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WO2018128982A1 - Procédé intégré de conversion de méthane en éthylène et benzène - Google Patents

Procédé intégré de conversion de méthane en éthylène et benzène Download PDF

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Publication number
WO2018128982A1
WO2018128982A1 PCT/US2018/012064 US2018012064W WO2018128982A1 WO 2018128982 A1 WO2018128982 A1 WO 2018128982A1 US 2018012064 W US2018012064 W US 2018012064W WO 2018128982 A1 WO2018128982 A1 WO 2018128982A1
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Prior art keywords
stream
reaction zone
reactor
zone
ethylene
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PCT/US2018/012064
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English (en)
Inventor
Krishnan Sankaranarayanan
Pankaj S. GAUTAM
Aghaddin Mamedov
Sreekanth Pannala
Balamurali Nair
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SABIC Global Technologies BV
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SABIC Global Technologies BV
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Publication of WO2018128982A1 publication Critical patent/WO2018128982A1/fr
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    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C2/00—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms
    • C07C2/02—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms by addition between unsaturated hydrocarbons
    • C07C2/42—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms by addition between unsaturated hydrocarbons homo- or co-oligomerisation with ring formation, not being a Diels-Alder conversion
    • C07C2/48—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms by addition between unsaturated hydrocarbons homo- or co-oligomerisation with ring formation, not being a Diels-Alder conversion of only hydrocarbons containing a carbon-to-carbon triple bond
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C5/00—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms
    • C07C5/02—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by hydrogenation
    • C07C5/08—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by hydrogenation of carbon-to-carbon triple bonds
    • C07C5/09—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by hydrogenation of carbon-to-carbon triple bonds to carbon-to-carbon double bonds
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G70/00—Working-up undefined normally gaseous mixtures obtained by processes covered by groups C10G9/00, C10G11/00, C10G15/00, C10G47/00, C10G51/00
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G70/00—Working-up undefined normally gaseous mixtures obtained by processes covered by groups C10G9/00, C10G11/00, C10G15/00, C10G47/00, C10G51/00
    • C10G70/02—Working-up undefined normally gaseous mixtures obtained by processes covered by groups C10G9/00, C10G11/00, C10G15/00, C10G47/00, C10G51/00 by hydrogenation
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G9/00—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
    • C10G2400/20—C2-C4 olefins
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
    • C10G2400/30—Aromatics
    • 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
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/10—Process efficiency
    • 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

  • the present disclosure relates to methods of producing olefins and aromatic hydrocarbons, more specifically methods of producing ethylene and benzene by integrating hydrocarbon pyrolysis with ethylene and benzene production.
  • Hydrocarbons and specifically olefins such as ethylene
  • ethylene can be typically used to produce a wide range of products, for example, break-resistant containers and packaging materials.
  • ethylene is produced by heating natural gas condensates and petroleum distillates, which include ethane and higher hydrocarbons, and the produced ethylene is separated from a product mixture by using gas separation processes.
  • Benzene is an important chemical, with applications ranging from chemical intermediates to solvents.
  • Benzene is a natural constituent of crude oil and it is used primarily as a precursor for manufacturing chemicals with more complex structure, such as cyclohexane, nitrobenzene, xylenes, ethylbenzene, cumene, and other various alkylbenzenes.
  • Benzene also has a high octane number, and as such is an important component of gasoline.
  • Benzene can also be used for making some types of rubbers, lubricants, dyes, detergents, drugs, explosives, and pesticides.
  • olefins such as ethylene
  • aromatic hydrocarbons such as benzene.
  • a process for producing ethylene and benzene comprising (a) introducing a fuel gas stream and an oxidant gas to a combustion zone to produce a combustion product, (b) introducing a first reactant mixture to a first reaction zone, wherein the first reactant mixture comprises a hydrocarbon stream and at least a portion of the combustion product, and wherein the combustion product heats the hydrocarbon stream to a first temperature effective for a pyrolysis reaction, (c) allowing at least a portion of the first reactant mixture to react via the pyrolysis reaction and produce a pyrolysis reaction product, wherein the pyrolysis reaction product comprises unconverted hydrocarbons, acetylene (C 2 H 2 ), ethylene (C 2 H 4 ), carbon monoxide (CO), hydrogen (H 2 ), water (H 2 0), and carbon dioxide (C0 2 ), (d) cooling at least a portion of the pyrolysis reaction product in a quench zone to form a cooled pyr
  • Also disclosed herein is a process for producing ethylene and benzene comprising (a) introducing a fuel gas stream and an oxidant gas to a combustion zone to produce a combustion product, (b) introducing a first reactant mixture to a first reaction zone, wherein the first reactant mixture comprises a hydrocarbon stream and at least a portion of the combustion product, and wherein the combustion product heats the hydrocarbon stream to a first temperature effective for a pyrolysis reaction, wherein the first temperature is equal to or greater than about 2,000 °C, (c) allowing at least a portion of the first reactant mixture to react via the pyrolysis reaction and produce a pyrolysis reaction product, wherein the pyrolysis reaction product comprises unconverted hydrocarbons, acetylene (C 2 H 2 ), ethylene (C 2 H 4 ), carbon monoxide (CO), hydrogen (H 2 ), water (H 2 0), and carbon dioxide (C0 2 ), (d) cooling at least a portion of the pyro
  • Figure 1 displays a schematic of an ethylene and benzene production system
  • Figure 2 displays a schematic of a reactor for the conversion of acetylene to ethylene and benzene
  • Figure 3 displays another schematic of a reactor for the conversion of acetylene to ethylene and benzene
  • Figure 4 displays yet another schematic of a reactor for the conversion of acetylene to ethylene and benzene
  • Figure 5 displays still yet another schematic of a reactor for the conversion of acetylene to ethylene and benzene.
