WO2012087557A2 - Ethylene recovery from off-gas - Google Patents

Ethylene recovery from off-gas Download PDF

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Publication number
WO2012087557A2
WO2012087557A2 PCT/US2011/063431 US2011063431W WO2012087557A2 WO 2012087557 A2 WO2012087557 A2 WO 2012087557A2 US 2011063431 W US2011063431 W US 2011063431W WO 2012087557 A2 WO2012087557 A2 WO 2012087557A2
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WIPO (PCT)
Prior art keywords
stream
ethylene
producing
methane
gas stream
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Ceased
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PCT/US2011/063431
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French (fr)
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WO2012087557A3 (en
Inventor
Hengky Mualim
Ralls Lee
Bhadra S. Grover
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Air Liquide SA
LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
Original Assignee
Air Liquide SA
LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
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Publication of WO2012087557A2 publication Critical patent/WO2012087557A2/en
Publication of WO2012087557A3 publication Critical patent/WO2012087557A3/en
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/002—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by condensation
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
    • B01D53/04—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with stationary adsorbents
    • B01D53/047—Pressure swing adsorption
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    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen; Reversible storage of hydrogen
    • C01B3/50—Separation of hydrogen or hydrogen-containing gases from gaseous mixtures, e.g. purification
    • C01B3/506—Separation of hydrogen or hydrogen-containing gases from gaseous mixtures, e.g. purification at low temperatures
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen; Reversible storage of hydrogen
    • C01B3/50—Separation of hydrogen or hydrogen-containing gases from gaseous mixtures, e.g. purification
    • C01B3/56—Separation of hydrogen or hydrogen-containing gases from gaseous mixtures, e.g. purification by contacting with solids; Regeneration of used solids
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/0204—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the feed stream
    • F25J3/0219—Refinery gas, cracking gas, coke oven gas, gaseous mixtures containing aliphatic unsaturated CnHm or gaseous mixtures of undefined nature
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
    • F25J3/0233—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of CnHm with 1 carbon atom or more
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
    • F25J3/0238—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of CnHm with 2 carbon atoms or more
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
    • F25J3/0252—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of hydrogen
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2256/00—Main component in the product gas stream after treatment
    • B01D2256/16—Hydrogen
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2256/00—Main component in the product gas stream after treatment
    • B01D2256/24—Hydrocarbons
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2256/00—Main component in the product gas stream after treatment
    • B01D2256/24—Hydrocarbons
    • B01D2256/245—Methane
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2259/00—Type of treatment
    • B01D2259/40—Further details for adsorption processes and devices
    • B01D2259/416—Further details for adsorption processes and devices involving cryogenic temperature treatment
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
    • C01B2203/042—Purification by adsorption on solids
    • C01B2203/043—Regenerative adsorption process in two or more beds, one for adsorption, the other for regeneration
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
    • C01B2203/046—Purification by cryogenic separation
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
    • C01B2203/0465—Composition of the impurity
    • C01B2203/048—Composition of the impurity the impurity being an organic compound
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/14—Details of the flowsheet
    • C01B2203/146—At least two purification steps in series
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/02—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum
    • F25J2205/04—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum in the feed line, i.e. upstream of the fractionation step
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/40—Processes or apparatus using other separation and/or other processing means using hybrid system, i.e. combining cryogenic and non-cryogenic separation techniques
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/60—Processes or apparatus using other separation and/or other processing means using adsorption on solid adsorbents, e.g. by temperature-swing adsorption [TSA] at the hot or cold end
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2210/00—Processes characterised by the type or other details of the feed stream
    • F25J2210/04—Mixing or blending of fluids with the feed stream
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2210/00—Processes characterised by the type or other details of the feed stream
    • F25J2210/12—Refinery or petrochemical off-gas
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2215/00—Processes characterised by the type or other details of the product stream
    • F25J2215/62—Ethane or ethylene
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
    • F25J2230/08—Cold compressor, i.e. suction of the gas at cryogenic temperature and generally without afterstage-cooler
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
    • F25J2230/30—Compression of the feed stream
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
    • F25J2245/02—Recycle of a stream in general, e.g. a by-pass stream
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P30/00—Technologies relating to oil refining and petrochemical industry
    • Y02P30/40—Ethylene production

