WO2015127435A1 - Récupération d'isoprène à partir de procédés de fermentation en utilisant la compression mécanique et la condensation - Google Patents

Récupération d'isoprène à partir de procédés de fermentation en utilisant la compression mécanique et la condensation Download PDF

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WO2015127435A1
WO2015127435A1 PCT/US2015/017285 US2015017285W WO2015127435A1 WO 2015127435 A1 WO2015127435 A1 WO 2015127435A1 US 2015017285 W US2015017285 W US 2015017285W WO 2015127435 A1 WO2015127435 A1 WO 2015127435A1
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isoprene
stream
vapor stream
compressed
vapor
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Werner Bussmann
David J. Gaskin
Mohammad SHADAB
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Glycos Biotechnologies Inc
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Glycos Biotechnologies Inc
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    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C7/00—Purification; Separation; Use of additives
    • C07C7/09—Purification; Separation; Use of additives by fractional condensation
    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12P—FERMENTATION OR ENZYME-USING PROCESSES TO SYNTHESISE A DESIRED CHEMICAL COMPOUND OR COMPOSITION OR TO SEPARATE OPTICAL ISOMERS FROM A RACEMIC MIXTURE
    • C12P5/00—Preparation of hydrocarbons or halogenated hydrocarbons
    • C12P5/007—Preparation of hydrocarbons or halogenated hydrocarbons containing one or more isoprene units, i.e. terpenes

Definitions

  • the present invention generally relates to processes for the recovery of isoprene produced via fermentation processes. More specifically, the present disclosure relates to the recovery of isoprene produced via a fermentation process, from the gas streams exiting the fermentor using a combination of mechanical compression and condensation to convert the isoprene from the gaseous phase to the liquid phase.
  • high-value chemicals or fuels are manufactured by thermochemical processes from hydrocarbons, including petroleum oil and natural gas. Also, high-value chemicals may be produced as by-products during the processing of crude oil into usable fractions.
  • Isoprene (CAS Number 78-79-5) is a 5-carbon hydrocarbon useful as a starting material for synthesizing a wide variety of chemicals.
  • isoprene may be used as a monomer or co-monomer for the production of higher value polymers.
  • chemicals that can be produced using isoprene include polyisoprene, as a copolymer in polybutylene, styrene-isoprene-styrene block co-polymers, and others.
  • An example of an industry that uses isoprene is the synthetic rubber industry. The majority of isoprene is produced as a "by-product" during the processing of crude oil into usable fractions.
  • isoprene has typically been produced during the catalytic cracking of crude oil fractions.
  • catalytic crackers has diminished due to the availability of inexpensive natural gas, resulting in a reduced supply of the four and five carbon chain molecules that are found in crude oil, but not natural gas.
  • isoprene a new method of isoprene production is desired.
  • the chemical production industry is seeking ways to replace chemicals made from non-renewable feedstocks with chemicals produced from renewable feedstocks using environmentally friendly practices.
  • Bact. 181 4700-4703; Fall, R. and S.D. Copley. 2000. Bacterial sources and sinks of isoprene. a reactive atmospheric hydrocarbon. Env. Microbiol. 2: 123-130; Xue, J., and B.K. Ahring. 2011. Enhancing isoprene production by the genetic modification of the 1-deoxy-D- xylulose-5 -phosphate pathway in Bacillus subtilis. Appl. Env. Microbiol. 77: 2399-2405), the mechanism of isoprene production is unknown and the levels of isoprene production are relatively low.
  • Isoprene boils at 34°C under atmospheric pressure and is hardly soluble in water.
  • substantially all of the isoprene exits the fermentor in the vapor phase.
  • the advent of fermentation-based isoprene production has required the concomitant development of technologies and processes for recovering isoprene from the gases exiting the fermentor.
  • recovery processes for bio-based isoprene have been proposed, e.g., U.S. Patents 8,324,442, 8,492,605 and 8,569,562, these recovery processes have limitations that affect their utility.