  • ethylene and benzene comprising (a) introducing a fuel gas stream and an oxidant gas to a combustion zone to produce a combustion product; (b) introducing a first reactant mixture to a first reaction zone, wherein the first reactant mixture comprises a hydrocarbon stream and at least a portion of the combustion product, and wherein the combustion product heats the hydrocarbon stream to a first temperature effective for a pyrolysis reaction; (c) allowing at least a portion of the first reactant mixture to react via the pyrolysis reaction and produce a pyrolysis reaction product, wherein the pyrolysis reaction product comprises unconverted hydrocarbons, acetylene (C 2 H 2 ), ethylene (C 2 H 4 ), carbon monoxide (CO), hydrogen (3 ⁇ 4), water (H 2 0), and carbon dioxide (C0 2 ); (d) cooling at least a portion of the pyrolysis reaction product in a quench zone to form a cooled pyrolysis reaction
  • the second temperature is a temperature effective for acetylene hydrogenation to ethylene and/or acetylene trimerization to C 6 H 6 .
  • At least a portion of the first C0 2 stream can be fed to a syngas production unit to produce a second syngas stream.
  • at least a portion of the first syngas stream and/or at least a portion of the second syngas stream can be used for methanol production.
  • the terms “inhibiting” or “reducing” or “preventing” or “avoiding” or any variation of these terms include any measurable decrease or complete inhibition to achieve a desired result.
  • the term "effective,” means adequate to accomplish a desired, expected, or intended result.
  • the terms “comprising” (and any form of comprising, such as “comprise” and “comprises"), “having” (and any form of having, such as “have” and “has”), “including” (and any form of including, such as “include” and “includes”) or “containing” (and any form of containing, such as “contain” and “contains”) are inclusive or open-ended and do not exclude additional, unrecited elements or method steps.
  • the ethylene and benzene production system 100 generally comprises a pyrolysis zone 10 for methane (CH 4 ) cracking (e.g., combustion zone; first reaction zone; quenching zone); a second reaction zone 20 for the selective thermal hydrogenation of acetylene to ethylene and for the trimerization of acetylene to benzene (e.g., hydrogenation and trimerization reaction zone); a separation unit 30 for the recovery of ethylene, benzene and syngas (e.g., a first syngas stream); and a syngas production unit 40 for the hydrogenation of carbon dioxide (e.g., first C0 2 stream and/or second C0 2 stream) to carbon monoxide.
  • CH 4 methane
  • second reaction zone 20 for the selective thermal hydrogenation of acetylene to ethylene and for the trimerization of acetylene to benzene (e.g., hydrogenation and trimerization reaction zone)
  • a separation unit 30 for the recovery of ethylene, benzene
  • ethylene and benzene production system components shown in Figure 1 can be in fluid communication with each other (as represented by the connecting lines indicating a direction of fluid flow) through any suitable conduits (e.g., pipes, streams, etc.).
  • the pyrolysis zone 10 can comprise a combustion zone and a first reaction zone. Impurities and contaminants can be removed from a fuel gas stream and/or a hydrocarbon stream prior to introducing to the combustion zone and/or the first reaction zone, respectively.
  • the fuel gas stream and the hydrocarbon stream can be the same (e.g., can comprise the same hydrocarbons, for example can be portions of the same gas stream feedstock).
  • the fuel gas stream and the hydrocarbon stream can be the different (e.g., can comprise different hydrocarbons, for example originating from different upstream sources).
  • the fuel gas stream and/or the hydrocarbon stream can comprise methane, ethane, propane, natural gas, natural gas liquids, associated gas, well head gas, enriched gas, heavy hydrocarbons, petcoke, naphtha, heavy oil, heavy oil residue, and the like, or combinations thereof.
  • natural gas is a naturally occurring hydrocarbon gas mixture comprising mostly methane, but commonly including varying amounts of other higher alkanes, and sometimes a small percentage of carbon dioxide, nitrogen, hydrogen sulfide, helium, etc.
  • Heavy oil residues generally comprise polyalkylbenzenes such as polyethylbenzenes (PEBs), and well as multi-ring compounds.
  • Petcoke generally refers to a carbonaceous solid produced in oil refinery coker units or other cracking processes.
  • Heavy hydrocarbons generally comprise hydrocarbons which are solid or extremely viscous at standard processing conditions, and can include materials such as, but not limited to, asphaltenes, tars, paraffin waxes, coke, refining residues, and other similar residual hydrocarbon materials.
  • Heavy hydrocarbons can include any material that comprises a majority of hydrocarbon materials with a molecular weight range of about 700 to 2,000,000 Daltons.
  • Heavy oil generally refers to heavy crude, oils sands bitumen, bottom of the barrel and residue left over from refinery processes (e.g., visbreaker bottoms), and any other lower quality material that contains a substantial quantity of high boiling hydrocarbon fractions (e.g., that boil at or above 343°C, or alternatively at or above about 524°C).
  • Nonlimiting examples of heavy oil feedstocks include, but are not limited to, Lloydminster heavy oil, Cold Lake bitumen, Athabasca bitumen, atmospheric tower bottoms, vacuum tower bottoms, residuum (or "resid"), resid pitch, vacuum residue, and nonvolatile liquid fractions that remain after subjecting crude oil, bitumen from tar sands, liquefied coal, oil shale, or coal tar feedstocks to distillation, hot separation, and the like; and that contain higher boiling fractions and/or asphaltenes.
  • Naptha generally comprises flammable liquid hydrocarbon mixtures.