Definitions

  • Ethylene is recovered from light gas mixtures such as cracked gas from hydrocarbon crackers which contain various concentrations of hydrogen, methane, ethane, ethylene, propane, propylene, and minor amounts of higher hydrocarbons, nitrogen, and other trace components.
  • the recovery of ethylene from crude light hydrocarbon gas mixtures is an economically important but highly energy intensive process.
  • a method of separating ethylene which is simple, durable and cost-effective is desirable
  • a method for the recovery of ethylene from an off-gas includes providing an ethylene containing feed gas stream, introducing the ethylene containing gas stream into a first cryogenic separation device, thereby producing a first condensed stream and a first ethylene poor stream, and introducing the ethylene poor stream into a first feed compressor, thereby producing a pressurized first ethylene poor stream. This is repeated three times, resulting in a pressurized third ethylene poor stream, which is introduced into a pressure swing adsorber, thereby producing a high purity hydrogen stream and a PSA tail gas stream.
  • the PSA tail gas stream is into a PSA tail gas compressor, thereby producing a pressurized PSA tail gas stream, which is then combined with an ethylene containing gas stream to produce the ethylene containing feed gas stream.
  • the first condensed stream, the second condensed stream and the third condensed stream are combined to produce a combined condensed stream, which is introduced into an ethylene separation column thereby producing an ethylene rich stream and a methane rich stream.
  • the methane rich stream is introduced into a methane compressor thereby producing a methane fuel stream.
  • Figure 1 illustrates an embodiment of the present invention.
  • Figure 2 illustrates another embodiment of the present invention.
  • the off gas is chilled in the cold box, methane and ethylene condense and drop out as liquid stream.
  • the stream is chilled in several stages to economize on the compression power of Feed Compressor.
  • the condensed stream is sent to an ethylene separator column, where ethylene is concentrated at the bottom and methane rich stream is removed at the top.
  • the column is driven by providing heat in a reboiler from a suitable stream within the process.
  • An ethylene rich stream may contain 50-99% ethylene, balance being mainly methane. This stream may be recycled to ethylene plant for further purification or further purified in a separate system.
  • This method includes providing an ethylene containing feed gas stream 102, and introducing the ethylene containing feed gas stream 102 into feed compressor 103, thereby producing a pressurized ethylene containing feed stream 104. Then pressurized ethylene containing feed stream 104 is introduced into a cryogenic separation device 105, thereby producing an ethylene rich stream 108, a high pressure methane rich stream 106, a low pressure methane rich stream 114, and an ethylene poor stream 107.
  • the ethylene poor stream 107 is introduced into a pressure swing adsorber 109, thereby producing a high purity hydrogen stream 110 and a PSA tail gas stream 111.
  • the PSA tail gas stream 111 is introduced into a PSA tail gas compressor 112, thereby producing a pressurized PSA tail gas stream 113, which is then combined with an ethylene containing gas stream 101 to produce the ethylene containing feed gas stream 102.
  • the low pressure methane rich stream 114 is introduced into a methane compressor 115 thereby producing a methane fuel stream 116.
  • the ethylene containing gas stream 101 may have less than 10% ethylene.
  • the ethylene containing gas stream 101 may have less than 5% ethylene.
  • the ethylene containing gas stream 101 may have less than 60% methane.
  • the ethylene containing gas stream 101 may have less than 50% hydrogen.
  • the ethylene containing gas stream 101 may have a composition of about 40% hydrogen, about 58% methane, and about 2% ethylene.
  • the high purity hydrogen stream 110 may have a pressure of about 300 psig.
  • the methane fuel stream 116. may have a pressure of about 75 psig.
  • This method includes providing an ethylene containing feed gas stream 203, and introducing the ethylene containing gas stream 201 into a first cryogenic separation device 204, thereby producing a first condensed stream 206 and a first ethylene poor stream 205.
  • the ethylene poor stream 205 is introduced into a first feed compressor 207, thereby producing a pressurized first ethylene poor stream 208.
  • the pressurized first ethylene poor stream 208 is introduced into a second cryogenic separation device 209, thereby producing a second condensed stream 211 and a second ethylene poor stream 210.
  • the second ethylene poor stream 210 is introduced into a second feed compressor 212, thereby producing a pressurized second ethylene poor stream 213.
  • the pressurized second ethylene poor stream 213 is introduced into a third cryogenic separation device 214, thereby producing a third condensed stream 216 and a third ethylene poor stream 215.
  • the third ethylene poor stream 215 is introduced into a third feed compressor 217, thereby producing a pressurized third ethylene poor stream 218.
  • the pressurized third ethylene poor stream 218 is introduced into a pressure swing adsorber 219, thereby producing a high purity hydrogen stream 220 and a PSA tail gas stream 221.
  • the PSA tail gas stream 221 is introduced into a PSA tail gas compressor 222, thereby producing a pressurized PSA tail gas stream 223, which is then combined with an ethylene containing gas stream 201 to produce the ethylene containing feed gas stream 203.
  • the first condensed stream 206, the second condensed stream 211 and the third condensed stream 216 are combined to produce a combined condensed stream 224.
  • the combined condensed stream 224 is introduced into an ethylene separation column 225 thereby producing an ethylene rich stream 226 and a methane rich stream 227.
  • the methane rich stream 227 is introduced into a methane compressor 228 thereby producing a methane fuel stream 229.
  • the ethylene containing gas stream 201 may have less than 10% ethylene.
  • the ethylene containing gas stream 201 may have less than 5% ethylene.
  • the ethylene containing gas stream 201 may have less than 60% methane.
  • the ethylene containing gas stream 201 may have less than 50% hydrogen.
  • the ethylene containing gas stream 201 may have a composition of about 40% hydrogen, about 58% methane, and about 2% ethylene.
  • the high purity hydrogen stream 220 may have a pressure of about 300 psig.
  • the methane fuel stream 229. may have a pressure of about 75 psig.