  • U.S. Patents 8,324,442, 8,492,605 and 8,569,562 these recovery processes have limitations that affect their utility.
  • Patents 8,324,442, and 8,492,605 teach the removal of water from the fermentation gases using cold condensation at temperatures as low as -10°C. This leaves residual water in the process gases that may freeze on surfaces as the process gases are further cooled to -35 °C and below. The accumulated ice may block process gas lines, reducing operability and potentially creating a dangerous failure of the isoprene recovery system.
  • U.S. Patent 8,569,562 teaches using a gas- liquid absorber to separate isoprene from non-condensable gases by absorbing the isoprene into a solvent. The isoprene is then recovered from the solvent using significant heat. Heat accelerates the formation of isoprene dimers and oligomers that may accumulate in the solvent or foul equipment surfaces. Thus, there is a need for a new recovery process for bio-based isoprene that avoids these potential problems.
  • the present invention provides processes for the recovery of bio-based isoprene from vapor streams produced using a fermentation process.
  • isoprene is recovered from the initial vapor stream produced by the fermentation process in three or more steps by compressing the initial vapor stream to condense a portion of the water contained therein to produce a second vapor stream with lower water content and a water condensate stream; drying the second vapor stream to remove substantially all of the water thereby producing a third vapor stream from which substantially all of the water has been removed; and condensing the isoprene present in the third vapor stream by one or more of lowering the temperature of the third vapor stream or adiabatically decompressing (also referred to herein as "adiabatic expansion”) the third vapor stream to form an isoprene condensate stream and a fourth vapor stream from which substantially all the isoprene has been removed.
  • the process further optionally comprises recovering the isoprene from the isoprene condensate stream and optionally
  • isoprene is recovered from the initial vapor stream by compressing the initial vapor stream in one or more stages, each stage consisting of a compressor and an intercooler or heat exchanger, followed by a vapor-liquid separator to produce a second compressed vapor stream and a water condensate stream; drying the second compressed vapor stream with either a molecular sieve or a membrane-based gas dryer to produce a compressed, third vapor stream from which substantially all of the water has been removed; and condensing the isoprene in the third vapor stream preferably using one or more heat exchangers to produce an isoprene condensate and a fourth compressed vapor stream from which substantially all of the isoprene has been removed; and optionally recovering and optionally further purifying the isoprene in the condensate stream.
  • isoprene is recovered from the initial vapor stream by compressing the vapor stream in one or more stages with isothermal compressors followed by a vapor-liquid separator to produce a compressed, second vapor stream and a water condensate stream; drying the compressed, second vapor stream with either a molecular sieve or a membrane- based gas dryer to produce a compressed third vapor stream from which substantially all of the water has been removed; and condensing the isoprene in the third compressed vapor stream using, for example, one or more heat exchangers to produce an isoprene condensate stream and a fourth compressed vapor stream from which substantially all of the isoprene has been removed; and optionally, recovering and optionally further purifying the isoprene in the isoprene condensate stream.
  • isoprene is recovered from the initial vapor stream by compressing the vapor stream in one or more stages, each stage consisting of a compressor and an intercooler or heat exchanger, followed by a vapor-liquid separator to produce a second compressed vapor stream and a water condensate stream; drying the second compressed vapor stream with either a molecular sieve or a membrane-based gas dryer to produce a third compressed vapor stream from which substantially all of the water has been removed; and condensing the isoprene in the third compressed vapor stream using, for example, one or more heat exchangers followed by adiabatic expansion to produce an isoprene condensate and a fourth vapor stream from which substantially all of the isoprene has been removed; and optionally, recovering and optionally further purifying the isoprene from the isoprene condensate stream.