  • a process for producing ethylene and benzene as disclosed herein can comprise a step of introducing the fuel gas stream and an oxidant gas to the combustion zone to produce a combustion product.
  • the combustion zone can comprise a burner, such as an in-line burner; a furnace; or combinations thereof; wherein the fuel gas stream is burned (e.g., combusted) with the oxidant gas to produce the combustion product.
  • the oxidant gas can comprise oxygen, purified oxygen, air, oxygen-enriched air, and the like, or combinations thereof.
  • the oxidant gas is oxygen-enriched, such as oxygen-enriched air, to minimize NO x production in the combustion zone.
  • NO x products can be acidic and as such would necessitate downstream removal.
  • Water or steam can be further introduced to the combustion zone to lower and thereby control the combustion product temperature.
  • the combustion product generally comprises combustion products, such as carbon monoxide (CO), C0 2 , water (H 2 0), as well as some unconverted hydrocarbons (e.g., hydrocarbons that were present in the fuel gas stream and did not combust).
  • CO carbon monoxide
  • C0 2 water
  • H 2 0 water
  • some unconverted hydrocarbons e.g., hydrocarbons that were present in the fuel gas stream and did not combust.
  • the combustion product may not be isolatable, and it might be introduced as produced to the first reaction zone.
  • a process for producing ethylene and benzene as disclosed herein can comprise introducing a first reactant mixture to the first reaction zone, wherein the first reactant mixture comprises the hydrocarbon stream and at least a portion of the combustion product, and wherein the combustion product heats the hydrocarbon stream to a first temperature effective for a pyrolysis reaction; and allowing at least a portion of the first reactant mixture to react via the pyrolysis reaction and produce a pyrolysis reaction product.
  • the pyrolysis reaction product can comprise unconverted hydrocarbons, acetylene, ethylene, CO, H 2 , water, and C0 2 .
  • the first reaction zone excludes the catalyst.
  • the catalyst As will be appreciated by one of skill in the art, and with the help of this disclosure, while there are catalytic processes for hydrocarbon pyrolysis (e.g., methane pyrolysis), the current disclosure does not utilize a catalyst for hydrocarbon pyrolysis; the hydrocarbon pyrolysis as disclosed herein is thermal in contrast to catalyzed.
  • the pyrolysis zone 10 can comprise a reactor (e.g., a first reactor) that contains both the combustion zone and the first reaction zone.
  • the pyrolysis zone 10 can comprise a furnace that contains the combustion zone; and a reactor (e.g., a first reactor) that contains the first reaction zone and is configured to receive the combustion product from the furnace comprising the combustion zone.
  • a diluent such as an inert gas (e.g., nitrogen, argon, helium, etc.) and/or steam can be further introduced to the first reaction zone.
  • the hydrocarbon stream can be further pre-heated in pre-heaters (e.g., electrical heaters, heat exchangers, etc.) before being heated to the first temperature (e.g., temperature effective for the pyrolysis reaction) by direct heat exchange through contact with the combustion product.
  • pre-heaters e.g., electrical heaters, heat exchangers, etc.
  • a temperature of the combustion product can be a temperature effective to reach a pyrolysis reaction temperature (e.g., first temperature, first reaction zone temperature) of equal to or greater than about 1,000 °C, alternatively equal to or greater than about 1,500 °C, alternatively equal to or greater than about 2,000 °C, alternatively equal to or greater than about 2,250 °C, alternatively from about 1,000 °C to about 2,500 °C, alternatively from about 1,500 °C to about 2,500 °C, or alternatively from about 2,000 °C to about 2,500 °C.
  • a pyrolysis reaction temperature e.g., first temperature, first reaction zone temperature
  • higher temperatures in the first reaction zone favor alkyne (e.g., acetylene) formation, while lower temperatures in the first reaction zone favor olefin or alkene (e.g., ethylene) formation.
  • alkyne e.g., acetylene
  • alkene e.g., ethylene
  • the first reaction zone can be characterized by a residence time effective to allow for the conversion of at least a portion of the first reactant mixture to acetylene and ethylene.
  • the first reaction zone can be characterized by a residence time of from about 0.1 milliseconds (ms) to 100 ms, alternatively from about 0.5 ms to about 80 ms, or alternatively from about 1 ms to about 50 ms.
  • the hydrocarbon stream that is introduced to the first reaction zone can be characterized by a pressure of from about 1 bar to about 20 bar (e.g., from about 100 kPa to about 2,000 kPa), to achieve the desired products.
  • the pyrolysis zone 10 can be designed to accommodate one or more gas feed streams (e.g., fuel gas stream, hydrocarbon stream), which may employ natural gas combined with other gas components including, but not limited to hydrogen, carbon monoxide, carbon dioxide, ethane, and ethylene.
  • the pyrolysis zone 10 can be designed to accommodate one or more oxidant gas streams, such as an oxygen stream and an oxygen-containing stream, for example an air stream, which employ unequal oxidant concentrations for purposes of temperature or composition control.
  • the pyrolysis zone 10 may comprise a single device or multiple devices. Each device of the pyrolysis zone 10 may comprise one or more sections.
  • Products from the combustion zone are communicated to the first reaction zone via the combustion product stream.
  • the combustion product stream may not be isolatable (for example, in configurations where the combustion zone and the first reaction zone are contained within a common vessel or reactor).
  • a process for producing ethylene and benzene as disclosed herein can comprise cooling at least a portion of the pyrolysis reaction product in a quench zone to form a cooled pyrolysis reaction product, wherein the cooled pyrolysis reaction product is characterized by a second temperature, and wherein the second temperature is lower than the first temperature.