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Combustion & Propulsion (AREA)
  • Inorganic Chemistry (AREA)
  • Analytical Chemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)

Abstract

A method for the recovery of ethylene from an off-gas is provided. This method includes providing an ethylene containing feed gas stream, introducing the ethylene containing gas stream into a first cryogenic separation device, thereby producing a first condensed stream and a first ethylene poor stream, and introducing the ethylene poor stream into a first feed compressor, thereby producing a pressurized first ethylene poor stream. This is repeated three times, resulting in a pressurized third ethylene poor stream, which is introduced into a pressure swing adsorber, thereby producing a high purity hydrogen stream and a PSA tail gas stream. The PSA tail gas stream is into a PSA tail gas compressor, thereby producing a pressurized PSA tail gas stream, which is then combined with an ethylene containing gas stream to produce the ethylene containing feed gas stream. The first condensed stream, the second condensed stream and the third condensed stream are combined to produce a combined condensed stream, which is introduced into an ethylene separation column thereby producing an ethylene rich stream and a methane rich stream. The methane rich stream is introduced into a methane compressor thereby producing a methane fuel stream.

Description

ETHYLENE RECOVERY FROM OFF-GAS
Background
Ethylene is recovered from light gas mixtures such as cracked gas from hydrocarbon crackers which contain various concentrations of hydrogen, methane, ethane, ethylene, propane, propylene, and minor amounts of higher hydrocarbons, nitrogen, and other trace components. The recovery of ethylene from crude light hydrocarbon gas mixtures is an economically important but highly energy intensive process. A method of separating ethylene which is simple, durable and cost-effective is desirable
Summary
A method for the recovery of ethylene from an off-gas is provided. This method includes providing an ethylene containing feed gas stream, introducing the ethylene containing gas stream into a first cryogenic separation device, thereby producing a first condensed stream and a first ethylene poor stream, and introducing the ethylene poor stream into a first feed compressor, thereby producing a pressurized first ethylene poor stream. This is repeated three times, resulting in a pressurized third ethylene poor stream, which is introduced into a pressure swing adsorber, thereby producing a high purity hydrogen stream and a PSA tail gas stream. The PSA tail gas stream is into a PSA tail gas compressor, thereby producing a pressurized PSA tail gas stream, which is then combined with an ethylene containing gas stream to produce the ethylene containing feed gas stream. The first condensed stream, the second condensed stream and the third condensed stream are combined to produce a combined condensed stream, which is introduced into an ethylene separation column thereby producing an ethylene rich stream and a methane rich stream. The methane rich stream is introduced into a methane compressor thereby producing a methane fuel stream.
Brief Description of the Figures
Figure 1 illustrates an embodiment of the present invention. Figure 2 illustrates another embodiment of the present invention.
Description of Preferred Embodiments
Illustrative embodiments of the invention are described below. While the invention is susceptible to various modifications and alternative forms, specific embodiments thereof have been shown by way of example in the drawings and are herein described in detail. It should be understood, however, that the description herein of specific embodiments is not intended to limit the invention to the particular forms disclosed, but on the contrary, the intention is to cover all modifications, equivalents, and alternatives falling within the spirit and scope of the invention as defined by the appended claims.
It will of course be appreciated that in the development of any such actual embodiment, numerous implementation-specific decisions must be made to achieve the developer's specific goals, such as compliance with system-related and business-related constraints, which will vary from one implementation to another. Moreover, it will be appreciated that such a development effort might be complex and time-consuming, but would nevertheless be a routine undertaking for those of ordinary skill in the art having the benefit of this disclosure.