  • isoprene is recovered from the initial vapor stream by compressing the initial vapor stream in one or more stages with isothermal compressors followed by a vapor- liquid separator to produce a compressed, second vapor stream and a water condensate stream; drying the second vapor stream with either a molecular sieve or a membrane-based gas dryer to produce a compressed, third vapor stream from which substantially all of the water has been removed; and condensing the third vapor stream using, for example, one or more heat exchangers to lower the temperature of the third vapor stream optionally followed by adiabatic expansion to produce an isoprene condensate stream and a fourth vapor stream from which substantially all of the isoprene has been removed; and optionally, recovering and further purifying the isoprene from the isoprene condensate stream.
  • the Figure is a process flow diagram showing one process for the recovery of isoprene from fermentor gases in accordance with the invention.
  • the present invention provides a method of recovering isoprene with high efficiency and purity from a vapor stream containing water, ethanol, and lower boiling components.
  • a vapor stream is the vapor stream of bio-based isoprene production using non-naturally occurring microorganisms engineered to produce isoprene from various carbon sources such as glucose, sucrose and other sugars; glycerol; fatty acids, monoglycerides, diglycerides or triglycerides; carbon dioxide or carbon monoxide; methanol; ethanol; or acetate.
  • Lower boiling components (with boiling points lower than that of isoprene under similar conditions) that may be present include acetaldehyde, hydrogen (H 2 ), nitrogen, (N 2 ), oxygen (O 2 ), and carbon dioxide (CO 2 ).
  • Other higher boiling components (with boiling points higher than that of isoprene under similar conditions) that may be present include acetone, ethyl acetate, 3-methyl-3-buten-l-ol, 3-methyl-2-buten-l-ol, 2-methyl-3-buten-2-ol, prenyl acetate and prenal.
  • the feed stream may contain additional components, including one or more sulfur-containing compounds such as methanethiol, dimethyl disulfide, or 3- methyl thiophene.
  • An initial vapor stream resulting from a fermentation process may comprise about 0.1% to 20% by volume isoprene. Water may be present in an amount that is greater than about 70% of its saturation point. For an initial vapor stream at atmospheric pressure and approximately 37 °C, this is approximately 30 to 50 grams of water per kilogram of vapor stream.
  • the present invention provides for at least three steps in the recovery of isoprene from a vapor feed stream. In the first step, the initial vapor feed stream resulting directly from fermentation is compressed isothermally or compressed with intercooling thereby forming a compressed, second vapor stream.
  • the temperature of the vapor stream at the start of the compression process is about 20 °C to about 50 °C and the final temperature is about 20 °C to about 150 °C.
  • the compressed, second vapor stream is dried to remove
  • substantially all of the water present thereby forming a compressed third vapor stream from which substantially all of the water has been removed.
  • substantially all of the water remaining in the third vapor stream means that water has been reduced to 0.01 gram of water per kilogram of vapor stream.
  • the first compression step and the second drying step may occur in any order. That is, as an alternate to the order described above, the initial vapor feed stream may be dried to remove substantially all of the water from the initial vapor feed stream prior to compression.
  • the compressed third vapor stream is condensed such that substantially all of the isoprene present in the third vapor stream is condensed to form isoprene condensate.
  • substantially all of the isoprene present in the third vapor stream is at least about 90% by volume, preferably at least about 95% by volume and preferably at least about 99% by volume of the isoprene present in the third vapor stream.
  • the isoprene condensate is separated and recovered from the compressed fourth vapor stream which is substantially free of isoprene.
  • the fourth vapor stream is substantially free of isoprene if less than about 10% by volume, less than about 5% by volume and preferably less than about 1% by volume of isoprene remains in the fourth vapor stream.
  • the condensation of the isoprene in the vapor stream may occur in one or more stages.
  • the condensation may be achieved through the use of, for example, chillers, heat exchangers, rapid expansion of the compressed vapor stream (the Joule-Thomson effect, for example), or through a combination of technologies.
  • the first compression of the initial vapor stream step may occur in one or more stages. That is a single compressor may be used to compress the initial vapor feed stream to the desired final pressure, or two or more compressors may be used to compress the vapor feed stream to the desired final pressure.