  • the pyrolysis zone 10 can further comprise a quench zone, wherein the pyrolysis reaction products are quenched prior to exiting the pyrolysis unit 10 via the cooled pyrolysis reaction product.
  • the quench zone can employ any suitable quenching methods, for example spraying a quench fluid such as steam, water, oil, or liquid product into a reactor quench zone or chamber; conveying the product stream through or into water, natural gas feed, or liquid products; preheating other streams such as fuel gas stream and/or hydrocarbon stream; generating steam; expanding in a kinetic energy quench, such as a Joule Thompson expander, choke nozzle, turbo expander, etc.; or combinations thereof.
  • a quench fluid such as steam, water, oil, or liquid product into a reactor quench zone or chamber
  • preheating other streams such as fuel gas stream and/or hydrocarbon stream
  • generating steam expanding in a kinetic energy quench, such as a Joule Thompson expander, choke nozzle, turbo expander, etc.; or combinations thereof.
  • a pyrolysis reactor e.g., a first reactor
  • the cooled pyrolysis reaction product can comprise unconverted hydrocarbons, acetylene, ethylene, CO, H 2 , water (H 2 0), and C0 2 .
  • water produced in the combustion zone can react with methane to produce syngas.
  • a first reactor can comprise the first reaction zone.
  • the first reactor can further comprise the combustion zone, the quench zone, or both the combustion zone and the quench zone.
  • the pyrolysis zone 10 can comprise the first reactor comprising the combustion zone, the first reaction zone, and the quench zone.
  • a process for producing ethylene and benzene as disclosed herein can comprise introducing the cooled pyrolysis reaction product to the second reaction zone 20 (e.g., hydrogenation and trimerization reaction zone); and allowing a first portion of the acetylene in the cooled pyrolysis reaction product to undergo hydrogenation to ethylene and a second portion of the acetylene in the cooled pyrolysis reaction product to undergo trimerization to benzene, to produce a second reaction zone effluent, wherein the second reaction zone effluent comprises unconverted hydrocarbons, unconverted C 2 H 2 , C 2 H 4 , benzene (C63 ⁇ 4), CO, H 2 , H 2 0, and C0 2 ; and wherein an amount of C 2 H 4 in the second reaction zone effluent is greater than an amount of C 2 H 4 in the cooled pyrolysis reaction product.
  • the second reaction zone effluent comprises unconverted hydrocarbons, unconverted C 2 H 2 , C 2 H
  • the cooled pyrolysis reaction product that is introduced to the second reaction zone 20 can comprise (i) acetylene in an amount of from about 5 vol.% to about 30 vol.%, alternatively from about 10 vol.% to about 25 vol.%, or alternatively from about 13 vol.% to about 18 vol.%, based on the total volume of the cooled pyrolysis reaction product; (ii) hydrogen in an amount of from about 10 vol.% to about 70 vol.%, alternatively from about 40 vol.% to about 70 vol.%, or alternatively from about 45 vol.% to about 60 vol.%, based on the total volume of the cooled pyrolysis reaction product; (iii) methane (e.g., unconverted methane from pyrolysis) in an amount of from about 5 vol.% to about 30 vol.%, alternatively from about 10 vol.% to about 25 vol.%, or alternatively from about 13 vol.% to about 18 vol.%, based on the total volume of the cooled
  • the second reaction zone 20 can be characterized by the second temperature, wherein the second temperature is a temperature effective for acetylene hydrogenation to ethylene and/or acetylene trimerization to C 6 H 6 .
  • the second temperature can be from about 600 °C to about 1,000 °C, alternatively from about 750 °C to about 975 °C, or alternatively from about 850 °C to about 950 °C.
  • the second reaction zone 20 excludes a catalyst.
  • a catalyst such as palladium (Pd), for example
  • the current disclosure does not utilize a catalyst for the conversion of acetylene to ethylene and/or benzene; the conversion of acetylene to ethylene and/or benzene as disclosed herein is thermal in contrast to catalyzed.
  • the second reaction zone 20 excludes liquid phase hydrogenation of acetylene to ethylene.
  • the entire contents of the second reaction zone 20 are in gas phase (e.g., 100% gas phase reaction zone).
  • the second reaction zone 20 employs the simultaneous production of benzene and ethylene by thermal conversion of acetylene in a non-metallic reactor, which in some configurations can be a tubular reactor.
  • the thermal conversion of acetylene with simultaneous production of benzene and ethylene can occur in the presence of one or more non-metallic surfaces, wherein the one or more non-metallic surfaces can comprise inner reactor walls or surfaces, reactor packing material surfaces (e.g., thermally conductive material particles surfaces), and the like, or combinations thereof.
  • the second reaction zone 20 is contained in a non-metallic reactor, such as a glass-lined reactor, a quartz-lined reactor, or a ceramic-lined reactor.
  • the second reaction zone is defined by non-metallic boundaries, such as one or more glass boundaries, one or more quartz boundaries, one or more ceramic boundaries, and the like, or combinations thereof.
  • acetylene conversion undesirably proceeds in the direction of a deep decomposition of acetylene with formation of hydrogen and coke fragments.
  • a common reactor can comprise both the first reaction zone and the second reaction zone 20.
  • the common reactor can have an inner common reactor surface, wherein at least a portion of the inner common reactor surface contacts the cooled pyrolysis reaction product, and wherein at least a portion of the inner common reactor surface is non-metallic.
  • the portion of the common reactor that contains the second reaction zone has an inner surface (e.g., inner common reactor surface) that is non-metallic, for example glass, quartz, ceramic, and the like, or combinations thereof.
