 
                 122.854977 
                 0.103571 
                 0 
                 146809.47 
                 1210.2909 
                 0 
                 0 
                 0 
                 0 
                 0 
               
               
                 12 
                 122.868132 
                 0.103929 
                 0 
                 146817.66 
                 1218.485 
                 0 
                 0 
                 0 
                 0 
                 0 
               
               
                 13 
                 122.88251 
                 0.104286 
                 0 
                 146825.93 
                 1226.6759 
                 0 
                 0 
                 0 
                 0 
                 0 
               
               
                 14 
                 123.082079 
                 0.104643 
                 0 
                 146866.29 
                 1234.9444 
                 0 
                 0 
                 0 
                 0 
                 0 
               
               
                 15 
                 147.019984 
                 0.105 
                 9045.051 
                 145590.98 
                 1275.3011 
                 0 
                 0 
                 0 
                 145590.984 
                 0 
               
               
                   
               
            
           
           
               
               
               
               
               
            
               
                   
                 Stage 
                 I—BUOH 
                 WATER 
                 OLEYLOH 
               
               
                   
               
               
                   
                 1 
                 0.999891 
                 9.07E−06 
                 0.0001 
               
               
                   
                 2 
                 0.245012 
                 1.93E−07 
                 0.754987 
               
               
                   
                 3 
                 0.017676 
                 1.37E−08 
                 0.982324 
               
               
                   
                 4 
                 0.016748 
                 1.32E−08 
                 0.983252 
               
               
                   
                 5 
                 0.01679 
                 1.32E−08 
                 0.98321 
               
               
                   
                 6 
                 0.016848 
                 1.33E−08 
                 0.983152 
               
               
                   
                 7 
                 0.016906 
                 2.59E−09 
                 0.983094 
               
               
                   
                 8 
                 0.016961 
                 4.80E−10 
                 0.983039 
               
               
                   
                 9 
                 0.017015 
                 8.85E−11 
                 0.982985 
               
               
                   
                 10 
                 0.01707 
                 1.63E−11 
                 0.98293 
               
               
                   
                 11 
                 0.017124 
                 2.98E−12 
                 0.982876 
               
               
                   
                 12 
                 0.017178 
                 5.43E−13 
                 0.982822 
               
               
                   
                 13 
                 0.017232 
                 9.86E−14 
                 0.982768 
               
               
                   
                 14 
                 0.017188 
                 1.75E−14 
                 0.982812 
               
               
                   
                 15 
                 0.009 
                 1.83E−15 
                 0.991 
               
               
                   
               
            
           
         
       
     
     
       
         
           
               
             
               
                 TABLE 5 
               
               
                   
               
               
                 Simulated Solvent Column Traffic and Liquid Mass 
               
               
                 Composition Profile Outputs for Example 1. 
               
               
                   
               
             
            
               
                   
               
            
           
           
               
               
               
               
               
               
               
            
               
                   
                 Temper- 
                   
                 Heat 
                 Liquid 
                 Vapor 
                 Liquid 
               
               
                   
                 ature 
                 Pressure 
                 duty 
                 flow 
                 flow 
                 feed 
               
               
                 Stage 
                 C. 
                 atm 
                 MJ/hr 
                 kg/hr 
                 kg/hr 
                 kg/hr 
               
               
                   
               
               
                 1 
                 92.5578171 
                 0.986923 
                 0 
                 190930.5 
                 32370.903 
                 189058.21 
               
               
                 2 
                 93.6721095 
                 0.993973 
                 0 
                 191294.94 
                 27291.757 
                 0 
               
               
                 3 
                 93.875775 
                 1.001022 
                 0 
                 191366.91 
                 27656.195 
                 0 
               
               
                 4 
                 94.0607027 
                 1.008072 
                 0 
                 191435.46 
                 27728.158 
                 0 
               
               
                 5 
                 94.2425765 
                 1.015121 
                 0 
                 191518.88 
                 27796.707 
                 0 
               
               
                 6 
                 94.4133652 
                 1.022171 
                 0 
                 191695.12 
                 27880.134 
                 0 
               
               
                 7 
                 94.5220752 
                 1.02922 
                 0 
                 192452.05 
                 28056.375 
                 0 
               
               
                 8 
                 94.2567509 
                 1.036269 
                 0 
                 197295.41 
                 28813.3 
                 0 
               
               
                 9 
                 97.1873422 
                 1.043319 
                 0 
                 211117.51 
                 33656.66 
                 0 
               