  • the compressor may be of any type suitable for vapor compression, including but not limited to, rotary compressors such as sliding vane, scroll, liquid ring, screw or lobe compressors; reciprocating compressors such as double- acting, diaphragm or piston compressors; centrifugal compressors; or axial compressors.
  • the one or more compressors are isothermal compressors.
  • isothermal compressors include liquid ring seal compressors or screw compressors with coolant injection. The injected coolant may be liquid water or another fluid to absorb the heat. Condensate from the compressors may be separated from the compressed vapor stream using a vapor-liquid separator.
  • the one or more compressors may be compressors with intercoolers.
  • the compressor unit consists of a compressor, an intercooler, and a vapor-liquid separator.
  • multiple compressor units are used in series to achieve the desired level of compression while limiting the temperature increase of the vapor stream as it is compressed to avoid unwanted chemical reactions of isoprene at the high temperatures normally caused by compression.
  • the intercooler may be a heat exchanger, for example, a double pipe heat exchanger, a shell and tube heat exchanger, a plate heat exchanger, a plate and shell heat exchanger, a plate fin heat exchanger, a pillow plate heat exchanger, an adiabatic wheel heat exchanger, or a phase-change heat exchanger.
  • the initial vapor feed stream typically with a moisture content of between 20 g water per kg of vapor feed stream and 500 g water per kg of vapor feed stream, an initial pressure between 0 and 2.5 bar(g), and an initial temperature of about 20°C to about 50°C, is compressed to form a second vapor streaming having a final moisture content between 0.01 g water per kg of vapor feed stream and 250 g water per kg of vapor feed stream, a final pressure between 5 and 50 bar(g) and a final temperature of 20°C and 150°C.
  • the final moisture content is between 0.01 g water per kg of vapor feed stream and 50 g water per kg of vapor feed stream
  • the final pressure is between 5 and 15 bar(g) and the final temperature is between 20° C and 100°C.
  • the drying step of the second vapor stream may be achieved using a variety of different technologies.
  • Molecular sieves for example zeolite molecular sieves or activated alumina, may be used to dry the compressed vapor stream.
  • a membrane system employing a membrane that selectively permits the separation of the water vapor from the isoprene vapor may be used to dry the compressed vapor stream.
  • Solid desiccants or deliquescent solids for example magnesium sulfate or calcium sulfate, may be used to dry the compressed vapor stream.
  • Liquid desiccants for example, glycol desiccants or concentrated sulfuric acid, may be used to dry the compressed vapor stream. Water may be condensed from the second vapor stream to achieve drying followed by separation of the second vapor stream from the water condensate stream.
  • the compressed second vapor stream with a moisture content between 0.01 and 250 g water per kg of compressed vapor feed stream, a pressure of between 5 and 50 bar(g), and a temperature of about 20°C to about 150°C is dried using molecular sieves, for example, a 3A or 4A zeolite molecular sieve or activated alumina desiccant, in a simple passage or a pressure swing adsorption configuration thereby forming a third vapor stream from which substantially all of the water has been removed.
  • the compressed second vapor stream is dried using a membrane gas dryer thereby forming a third vapor stream from which substantially all of the water has been removed.
  • the drying step reduces the moisture content of the compressed third vapor stream to 0.01 g water per kg of compressed vapor feed stream or less, preferably below 0.001 g water per kg of compressed third vapor stream or less, and more preferably, below 0.0001 g water per kg of compressed vapor stream.
  • the drying step reduces the water content to a level that is below the dew point or frost point for water at the temperature and pressure used to condense the isoprene in the condensing step.
  • the isoprene-condensing step may be achieved, for example, by decreasing the temperature of the compressed vapor stream in one stage, for example, from 20° C to -60° C or in two or more stages, for example, cooling from 20°C to 0°C followed by cooling from 0°C to -60°C.
  • Isoprene from the compressed third vapor stream condenses to form an isoprene condensate and a second compressed vapor phase with reduced isoprene content.