  • At least the portion of the common reactor that contains the second reaction zone can be lined with glass, quartz, ceramic, and the like, or combinations thereof, to provide for a non-metallic inner common reactor surface.
  • the common reactor that comprises both the first reaction zone and the second reaction zone can further comprise the quench zone and optionally the combustion zone.
  • the common reactor can be an autothermal reactor.
  • the first reactor can comprise the first reaction zone, and a second reactor can comprise the second reaction zone 20.
  • the second reactor can have an inner second reactor surface, wherein at least a portion of the inner second reactor surface contacts the cooled pyrolysis reaction product, and wherein the inner second reactor surface is non-metallic, for example glass, quartz, ceramic, and the like, or combinations thereof.
  • the second reactor can be an autothermal reactor.
  • the second reaction zone 20 can comprise a reactor packing material, wherein the reactor packing material is non-metallic and/or has non-metallic surfaces.
  • the reactor packing material can be of any suitable size or shape to provide a desired effective surface area, fluid flow characteristics, heat exchange, and the like.
  • the reactor packing material can be part of a fixed bed of a fluidized bed in the second reaction zone 20.
  • the reactor packing material can have any suitable size or shape, such as fibers, filaments, particles, spheres, pellets, rods, cylinders, trilobes, quadralobes, and the like, or combinations thereof.
  • the reactor packing material can comprise thermally conductive material particles, wherein the thermally conductive material particles are non-metallic and/or have non- metallic surfaces.
  • the thermally conductive material particles can be glass particles, quartz particles, ceramic particles, and the like, or combinations thereof.
  • the thermally conductive material particles can have surfaces that are coated with non-metallic materials (e.g., glass, quartz, ceramic, and the like, or combinations thereof), such as glass-coated particles, quartz-coated particles, ceramic-coated particles, and the like, or combinations thereof.
  • the spent thermally conductive material particles can be regenerated by (i) removing at least a portion of the spent thermally conductive material particles from the second reaction zone; (ii) burning the coke off the at least a portion of the spent thermally conductive material particles in an oxidant gas, thereby producing the thermally conductive material particles (e.g., regenerated thermally conductive material particles) and the second C0 2 stream; and (iii) reintroducing at least a portion of the regenerated thermally conductive material particles to the second reaction zone.
  • the second reaction zone can be contained in a riser type reactor with an outer thermally conductive material particles regeneration flow or circulation loop such as shown in Figure 5.
  • the second reaction zone can be characterized by a space velocity of from about 400 h "1 to about 5,000 h “1 , or alternatively from about 1,800 h "1 to about 3,000 h “1 .
  • the space velocity is an important factor affecting the benzene/ethylene ratio in the second reaction zone effluent, wherein a high space velocity gives a high ethylene yield, while a low space velocity gives a high benzene yield.
  • a process for producing ethylene and benzene as disclosed herein can comprise separating in separation unit 30 at least a portion of the second reaction zone effluent into an ethylene stream, a benzene stream, a first C0 2 stream, and a first syngas stream, wherein the first syngas stream comprises H 2 and CO.
  • the first syngas stream can be characterized by a H 2 /CO molar ratio of from about 1 :1 to about 2: 1, alternatively from about 1.1 : 1 to about 1.95: 1, or alternatively from about 1.2: 1 to about 1.9: 1.
  • the separation unit 30 can employ distillation and/or cryogenic distillation to produce the ethylene stream, the benzene stream, and the first syngas stream.
  • At least a portion of the first C0 2 stream and/or at least a portion of the second C0 2 stream can be contacted with hydrogen in a syngas production unit 40 to produce a second syngas stream comprising H 2 and CO.
  • the second syngas stream can be characterized by a H 2 /CO molar ratio of from about 1 :1 to about 2: 1, alternatively from about 1.1 : 1 to about 1.95: 1, or alternatively from about 1.2:1 to about 1.9: 1.
  • C0 2 can be converted to syngas by using a hydrogenating agent, e.g., hydrogen or any suitable compound that can provide hydrogen for hydrogenation reaction. Hydrogenation of C0 2 to syngas composition can be described by reactions (l)-(3):
  • reaction (1) is an equilibrium controlled reaction which depends on the H 2 /C0 2 ratio, as it can be seen from reactions (2) and (3).
  • a catalyst for C0 2 hydrogenation to syngas can comprise mixed oxides of redox types, for example Cr, Fe, Mn, or Cu based oxides.
  • the hydrogenation of carbon dioxide to syngas can be conducted in the presence of a CATOFIN catalyst, which is a chromium (Cr) based catalyst commercially available from Clariant, wherein the resulting syngas composition is suitable for methanol and/or olefins synthesis.
  • the composition of syngas produced by C0 2 hydrogenation is dependent upon the H 2 /C0 2 ratio and on the C0 2 hydrogenation temperature.
  • a third reaction zone e.g., methanol production unit
  • a catalyst to produce a methanol stream.
  • a feed stream to the third reaction zone can be characterized by a H 2 /CO molar ratio of about 2:1, alternatively about 2.1 : 1, alternatively from about 1.5:1 to about 2.5:1, alternatively from about 1.8: 1 to about 2.3:1, or alternatively from about 2.0: 1 to about 2.1 : 1.
  • the H 2 /CO molar ratio of the feed stream to the third reaction zone can be adjusted as necessary to meet the requirements of the methanol production unit, for example by varying a ratio of the first syngas stream to the second syngas stream; by subjecting the first syngas stream and/or the second syngas stream to a water-gas shift reaction; and the like; or combinations thereof.
  • the water-gas shift reaction describes the catalytic reaction of carbon monoxide and water vapor to form carbon dioxide and hydrogen according to the reaction CO + H 2 0 ⁇ C0 2 + H 2 .