               
                 10 
                 106.390013 
                 1.050368 
                 0 
                 230900.1 
                 47478.762 
                 0 
               
               
                 11 
                 114.300372 
                 1.057418 
                 0 
                 244353.88 
                 67261.351 
                 0 
               
               
                 12 
                 117.024529 
                 1.064467 
                 0 
                 248884.39 
                 80715.128 
                 0 
               
               
                 13 
                 117.793003 
                 1.071517 
                 0 
                 249926.35 
                 85245.644 
                 0 
               
               
                 14 
                 118.611501 
                 1.078566 
                 0 
                 243744.67 
                 86287.599 
                 0 
               
               
                 15 
                 145.617646 
                 1.085616 
                 59612.44 
                 163638.75 
                 80105.926 
                 0 
               
               
                   
               
            
           
           
               
               
               
               
               
               
               
            
               
                   
                   
                   
                   
                   
                 1st 
                 2nd 
               
               
                   
                 Vapor 
                 Mixed 
                 Liquid 
                 Vapor 
                 liquid 
                 liquid 
               
               
                   
                 feed 
                 feed 
                 product 
                 product 
                 flow 
                 flow 
               
               
                 Stage 
                 kg/hr 
                 kg/hr 
                 kg/hr 
                 kg/hr 
                 kg/hr 
                 kg/hr 
               
               
                   
               
               
                 1 
                 6951.4374 
                 0 
                 0 
                 32369.8779 
                 187271.886 
                 3658.6179 
               
               
                 2 
                 0 
                 0 
                 0 
                 0 
                 187484.04 
                 3810.90195 
               
               
                 3 
                 0 
                 0 
                 0 
                 0 
                 187538.31 
                 3828.59527 
               
               
                 4 
                 0 
                 0 
                 0 
                 0 
                 187593.472 
                 3841.98237 
               
               
                 5 
                 0 
                 0 
                 0 
                 0 
                 187673.645 
                 3845.23649 
               
               
                 6 
                 0 
                 0 
                 0 
                 0 
                 187907.591 
                 3787.53341 
               
               
                 7 
                 0 
                 0 
                 0 
                 0 
                 189102.216 
                 3349.83052 
               
               
                 8 
                 0 
                 0 
                 0 
                 0 
                 197295.407 
                 0 
               
               
                 9 
                 0 
                 0 
                 0 
                 0 
                 211117.509 
                 0 
               
               
                 10 
                 0 
                 0 
                 0 
                 0 
                 230900.098 
                 0 
               
               
                 11 
                 0 
                 0 
                 0 
                 0 
                 244353.875 
                 0 
               
               
                 12 
                 0 
                 0 
                 0 
                 0 
                 248884.391 
                 0 
               
               
                 13 
                 0 
                 0 
                 0 
                 0 
                 249926.346 
                 0 
               
               
                 14 
                 0 
                 0 
                 0 
                 0 
                 243744.673 
                 0 
               
               
                 15 
                 0 
                 0 
                 163638.747 
                 0 
                 163638.747 
                 0 
               
               
                   
               
            
           
           
               
               
               
               
               
            
               
                 Stage 
                 I—BUOH 
                 WATER 
                 CO2 
                 OLEYLOH 
               
               
                   
               
               
                 1 
                 0.175304 
                 0.068834 
                 0.000144 
                 0.755718 
               
               
                 2 
                 0.176064 
                 0.069654 
                 2.77E−06 
                 0.754279 
               
               
                 3 
                 0.176227 
                 0.069777 
                 5.31E−08 
                 0.753996 
               
               
                 4 
                 0.176394 
                 0.069879 
                 1.02E−09 
                 0.753726 
               
               
                 5 
                 0.176655 
                 0.069947 
                 1.97E−11 
                 0.753398 
               
               
                 6 
                 0.177494 
                 0.069801 
                 3.82E−13 
                 0.752705 
               
               
                 7 
                 0.18192 
                 0.068339 
                 7.49E−15 
                 0.749741 
               
               
                 8 
                 0.211661 
                 0.057001 
                 0 
                 0.731338 
               
               
                 9 
                 0.284384 
                 0.032138 
                 0 
                 0.683478 
               
               
                 10 
                 0.364523 
                 0.010521 
                 0 
                 0.624956 
               
               
                 11 
                 0.406922 
                 0.002509 
                 0 
                 0.590569 
               
               
                 12 
                 0.419647 
                 0.000527 
                 0 
                 0.579826 
               
               
                 13 
                 0.422474 
                 0.000107 
                 0 
                 0.57742 
               
               
                 14 
                 0.40689 
                 2.04E−05 
                 0 
                 0.593089 
               
               
                 15 
                 0.118286 
                 1.00E−06 
                 0 
                 0.881713 
               
               
                   
               
            
           
         
       
     
     
       
         
           
               
             
               
                 TABLE 6 
               
               
                   
               
               
                 Simulated Stream Outputs for Example 2. 
               