  • more than 80%, 85%, 90%, 95%, 98% or 99% of the isoprene present in the compressed second vapor stream is condensed to form the isoprene condensate. More preferably, substantially all of the isoprene is condensed from the compressed second vapor stream to form the isoprene condensate.
  • Isoprene condensation can be achieved, for example, by using one or more heat exchangers.
  • heat exchangers include a double pipe heat exchanger, a shell and tube heat exchanger, a plate heat exchanger, a plate and frame heat exchanger, a plate and shell heat exchanger, a plate fin heat exchanger, a pillow plate heat exchanger, an adiabatic wheel heat exchanger, or a phase-change heat exchanger.
  • Cooling for the heat exchangers may be supplied by one or more refrigeration systems, for example an ammonia cycle refrigeration system or a propane cycle refrigeration system, or a mixed refrigerant system.
  • the second compressed vapor phase with reduced isoprene content is recycled to a heat exchanger to provide at least a portion of the cooling requirements.
  • the second compressed vapor phase with reduced isoprene content that is recycled to a heat exchanger to assist with cooling is optionally at a temperature ranging from about -60 °C to about -90 °C.
  • solid carbon dioxide also known as "dry ice”
  • dry ice may be removed using known techniques for withdrawing solid carbon dioxide from the process.
  • condensation can be achieved through, for example, the adiabatic expansion of the compressed vapor stream.
  • the compressed vapor stream is passed through an appropriate valve or porous plug, e.g., a Joule-Thomson valve, into a zone of lower pressure.
  • the rapid expansion of the compressed vapor stream produces a second vapor stream of lower temperature and pressure, causing a portion of the isoprene to condense into an isoprene condensate.
  • Examples of devices that may be used for adiabatic expansion of the compressed vapor stream include Joule-Thomson valves, globe valves, stop-check valves, and other throttling equipment.
  • the temperature of the compressed vapor stream is lowered to facilitate isoprene condensation using a combination of heat exchangers and adiabatic expansion using Joule-Thomson valves to achieve a temperature at which isoprene forms a condensate.
  • the temperature of the compressed vapor stream is typically in the range of -30°C to -80°C, preferably in the range of -40°C to -60°C, while the pressure is typically in the range of 5 bar(g) to 50 bar(g), preferably between 5 bar(g) and 15 bar(g).
  • the pressure is reduced to 0 to 20 bar(g), preferably between 0 and 2 bar(g), and the temperature is reduced to -45 °C to -90° C.
  • the pressure is reduced to 0 to 20 bar(g), preferably between 0 and 4 bar(g), and the temperature is reduced to -45°C to -120 °C.
  • solid carbon dioxide also known as "dry ice”
  • the process can be operated by also removing and isolating the carbon dioxide in the process gas at every stage in the process (e.g. stream 101 through stream 701 et seq).
  • the step 22 where water removal is achieved can be used to remove carbon dioxide in the same or an additional unit operation using the known principles to separate carbon dioxide from a gas stream.
  • the concentration of the carbon dioxide in the stream 301 is preferably in the range of 0 to 2% preferably between 0 and 0.1% and more preferably between 0 and 0.01% of carbon dioxide by volume. The removal of carbon dioxide leads to a smaller amount of residual dissolved gasses in the liquefied isoprene stream.
  • the lower temperature for the condensation step Step 44 with stream 501 is no longer limited by the potential condensation of carbon dioxide in solid form (i.e. dry ice). Consequently, the temperature can be reduced further to eliminate isoprene from the gas stream more completely and thus improve the yield of the process. This will lead to removal efficiency for isoprene of 99.9 % at -1 10 °C.
  • the elevation of the final condensation pressure in step 44, stream 501 has a similar effect.
  • a doubling of the pressure from 1 atm to 2 atm will reduce the remaining isoprene in the gas stream by 50%.
  • a combination of elevated pressure and lowered temperatures can be used to provide degree of elimination of the isoprene from the gas stream that result in an off- gas that can be released to the environment without further treatment.