  • the water-gas shift reaction is used to increase the H 2 /CO molar ratio of gas streams comprising carbon monoxide and hydrogen (e.g., syngas streams).
  • Water-gas shift catalysts can comprise any suitable water-gas shift catalysts, such as commercial water-gas shift catalysts; chromium or copper promoted iron-based catalysts; copper-zinc-aluminum catalyst; and the like; or combinations thereof.
  • the H 2 /CO molar ratio of the second syngas stream can be increased by increasing the amount of hydrogen introduced to the syngas production unit 40, as shown in reactions (2) and (3).
  • the methanol production unit can comprise any reactor suitable for a methanol synthesis reaction from CO and H 2 , such as for example an isothermal reactor, an adiabatic reactor, a slurry reactor, a cooled multi tubular reactor, and the like, or combinations thereof.
  • At least a portion of the CO and at least a portion of the H 2 of a feed stream to the methanol production unit can undergo a methanol synthesis reaction.
  • Methanol synthesis from CO and H 2 is a catalytic process, and is most often conducted in the presence of copper based catalysts.
  • the third reaction zone can comprise a catalyst, such as any suitable commercial catalyst used for methanol synthesis.
  • Nonlimiting examples of catalysts suitable for use in the methanol production unit in the current disclosure include Cu, Cu/ZnO, Cu/Th0 2 , Cu/Zn/Al 2 0 3 , Cu/ZnO/Al 2 0 3 , Cu/Zr, and the like, or combinations thereof.
  • coke can be further separated from the second reaction zone effluent, for example by using cyclones, centrifugation, screening, or any other suitable particulates removal or separation systems.
  • coke is an undesired by-product in the process for producing ethylene and benzene as disclosed herein, and as such, the lower the amount of produced coke, the better.
  • the process for producing ethylene and benzene as disclosed herein can be characterized by a selectivity to coke of less than about 25%, alternatively less than about 20%, or alternatively less than about 15%.
  • a selectivity to a certain product refers to the amount of that particular product formed divided by the total amount of products formed.
  • the process for producing ethylene and benzene as disclosed herein can be characterized by a selectivity to ethylene and benzene of equal to or greater than about 50%, alternatively equal to or greater than about 60%, or alternatively equal to or greater than about 75%.
  • a process for producing ethylene and benzene as disclosed herein can comprise (a) introducing a fuel gas stream and an oxidant gas to a combustion zone to produce a combustion product; (b) introducing a first reactant mixture to a first reaction zone, wherein the first reactant mixture comprises a hydrocarbon stream and at least a portion of the combustion product, and wherein the combustion product heats the hydrocarbon stream to a first temperature effective for a pyrolysis reaction, wherein the first temperature is equal to or greater than about 2,000 °C; (c) allowing at least a portion of the first reactant mixture to react via the pyrolysis reaction and produce a pyrolysis reaction product, wherein the pyrolysis reaction product comprises unconverted hydrocarbons, acetylene (C 2 H 2 ), ethylene (C 2 H 4 ), carbon monoxide (CO), hydrogen (3 ⁇ 4), water (H 2 0), and carbon dioxide (C0 2 ); (d) cooling at least a portion of the
  • a process for producing ethylene and benzene as disclosed herein can advantageously display improvements in one or more process characteristics when compared to an otherwise similar process that does not integrate hydrocarbon pyrolysis with other processes for producing desired products.
  • a synthesis gas (e.g., 3 ⁇ 4 and CO) to methanol conversion process as disclosed herein can increase further the overall efficiency of the process by producing methanol from the H 2 and CO obtained from hydrocarbon pyrolysis, as well as C0 2 hydrogenation.
  • Methane catalytic conversion to benzene generally displays a very low conversion, and it is hindered by a high rate of catalyst deactivation.
  • thermal conversion of methane to acetylene, with subsequent thermal conversion of acetylene to both benzene and ethylene advantageously improves the overall process efficiency for the conversion of natural gas to aromatic hydrocarbons such as benzene.
  • a further increase in overall process efficiency can be achieved by methanol production from the syngas produced in the process.
  • the methanol can be advantageously used as a liquid fuel, and can be easily transported, as compared to transporting gases. Additional advantages of the process for producing ethylene and benzene as disclosed herein can be apparent to one of skill in the art viewing this disclosure.
  • the combustion and pyrolysis of methane was investigated at high temperature, and the products after pyrolysis were quenched to room temperature.
  • the combustion and pyrolysis was conducted via three steps: (i) the combustion of fuel gases in a combustion chamber; (ii) mixing of cracking feed (natural gas/field gas) with the products of combustion in a mixing section; followed by (iii) the cracking or pyrolysis of the above mixture from step (ii) in the reactor section.
  • the combustion chamber produced hot gases with a temperature of about 2,500 °C.
  • the hot gases produced in the combustion chamber were mixed with feed natural gas which was optionally preheated to 300-500 °C.
  • the combustion gases transferred heat to the feed natural gas by direct contact and the feed underwent pyrolysis.
  • the data in Table 1 provides a typical composition of various gas streams produced in the methane combustion and pyrolysis as disclosed herein. As can be seen from data in Table 1 , a C 2 yield of about 30% was achieved. The achieved C 2 yield is high by comparison with the maximum C 2 yield (less than 24%, as outlined in J. Chem. Soc, Chem. Commun., 1992, p. 1546, which is incorporated by reference herein in its entirety) that can be obtained via catalytic oxidative methane coupling.
  • the outlet gases comprised C 2 H 4 , C 6 H6, CH 4 , CO, H 2 , C0 2 , and coke.