As the off gas is chilled in the cold box, methane and ethylene condense and drop out as liquid stream. The stream is chilled in several stages to economize on the compression power of Feed Compressor. The condensed stream is sent to an ethylene separator column, where ethylene is concentrated at the bottom and methane rich stream is removed at the top. The column is driven by providing heat in a reboiler from a suitable stream within the process. An ethylene rich stream may contain 50-99% ethylene, balance being mainly methane. This stream may be recycled to ethylene plant for further purification or further purified in a separate system.
Turning now to fig. 1 , a method for the recovery of ethylene from an off- gas is provided. This method includes providing an ethylene containing feed gas stream 102, and introducing the ethylene containing feed gas stream 102 into feed compressor 103, thereby producing a pressurized ethylene containing feed stream 104. Then pressurized ethylene containing feed stream 104 is introduced into a cryogenic separation device 105, thereby producing an ethylene rich stream 108, a high pressure methane rich stream 106, a low pressure methane rich stream 114, and an ethylene poor stream 107.
The ethylene poor stream 107 is introduced into a pressure swing adsorber 109, thereby producing a high purity hydrogen stream 110 and a PSA tail gas stream 111. The PSA tail gas stream 111 is introduced into a PSA tail gas compressor 112, thereby producing a pressurized PSA tail gas stream 113, which is then combined with an ethylene containing gas stream 101 to produce the ethylene containing feed gas stream 102. The low pressure methane rich stream 114 is introduced into a methane compressor 115 thereby producing a methane fuel stream 116.
The ethylene containing gas stream 101 may have less than 10% ethylene. The ethylene containing gas stream 101 may have less than 5% ethylene. The ethylene containing gas stream 101 may have less than 60% methane. The ethylene containing gas stream 101 may have less than 50% hydrogen. The ethylene containing gas stream 101 may have a composition of about 40% hydrogen, about 58% methane, and about 2% ethylene. The high purity hydrogen stream 110 may have a pressure of about 300 psig. The methane fuel stream 116. may have a pressure of about 75 psig.
Turning now to fig. 2, a method for the recovery of ethylene from an off- gas is provided. This method includes providing an ethylene containing feed gas stream 203, and introducing the ethylene containing gas stream 201 into a first cryogenic separation device 204, thereby producing a first condensed stream 206 and a first ethylene poor stream 205. The ethylene poor stream 205 is introduced into a first feed compressor 207, thereby producing a pressurized first ethylene poor stream 208. The pressurized first ethylene poor stream 208 is introduced into a second cryogenic separation device 209, thereby producing a second condensed stream 211 and a second ethylene poor stream 210.
The second ethylene poor stream 210 is introduced into a second feed compressor 212, thereby producing a pressurized second ethylene poor stream 213. The pressurized second ethylene poor stream 213 is introduced into a third cryogenic separation device 214, thereby producing a third condensed stream 216 and a third ethylene poor stream 215. The third ethylene poor stream 215 is introduced into a third feed compressor 217, thereby producing a pressurized third ethylene poor stream 218. The pressurized third ethylene poor stream 218 is introduced into a pressure swing adsorber 219, thereby producing a high purity hydrogen stream 220 and a PSA tail gas stream 221.
The PSA tail gas stream 221 is introduced into a PSA tail gas compressor 222, thereby producing a pressurized PSA tail gas stream 223, which is then combined with an ethylene containing gas stream 201 to produce the ethylene containing feed gas stream 203. The first condensed stream 206, the second condensed stream 211 and the third condensed stream 216 are combined to produce a combined condensed stream 224. The combined condensed stream 224 is introduced into an ethylene separation column 225 thereby producing an ethylene rich stream 226 and a methane rich stream 227. The methane rich stream 227 is introduced into a methane compressor 228 thereby producing a methane fuel stream 229.
The ethylene containing gas stream 201 may have less than 10% ethylene. The ethylene containing gas stream 201 may have less than 5% ethylene. The ethylene containing gas stream 201 may have less than 60% methane. The ethylene containing gas stream 201 may have less than 50% hydrogen. The ethylene containing gas stream 201 may have a composition of about 40% hydrogen, about 58% methane, and about 2% ethylene. The high purity hydrogen stream 220 may have a pressure of about 300 psig. The methane fuel stream 229. may have a pressure of about 75 psig.