               
                   
               
             
            
               
                   
               
            
           
           
               
               
               
               
               
               
               
               
            
               
                   
                 9 
                 10 
                 11 
                 30 
                 31 
                 40 
                 42 
               
               
                   
               
               
                 Temperature C. 
                 32.2 
                 84.9 
                 125.2 
                 90.6 
                 90.6 
                 56.5 
                 147 
               
               
                 Pressure atm 
                 1.09 
                 1.04 
                 1.09 
                 0.99 
                 0.99 
                 0.1 
                 0.11 
               
               
                 Vapor Frac 
                 0 
                 0.063 
                 0 
                 1 
                 1 
                 0 
                 0 
               
               
                 Mole Flow kmol/hr 
                 797.981 
                 797.981 
                 431.612 
                 727.821 
                 727.821 
                 241.521 
                 190.091 
               
               
                 Mass Flow kg/hr 
                 75171.2 
                 75171.2 
                 67759.48 
                 24453.15 
                 24453.15 
                 17902.59 
                 49856.89 
               
               
                 Volume Flow l/hr 
                 90271.19 
                 1.50E+06 
                 90110.59 
                 2.17E+07 
                 2.17E+07 
                 23221.75 
                 66101.83 
               
               
                 Enthalpy MMBtu/hr 
                 −273.088 
                 −262.246 
                 −157.514 
                 −174.532 
                 −174.532 
                 −75.019 
                 −83.753 
               
               
                 Mass Flow kg/hr 
                   
                   
                   
                   
                   
                   
                   
               
               
                 I—BUOH 
                 18869.86 
                 18869.86 
                 18349.44 
                 14357.87 
                 14357.87 
                 17900.73 
                 448.712 
               
               
                 WATER 
                 6184.856 
                 6184.856 
                 0.067759 
                 9296.486 
                 9296.486 
                 0.067759 
                 4.32E−14 
               
               
                 CO2 
                 706.512 
                 706.512 
                 0 
                 795.989 
                 795.989 
                 0 
                 0 
               
               
                 OLEYLOH 
                 49409.97 
                 49409.97 
                 49409.97 
                 2.811 
                 2.811 
                 1.79 
                 49408.18 
               
               
                 Mass Frac 
                   
                   
                   
                   
                   
                   
                   
               
               
                 I—BUOH 
                 0.251025 
                 0.251025 
                 0.270803 
                 0.587158 
                 0.587158 
                 0.999896 
                 0.009 
               
               
                 WATER 
                 0.082277 
                 0.082277 
                 1.00E−06 
                 0.380175 
                 0.380175 
                 3.78E−06 
                 8.67E−19 
               
               
                 CO2 
                 0.009399 
                 0.009399 
                 1.49E−28 
                 0.032552 
                 0.032552 
                 0 
                 0 
               
               
                 OLEYLOH 
                 0.657299 
                 0.657299 
                 0.729196 
                 0.000115 
                 0.000115 
                 0.0001 
                 0.991 
               
               
                   
               
            
           
           
               
               
               
               
               
               
               
               
            
               
                   
                   
                 44 
                 45 
                 46 
                 47 
                 48 
                 49 
               
               
                   
               
               
                   
                 Temperature C. 
                 45 
                 44 
                 40 
                 40 
                 40 
                 40 
               
               
                   
                 Pressure atm 
                 1.26 
                 1 
                 1 
                 1 
                 1 
                 0.1 
               
               
                   
                 Vapor Frac 
                 0 
                 0 
                 1 
                 0 
                 0 
                 0 
               
               
                   
                 Mole Flow kmol/hr 
                 190.091 
                 538.959 
                 17.528 
                 361.426 
                 348.867 
                 241.521 
               
               
                   
                 Mass Flow kg/hr 
                 49856.89 
                 56518.78 
                 750.182 
                 17041.08 
                 6661.889 
                 17902.59 
               