  • the conversion of acetylene was 96%, with a total selectivity to C 2 H 4 + benzene of 65%.
  • CO selectivity was 18%, and coke selectivity was 17%.
  • C0 2 separated from a regeneration gas could be connected with a main stream CO/C0 2 stream of a reactor outlet and could be converted to syngas, and subsequently to methanol.
  • a first aspect which is a process for ethylene and benzene comprising (a) introducing a fuel gas stream and an oxidant gas to a combustion zone to produce a combustion product; (b) introducing a first reactant mixture to a first reaction zone, wherein the first reactant mixture comprises a hydrocarbon stream and at least a portion of the combustion product, and wherein the combustion product heats the hydrocarbon stream to a first temperature effective for a pyrolysis reaction; (c) allowing at least a portion of the first reactant mixture to react via the pyrolysis reaction and produce a pyrolysis reaction product, wherein the pyrolysis reaction product comprises unconverted hydrocarbons, acetylene (C 2 H 2 ), ethylene (C 2 H 4 ), carbon monoxide (CO), hydrogen (3 ⁇ 4), water (3 ⁇ 40), and carbon dioxide (CO 2 ); (d) cooling at least a portion of the pyrolysis reaction product in a quench zone to form a cooled pyrolysis reaction product,
  • a second aspect which is the process of the first aspect, wherein the second reaction zone is contained within a glass-lined reactor, a quartz-lined reactor, or a ceramic-lined reactor.
  • a third aspect which is the process of the second aspect, wherein the first reaction zone and the second reaction zone exclude a catalyst.
  • a fourth aspect which is the process of the third aspect, wherein a common reactor comprises both the first reaction zone and the second reaction zone.
  • a fifth aspect which is the process of the fourth aspect, wherein the common reactor has an inner common reactor surface, wherein at least a portion of the inner common reactor surface contacts the cooled pyrolysis reaction product, and wherein at least a portion of the inner common reactor surface is non-metallic.
  • a sixth aspect which is the process of the fifth aspect, wherein the inner common reactor surface comprises glass, quartz, ceramic, or combinations thereof.
  • a seventh aspect which is the process of any one of the first through the sixth aspects, wherein at least a portion of the common reactor is lined with glass, quartz, ceramic, or combinations thereof.
  • An eighth aspect which is the process of any one of the first through the seventh aspects, wherein the common reactor further comprises the quench zone and optionally the combustion zone.
  • a ninth aspect which is the process of any one of the first through the eighth aspects, wherein the common reactor comprises an autothermal reactor.
  • a tenth aspect which is the process of the third aspect, wherein a first reactor comprises the first reaction zone, and wherein a second reactor comprises the second reaction zone.
  • An eleventh aspect which is the process of the tenth aspect, wherein the second reactor has an inner second reactor surface, wherein at least a portion of the inner second reactor surface contacts the cooled pyrolysis reaction product.
  • a twelfth aspect which is the process of the eleventh aspect, wherein the inner second reactor surface is non-metallic.
  • a thirteenth aspect which is the process of any one of the tenth through the twelfth aspects, wherein the inner second reactor surface comprises glass, quartz, ceramic, or combinations thereof.
  • a fourteenth aspect which is the process of any one of the tenth through the thirteenth aspects, wherein the first reactor further comprises the quench zone.
  • a fifteenth aspect which is the process of the fourteenth aspect, wherein the first reactor further comprises the combustion zone.
  • a sixteenth aspect which is the process of any one of the first through the fifteenth aspects, wherein the second reaction zone excludes liquid phase hydrogenation of acetylene to ethylene.
  • a seventeenth aspect which is the process of any one of the first through the sixteenth aspects, wherein the first temperature is equal to or greater than about 2,000 °C.
  • An eighteenth aspect which is the process of any one of the first through the seventeenth aspects, wherein the second temperature is a temperature effective for acetylene hydrogenation to ethylene and/or acetylene trimerization to C 6 H 6 .
  • a nineteenth aspect which is the process of any one of the first through the eighteenth aspects, wherein the second temperature is from about 600 °C to about 1,000 °C.
  • a twentieth aspect which is the process of any one of the first through the nineteenth aspects, wherein the second temperature is from about 850 °C to about 950 °C.
  • a twenty-first aspect which is the process of any one of the first through the twentieth aspects, wherein the second reaction zone comprises thermally conductive material particles.
  • a twenty-second aspect which is the process of the twenty-first aspect, wherein the thermally conductive material particles are non-metallic and/or have non-metallic surfaces.
  • a twenty-third aspect which is the process of any one of the first through the twenty- second aspects, wherein the thermally conductive material particles comprise glass, quartz, ceramic, or combinations thereof.
  • a twenty-fourth aspect which is the process of any one of the first through the twenty-third aspects, wherein coke is deposited on the thermally conductive material particles during step (f) to produce spent thermally conductive material particles, and wherein at least a portion of the spent thermally conductive material particles is regenerated to produce the thermally conductive material particles and a second C0 2 stream.
  • a twenty-fifth aspect which is the process of the twenty-fourth aspect, wherein at least a portion of the first C0 2 stream and/or at least a portion of the second C0 2 stream is contacted with hydrogen to produce a second syngas stream comprising H 2 and CO.
  • a twenty-sixth aspect which is the process of the twenty-fifth aspect, wherein the second syngas stream is characterized by a H 2 /CO molar ratio of from about 1 : 1 to about 2: 1.
  • a twenty-seventh aspect which is the process of any one of the first through the twenty-sixth aspects, wherein at least a portion of the first syngas stream and/or at least a portion of the second syngas stream is introduced to a third reaction zone comprising a catalyst to produce a methanol stream.