Claims

What is claimed is:
Claim 1 : A method for the recovery of ethylene from an off-gas, comprising; a) providing an ethylene containing feed gas stream,
b) introducing the ethylene containing feed gas stream into a feed
compressor, thereby producing a pressurized ethylene containing feed stream,
c) introducing said pressurized ethylene containing gas feed stream into a cryogenic separation device, thereby producing an ethylene rich stream, high pressure methane rich stream, a low pressure methane rich stream, and an ethylene poor stream,
d) introducing said ethylene poor stream into a pressure swing adsorber, thereby producing a high purity hydrogen stream and a PSA tail gas stream,
e) introducing said PSA tail gas stream into a PSA tail gas compressor, thereby producing a pressurized PSA tail gas stream, which is then combined with an ethylene containing gas stream to produce said ethylene containing feed gas stream,
f) introducing said low pressure methane rich stream to a methane
compressor thereby producing a methane fuel stream.
Claim 2: The method of claim 1 , wherein said ethylene containing gas stream has less than 10% ethylene.
Claim 3: The method of claim 2, wherein said ethylene containing gas stream has less than 5% ethylene Claim 4: The method of claim 2, wherein said ethylene containing gas stream has less than 60% methane.
Claim 5: The method of claim 2, wherein said ethylene containing gas stream has less than 50% hydrogen.
Claim 6: The method of claim 1 , wherein said ethylene containing gas stream has a composition of about 40% hydrogen, about 58% methane, and about 2% ethylene.
Claim 7: The method of claim 1 , wherein said high purity hydrogen stream has a pressure of about 300 psig.
Claim 8: The method of claim 1 , wherein said methane fuel stream has a pressure of about 75 psig.
Claim 9: A method for the recovery of ethylene from an off-gas, comprising; a) providing an ethylene containing feed gas stream ,
b) introducing said ethylene containing gas stream into a first cryogenic separation device, thereby producing a first condensed stream and a first ethylene poor stream,
c) introducing said ethylene poor stream into a first feed compressor,
thereby producing a pressurized first ethylene poor stream,
d) introducing said pressurized first ethylene poor stream into a second cryogenic separation device, thereby producing a second condensed stream and a second ethylene poor stream,
e) introducing said second ethylene poor stream into a second feed
compressor, thereby producing a pressurized second ethylene poor stream, f) introducing said pressurized second ethylene poor stream into a third cryogenic separation device, thereby producing a third condensed stream and a third ethylene poor stream,
g) introducing said third ethylene poor stream into a third feed compressor, thereby producing a pressurized third ethylene poor stream,
h) introducing said pressurized third ethylene poor stream into a pressure swing adsorber, thereby producing a high purity hydrogen stream (120) and a PSA tail gas stream,
i) introducing said PSA tail gas stream into a PSA tail gas compressor, thereby producing a pressurized PSA tail gas stream, which is then combined with an ethylene containing gas stream to produce said ethylene containing feed gas stream,
j) combining said first condensed stream, said second condensed stream and said third condensed stream to produce a combined condensed stream,
k) introducing said combined condensed stream into an ethylene separation column thereby producing an ethylene rich stream and a methane rich stream, and
I) introducing said methane rich stream to a methane compressor thereby producing a methane fuel stream.
Claim 10: The method of claim 9, wherein said ethylene containing gas stream (101 ) has less than 10% ethylene. Claim 1 1 : The method of claim 10, wherein said ethylene containing gas stream has less than 5% ethylene
Claim 12: The method of claim 10, wherein said ethylene containing gas stream has less than 60% methane. Claim 13: The method of claim 10, wherein said ethylene containing gas stream has less than 50% hydrogen.
Claim 14: The method of claim 9, wherein said ethylene containing gas stream has a composition of about 40% hydrogen, about 58% methane, and about 2% ethylene.
Claim 15: The method of claim 9, wherein said high purity hydrogen stream has a pressure of about 300 psig.
Claim 16: The method of claim 9, wherein said methane fuel stream has a pressure of about 75 psig.
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