               
                   
                 Volume Flow l/hr 
                 60184.94 
                 66985.58 
                 447766.1 
                 20937.83 
                 6833.643 
                 22799.48 
               
               
                   
                 Enthalpy MMBtu/hr 
                 −94.595 
                 −188.968 
                 −6.304 
                 −105.921 
                 −94.373 
                 −75.786 
               
               
                   
                 Mass Flow kg/hr 
                   
                   
                   
                   
                   
                   
               
               
                   
                 I—BUOH 
                 448.712 
                 939.7063 
                 29.25273 
                 13837.62 
                 490.9942 
                 17900.73 
               
               
                   
                 WATER 
                 4.32E−14 
                 6162.359 
                 22.93916 
                 3111.188 
                 6162.359 
                 0.067759 
               
               
                   
                 CO2 
                 0 
                 8.536 
                 697.99 
                 89.463 
                 8.536 
                 0 
               
               
                   
                 OLEYLOH 
                 49408.18 
                 49408.18 
                 0 
                 2.811 
                 0 
                 1.79 
               
               
                   
                 Mass Frac 
                   
                   
                   
                   
                   
                   
               
               
                   
                 I—BUOH 
                 0.009 
                 0.016626 
                 0.038994 
                 0.812015 
                 0.073702 
                 0.999896 
               
               
                   
                 WATER 
                 8.67E−19 
                 0.109032 
                 0.030578 
                 0.18257 
                 0.925017 
                 3.78E−06 
               
               
                   
                 CO2 
                 0 
                 0.000151 
                 0.930428 
                 0.00525 
                 0.001281 
                 0 
               
               
                   
                 OLEYLOH 
                 0.991 
                 0.87419 
                 2.38E−10 
                 0.000165 
                 1.12E−09 
                 0.0001 
               
               
                   
               
            
           
         
       
     
     
       
         
           
               
             
               
                 TABLE 7 
               
               
                   
               
               
                 Simulated BUOHCOL Column Traffic and Liquid Mass Composition Profile Outputs for Example 2. 
               
               
                   
               
             
            
               
                   
               
            
           
           
               
               
               
               
               
               
               
               
               
               
               
            
               
                   
                   
                   
                 Heat 
                 Liquid 
                 Vapor 
                 Liquid 
                 Vapor 
                 Mixed 
                 Liquid 
                 Vapor 
               
               
                   
                 Temperature 
                 Pressure 
                 duty 
                 flow 
                 flow 
                 feed 
                 feed 
                 feed 
                 product 
                 product 
               
               
                 Stage 
                 C. 
                 atm 
                 MJ/hr 
                 kg/hr 
                 kg/hr 
                 kg/hr 
                 kg/hr 
                 kg/hr 
                 kg/hr 
                 kg/hr 
               
               
                   
               
               
                 1 
                 56.50411 
                 0.1 
                 −12277.7 
                 580.4229 
                 0 
                 0 
                 0 
                 0 
                 17902.59 
                 0 
               
               
                 2 
                 66.12733 
                 0.100357 
                 0 
                 8.058413 
                 18483.01 
                 0 
                 0 
                 0 
                 0 
                 0 
               
               
                 3 
                 78.95627 
                 0.100714 
                 0 
                 6.737 
                 17910.65 
                 0 
                 0 
                 0 
                 0 
                 0 
               
               
                 4 
                 78.99224 
                 0.101071 
                 0 
                 6.69776 
                 17909.32 
                 0 
                 0 
                 0 
                 0 
                 0 
               
               
                 5 
                 78.9936 
                 0.101429 
                 0 
                 6.660182 
                 17909.29 
                 0 
                 0 
                 0 
                 0 
                 0 
               
               
                 6 
                 78.99491 
                 0.101786 
                 0 
                 6.622855 
                 17909.25 
                 0 
                 12857.16 
                 0 
                 0 
                 0 
               
               
                 7 
                 78.99731 
                 0.102143 
                 0 
                 54908.56 
                 5052.046 
                 54902.32 
                 0 
                 0 
                 0 
                 0 
               
               
                 8 
                 79.04864 
                 0.1025 
                 0 
                 54918.21 
                 5051.663 
                 0 
                 0 
                 0 
                 0 
                 0 
               
               
                 9 
                 79.09983 
                 0.102857 
                 0 
                 54927.84 
                 5061.317 
                 0 
                 0 
                 0 
                 0 
                 0 
               