  • the table below shows the Temperature-Pressure combinations for a certain vapor pressure of isoprene that would correspond to a release of less than 10 ppm (30 mg/m3) isoprene in the off-gas stream 601 and consecutive.
  • non-naturally occurring microorganisms are used to convert fatty acids to isoprene in a fermentation-based process that results in an isoprene-rich vapor feed stream, stream 101.
  • the major components of stream 101 are presented in Table 1 and Table 2. Isoprene is recovered from this vapor feed stream, stream 101, in high yield using the process of the present invention. TABLE 1: STREAM 101
  • feed stream 101 at a vapor fraction of 1, 37°C and 0 bar(g) is compressed in compressor train 11, which comprises two compressor stages, to a vapor fraction of 0.96 (part of the water present in stream 101 is condensed to the liquid fraction), 37°C and 10 bar(g) to produce a second vapor/liquid stream 201.
  • the vapor/liquid stream 201 is then passed to a vapor/liquid separator and molecular 22 to yield a vapor stream 301 that is substantially free of water and a liquid stream
  • the vapor stream 301 comprises mostly isoprene and lower boiling, non-condensable gases such as N 2 , CO2, and O2, while the liquid stream 801 comprises mostly water and some residual, higher boiling, polar components such as traces of acetone, ethanol, ethyl acetate, etc.
  • the vapor stream 301 is sufficiently dry that any traces of water present in vapor stream 301 will not freeze out onto piping and equipment surfaces, thereby reducing the risk of blocking the gas flow with ice.
  • the vapor stream 301 is passed through a heat exchanger 33, which may comprise one or more heat exchangers in series or in parallel, to yield stream 401 at -61 °C and 10 bar(g).
  • Stream 401 is then decompressed by adiabatic expansion using a Joule-Thomson valve 44 resulting in stream 501 with a reduced temperature of -79°C and a reduced pressure of 0 bar(g).
  • Isoprene present in stream 501 condenses to the liquid phase, while non- condensable gases such as N 2 , CO2, and O2 remain in the vapor phase.
  • Stream 501 is passed to vapor/liquid separator 55 to produce a vapor stream 601 comprised primarily of non-condensable gases such as N 2 , CO2, and O2 and a liquid stream 701 comprised primarily of the majority of the isoprene and a small amount of dissolved C0 2 .
  • Stream 601 is passed through a heat exchanger 66 to produce stream 1201, increasing the temperature of the vapor phase to 5°C.
  • Stream 701 is then passed through heat exchanger 77 to produce stream 901, increasing the temperature of the liquid isoprene to 5 ° C and lowering the solubility of C0 2 dissolved in the isoprene.
  • streams 601 and 701 may be used to supply a portion of the cooling required to cool stream 301 by integrating heat exchangers 66 and 77 into heat exchanger 33, thereby lowering the energy requirements and operational costs of the process.
  • Stream 901 is then routed to vapor-liquid separator 88 to remove residual C0 2 in the vapor phase (stream 1001), while the liquid isoprene (stream 1101) is recovered and stored for further use. Residual isoprene present in stream 1001 may be recovered by combining stream 1001 with stream 101, thereby improving the yield of isoprene recovered by the process.
  • Example 2 describes an embodiment, which further increases the recovery rate of isoprene from the product gas mix and reduces the isoprene load of the off-gas.
  • non-naturally occurring microorganisms are used to convert fatty acids to isoprene in a fermentation-based process that results in an isoprene-rich vapor feed stream, stream 101.
  • the major components of stream 101 are presented in Table 1 and Table 2 above. Isoprene is recovered from this vapor feed stream, stream 101, in high yield using the process of the present invention.
  • feed stream 101 at a vapor fraction of 1, 37°C and 0 bar(g) is compressed in compressor train 11, which comprises two compressor stages, to a vapor fraction of 0.96 (part of the water present in stream 101 is condensed to the liquid fraction), 37°C and 10 bar(g) to produce a second vapor/liquid stream 201.