  • a twenty-eighth aspect which is the process of the twenty-seventh aspect, wherein the catalyst for the third reaction zone comprises Cu, Cu/ZnO, Cu/Th0 2 , Cu/Zn/Al 2 0 3 , Cu/ZnO/Al 2 0 3 , Cu/Zr, or combinations thereof.
  • a twenty-ninth aspect which is the process of any one of the first through the twenty- eighth aspects, wherein the first syngas stream is characterized by a H 2 /CO molar ratio of from about 1 : 1 to about 2: 1.
  • a thirtieth aspect which is the process of any one of the first through the twenty- ninth aspects, wherein the first C0 2 stream is separated from the second reaction zone effluent by amine absorption.
  • a thirty-first aspect which is the process of any one of the first through the thirtieth aspects, wherein the fuel gas stream and the hydrocarbon stream are the same or different.
  • a thirty-second aspect which is the process of any one of the first through the thirty- first aspects, wherein the fuel gas stream and/or the hydrocarbon stream comprise methane, ethane, propane, natural gas, natural gas liquids, associated gas, well head gas, enriched gas, heavy hydrocarbons, petcoke, naphtha, heavy oil, heavy oil residue, or combinations thereof.
  • a thirty-third aspect which is the process of any one of the first through the thirty- second aspects, wherein the oxidant gas comprises oxygen, purified oxygen, air, oxygen- enriched air, or combinations thereof.
  • a thirty-fourth aspect which is the process of any one of the first through the thirty- third aspects, wherein coke is further separated from the second reaction zone effluent.
  • a thirty-fifth aspect which is the process of the thirty-fourth aspect, wherein a selectivity to coke is less than about 25%.
  • a thirty-sixth aspect which is the process of any one of the first through the thirty- fifth aspects, wherein a selectivity to ethylene and benzene is equal to or greater than about 50%.
  • a thirty-seventh aspect which is a process for producing ethylene and benzene comprising (a) introducing a fuel gas stream and an oxidant gas to a combustion zone to produce a combustion product; (b) introducing a first reactant mixture to a first reaction zone, wherein the first reactant mixture comprises a hydrocarbon stream and at least a portion of the combustion product, and wherein the combustion product heats the hydrocarbon stream to a first temperature effective for a pyrolysis reaction, wherein the first temperature is equal to or greater than about 2,000 °C; (c) allowing at least a portion of the first reactant mixture to react via the pyrolysis reaction and produce a pyrolysis reaction product, wherein the pyrolysis reaction product comprises unconverted hydrocarbons, acetylene (C 2 H 2 ), ethylene (C 2 H 4 ), carbon monoxide (CO), hydrogen (H 2 ), water (H 2 0), and carbon dioxide (C0 2 ); (d) cooling at least a portion
  • a thirty-eighth aspect which is the process of the thirty-seventh aspect, wherein a selectivity to coke is less than about 20%, and wherein a selectivity to ethylene and benzene is equal to or greater than about 60%.

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Abstract

La présente invention concerne un procédé de production d'éthylène et de benzène comprenant les étapes consistant à : introduire le combustible et l'oxydant dans une zone de combustion pour produire un produit de combustion; introduire un premier mélange réactif comprenant des hydrocarbures et un produit de combustion dans une première zone de réaction, le produit de combustion chauffant des hydrocarbures à une température efficace pour la pyrolyse; permettre à un premier mélange réactif de réagir par pyrolyse et produire un produit de pyrolyse comprenant des hydrocarbures non convertis, C2H2, C2H4, CO, H2, H2O et CO2; refroidir le produit de pyrolyse dans la zone de refroidissement pour former un produit de pyrolyse refroidi; introduire un produit de pyrolyse refroidi dans une seconde zone de réaction; permettre à une première partie d'acétylène dans le produit de pyrolyse refroidi de subir une hydrogénation à l'éthylène et une seconde partie d'acétylène dans le produit de pyrolyse refroidi pour subir une trimérisation au benzène, pour produire un effluent de seconde zone comprenant des hydrocarbures non convertis, C2H2, C2H4, C6H6, CO, H2, H2O et CO2; et séparer l'effluent de la seconde zone en éthylène, benzène, CO2 et gaz de synthèse.
PCT/US2018/012064 2017-01-04 2018-01-02 Procédé intégré de conversion de méthane en éthylène et benzène Ceased WO2018128982A1 (fr)

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Cited By (2)

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CN112707884A (zh) * 2019-10-24 2021-04-27 中国石油化工股份有限公司 一种乙交酯及其制备方法与应用
CN114920618A (zh) * 2022-05-27 2022-08-19 汕尾职业技术学院 一种乙炔和乙烯共进料芳构化制备苯的方法和催化剂

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US8080697B2 (en) * 2006-01-23 2011-12-20 Saudi Basic Industries Corporation Process for the production of ethylene from natural gas with heat integration

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US3156733A (en) * 1960-12-02 1964-11-10 Happel John Selective pyrolysis of methane to acetylene and hydrogen
US6323247B1 (en) * 1998-11-25 2001-11-27 Texas A & M University Syst Method for converting natural gas to liquid hydrocarbons
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* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN112707884A (zh) * 2019-10-24 2021-04-27 中国石油化工股份有限公司 一种乙交酯及其制备方法与应用
CN112707884B (zh) * 2019-10-24 2022-07-12 中国石油化工股份有限公司 一种乙交酯及其制备方法与应用
CN114920618A (zh) * 2022-05-27 2022-08-19 汕尾职业技术学院 一种乙炔和乙烯共进料芳构化制备苯的方法和催化剂

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