               
                 10 
                 79.15088 
                 0.103214 
                 0 
                 54937.45 
                 5070.946 
                 0 
                 0 
                 0 
                 0 
                 0 
               
               
                 11 
                 79.20184 
                 0.103571 
                 0 
                 54947.02 
                 5080.554 
                 0 
                 0 
                 0 
                 0 
                 0 
               
               
                 12 
                 79.25394 
                 0.103929 
                 0 
                 54956.15 
                 5090.13 
                 0 
                 0 
                 0 
                 0 
                 0 
               
               
                 13 
                 79.3555 
                 0.104286 
                 0 
                 54948.29 
                 5099.253 
                 0 
                 0 
                 0 
                 0 
                 0 
               
               
                 14 
                 81.40961 
                 0.104643 
                 0 
                 54559.54 
                 5091.393 
                 0 
                 0 
                 0 
                 0 
                 0 
               
               
                 15 
                 147.02 
                 0.105 
                 10950.61 
                 49856.89 
                 4702.649 
                 0 
                 0 
                 0 
                 49856.89 
                 0 
               
               
                   
               
            
           
           
               
               
               
               
               
            
               
                   
                 Stage 
                 I—BUOH 
                 WATER 
                 OLEYLOH 
               
               
                   
               
               
                   
                 1 
                 0.999896 
                 3.78E−06 
                 0.0001 
               
               
                   
                 2 
                 0.245 
                 8.07E−08 
                 0.755 
               
               
                   
                 3 
                 0.098561 
                 2.81E−08 
                 0.901439 
               
               
                   
                 4 
                 0.098808 
                 2.82E−08 
                 0.901192 
               
               
                   
                 5 
                 0.09925 
                 2.83E−08 
                 0.900749 
               
               
                   
                 6 
                 0.099694 
                 2.85E−08 
                 0.900306 
               
               
                   
                 7 
                 0.100134 
                 3.18E−09 
                 0.899866 
               
               
                   
                 8 
                 0.100292 
                 2.63E−10 
                 0.899708 
               
               
                   
                 9 
                 0.100449 
                 2.17E−11 
                 0.899551 
               
               
                   
                 10 
                 0.100607 
                 1.79E−12 
                 0.899394 
               
               
                   
                 11 
                 0.100763 
                 1.48E−13 
                 0.899237 
               
               
                   
                 12 
                 0.100912 
                 1.23E−14 
                 0.899088 
               
               
                   
                 13 
                 0.100775 
                 1.01E−15 
                 0.899225 
               
               
                   
                 14 
                 0.090278 
                 0 
                 0.909722 
               
               
                   
                 15 
                 0.009 
                 0 
                 0.991 
               
               
                   
               
            
           
         
       
     
     
       
         
           
               
             
               
                 TABLE 8 
               
               
                   
               
               
                 Simulated Solvent Column Traffic and Liquid Mass Composition Profile Outputs for Example 2. 
               
               
                   
               
             
            
               
                   
               
            
           
           
               
               
               
               
               
               
               
               
               
               
               
               
               
            
               
                   
                   
                   
                   
                   
                   
                   
                   
                   
                   
                   
                 1st 
                 2nd 
               
               
                   
                 Temper- 
                   
                 Heat 
                 Liquid 
                 Vapor 
                 Liquid 
                 Vapor 
                 Mixed 
                 Liquid 
                 Vapor 
                 liquid 
                 liquid 
               
               
                   
                 ature 
                 Pressure 
                 duty 
                 flow 
                 flow 
                 feed 
                 feed 
                 feed 
                 product 
                 product 
                 flow 
                 flow 
               
               
                 Stage 
                 C. 
                 atm 
                 MJ/hr 
                 kg/hr 
                 kg/hr 
                 kg/hr 
                 kg/hr 
                 kg/hr 
                 kg/hr 
                 kg/hr 
                 kg/hr 
                 kg/hr 
               
               
                   
               
               
                 1 
                 90.62398 
                 0.986923 
                 0 
                 93278.67 
                 24452.8 
                 90384.63 
                 1827.657 
                 0 
                 0 
                 24453.68 
                 90909.07 
                 2369.606 
               
               
                 2 
                 91.46275 
                 0.993973 
                 0 
                 93442.51 
                 25519.19 
                 0 
                 0 
                 0 
                 0 
                 0 
                 91034.75 
                 2407.763 
               