  • the vapor/liquid stream 201 is then passed to separator 22 suitable to remove carbon dioxide from the gas mixture to yield a vapor stream 301 that is substantially free of carbon dioxide and a carbon dioxide containing stream 801.
  • the vapor stream 301 comprises mostly isoprene and lower boiling, non-condensable gases such as N 2 , and (3 ⁇ 4, while the liquid stream 801 comprises mostly carbon dioxide, some water and some residual, higher boiling, polar components such as traces of acetone, ethanol, ethyl acetate, etc.
  • the vapor stream 301 is sufficiently dry that any traces of water present in vapor stream 301 will not freeze out onto piping and equipment surfaces, thereby reducing the risk of blocking the gas flow with ice.
  • the vapor stream 301 is treated similar to example 1 in that it is passed through a heat exchanger 33, which may comprise one or more heat exchangers in series or in parallel, to yield stream 401 at sufficiently cooled to below -70° C and 10 bar(g).
  • a heat exchanger 33 which may comprise one or more heat exchangers in series or in parallel, to yield stream 401 at sufficiently cooled to below -70° C and 10 bar(g).
  • Stream 401 is then decompressed by adiabatic expansion using a Joule-Thomson valve 44 resulting in stream 501 with a reduced temperature of below -80° C and a reduced pressure of 0 bar(g) or higher, e.g. 1 bar(g) or 2 bar(g), or 4 bar(g).
  • Isoprene present in stream 501 condenses to the liquid phase, while non-condensable gases such as N 2 , and (3 ⁇ 4 remain in the vapor phase.
  • Stream 501 is passed to vapor/liquid separator 55 to produce a vapor stream 601 comprised primarily of non-condensable gases such as N 2 , and O2 and a liquid stream 701 comprised primarily of the majority of the isoprene and a only traces of dissolved gases like nitrogen.
  • the off-gas stream 601 is now much lower in residual isoprene concentration depending on the final temperature and pressure in the gas liquid separator.
  • Stream 601 is passed through a heat exchanger 66 to produce stream 1201, increasing the temperature of the vapor phase to 5°C.
  • Stream 701 is then passed through heat exchanger 77 to produce stream 901, increasing the temperature of the liquid isoprene to 5°C and lowering the solubility of CO 2 dissolved in the isoprene.

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Abstract

La présente invention concerne des procédés de récupération d'isoprène à partir d'un flux d'alimentation constitué d'isoprène, d'eau, d'éthanol, et de composés de point d'ébullition inférieur. Le flux d'alimentation contenant de l'isoprène est comprimé de manière à éviter la génération d'une chaleur excessive tout en condensant une partie de l'eau contenue dans le flux d'alimentation, le flux de vapeur est séché plus avant, et l'isoprène y est condensé, ce qui permet de séparer l'isoprène d'une partie substantielle des composés de point d'ébullition inférieur, puis l'isoprène est récupéré.
PCT/US2015/017285 2014-02-24 2015-02-24 Récupération d'isoprène à partir de procédés de fermentation en utilisant la compression mécanique et la condensation Ceased WO2015127435A1 (fr)

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CN106606889A (zh) * 2015-10-22 2017-05-03 浙江诚信医化设备有限公司 一种分子筛脱水工艺及其装置
FR3067099A1 (fr) * 2017-05-30 2018-12-07 Madhav Rathour Dispositif de separation de melange gazeux

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US8470581B2 (en) * 2008-09-15 2013-06-25 Danisco Us Inc. Reduction of carbon dioxide emission during isoprene production by fermentation

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US4885063A (en) * 1988-02-01 1989-12-05 Air Products And Chemicals, Inc. Method and apparatus for olefin recovery
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CN106606889A (zh) * 2015-10-22 2017-05-03 浙江诚信医化设备有限公司 一种分子筛脱水工艺及其装置
FR3067099A1 (fr) * 2017-05-30 2018-12-07 Madhav Rathour Dispositif de separation de melange gazeux

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