               
                 3 
                 91.65498 
                 1.001022 
                 0 
                 93481.11 
                 25683.03 
                 0 
                 0 
                 0 
                 0 
                 0 
                 91070.53 
                 2410.574 
               
               
                 4 
                 91.83796 
                 1.008072 
                 0 
                 93520.73 
                 25721.63 
                 0 
                 0 
                 0 
                 0 
                 0 
                 91109.71 
                 2411.021 
               
               
                 5 
                 92.0175 
                 1.015121 
                 0 
                 93598.2 
                 25761.25 
                 0 
                 0 
                 0 
                 0 
                 0 
                 91213.06 
                 2385.141 
               
               
                 6 
                 92.16465 
                 1.022171 
                 0 
                 94198.65 
                 25838.72 
                 0 
                 0 
                 0 
                 0 
                 0 
                 92221.08 
                 1977.569 
               
               
                 7 
                 92.40016 
                 1.02922 
                 0 
                 98158.28 
                 26439.17 
                 0 
                 0 
                 0 
                 0 
                 0 
                 98158.28 
                 0 
               
               
                 8 
                 95.35407 
                 1.036269 
                 0 
                 107889.8 
                 30398.8 
                 0 
                 0 
                 0 
                 0 
                 0 
                 107889.8 
                 0 
               
               
                 9 
                 102.9854 
                 1.043319 
                 0 
                 119982.9 
                 40130.34 
                 0 
                 0 
                 0 
                 0 
                 0 
                 119982.9 
                 0 
               
               
                 10 
                 109.7331 
                 1.050368 
                 0 
                 127742.4 
                 52223.47 
                 0 
                 0 
                 0 
                 0 
                 0 
                 127742.4 
                 0 
               
               
                 11 
                 112.4066 
                 1.057418 
                 0 
                 130587.3 
                 59982.94 
                 0 
                 0 
                 0 
                 0 
                 0 
                 130587.3 
                 0 
               
               
                 12 
                 113.2472 
                 1.064467 
                 0 
                 131403 
                 62827.79 
                 0 
                 0 
                 0 
                 0 
                 0 
                 131403 
                 0 
               
               
                 13 
                 113.5887 
                 1.071517 
                 0 
                 131648.5 
                 63643.56 
                 0 
                 0 
                 0 
                 0 
                 0 
                 131648.5 
                 0 
               
               
                 14 
                 113.9111 
                 1.078566 
                 0 
                 129620 
                 63889.04 
                 0 
                 0 
                 0 
                 0 
                 0 
                 129620 
                 0 
               
               
                 15 
                 125.1555 
                 1.085616 
                 38116.05 
                 67759.48 
                 61860.52 
                 0 
                 0 
                 0 
                 67759.48 
                 0 
                 67759.48 
                 0 
               
               
                   
               
            
           
           
               
               
               
               
               
            
               
                 Stage 
                 I—BUOH 
                 WATER 
                 CO2 
                 OLEYLOH 
               
               
                   
               
               
                 1 
                 0.362857 
                 0.107294 
                 0.000112 
                 0.529736 
               
               
                 2 
                 0.363393 
                 0.107798 
                 1.41E−06 
                 0.528808 
               
               
                 3 
                 0.363534 
                 0.107877 
                 1.77E−08 
                 0.52859 
               
               
                 4 
                 0.363698 
                 0.107936 
                 2.22E−10 
                 0.528366 
               
               
                 5 
                 0.36426 
                 0.107812 
                 2.81E−12 
                 0.527929 
               
               
                 6 
                 0.370412 
                 0.105027 
                 3.59E−14 
                 0.524561 
               
               
                 7 
                 0.410794 
                 0.085803 
                 0 
                 0.503402 
               
               
                 8 
                 0.494394 
                 0.047597 
                 0 
                 0.458009 
               
               
                 9 
                 0.571843 
                 0.016292 
                 0 
                 0.411865 
               
               
                 10 
                 0.608865 
                 0.004277 
                 0 
                 0.386858 
               
               
                 11 
                 0.620548 
                 0.001017 
                 0 
                 0.378435 
               
               
                 12 
                 0.623678 
                 0.000235 
                 0 
                 0.376087 
               
               
                 13 
                 0.624558 
                 5.40E−05 
                 0 
                 0.375388 
               
               
                 14 
                 0.618452 
                 1.21E−05 
                 0 
                 0.381536 
               
               
                 15 
                 0.270803 
                 1.00E−06 
                 0 
                 0.729196