US3192732A - Low temperature refrigeration in ethylene plants - Google Patents

Low temperature refrigeration in ethylene plants Download PDF

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US3192732A
US3192732A US105144DA US3192732A US 3192732 A US3192732 A US 3192732A US 105144D A US105144D A US 105144DA US 3192732 A US3192732 A US 3192732A
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ethane
line
refrigeration
liquid
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    • 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
    • F25J3/0242—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 3 carbon atoms or more
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C7/00—Purification; Separation; Use of additives
    • C07C7/005—Processes comprising at least two steps in series
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C7/00—Purification; Separation; Use of additives
    • C07C7/11—Purification; Separation; Use of additives by absorption, i.e. purification or separation of gaseous hydrocarbons with the aid of liquids
    • 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
    • F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
    • F25B9/00—Compression machines, plants or systems, in which the refrigerant is air or other gas of low boiling point
    • F25B9/002—Compression machines, plants or systems, in which the refrigerant is air or other gas of low boiling point characterised by the refrigerant
    • F25B9/004—Compression machines, plants or systems, in which the refrigerant is air or other gas of low boiling point characterised by the refrigerant the refrigerant being air
    • 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
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/50—Processes or apparatus using other separation and/or other processing means using absorption, i.e. with selective solvents or lean oil, heavier CnHm and including generally a regeneration step for the solvent or lean oil
    • 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
    • F25J2215/00—Processes characterised by the type or other details of the product stream
    • F25J2215/64—Propane or propylene
    • 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
    • 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
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/02—Internal refrigeration with liquid vaporising loop

Definitions

  • the present invention relates to an improved method for utilizing at low temperatures the refrigeration available in a high pressure liquid ethane stream.
  • this invention relates to cooling the said liquid ethane stream to a temperature below F., followed by expanding it into a large volume of a colder light gaseous stream to thereby obtain vaporization of the liquid stream and further cooling of the combined stream.
  • this invention relates to an improved light ends system for recovering propylene and ethylene from a C stream from steam cracking.
  • this system comprising a first demethanization by absorption followed by successive fractionations the liquid ethane stream from the ethylene-ethane splitter is cooled to a temperature below -20 F. and is flashed in the presence of the expanded cold 110 to 140" F. tail gas from the absorber demethanizer to provide additional low temperature refrigeration for the process.
  • the effective pressures are reduced in accordance with Daltons Law as follows: partial pressure of ethane total pressure mol fraction of ethane. It can be seen that for practical expansion, vaporization of liquid ethane to pressures of 50-150, preferably 50-100 p.s.i.g., the relative proportion of the light gases should be 1:1 to 25: 1, preferably 2:1 to 20:1, e.g. 6:1 mols of light gas per mol of liquid ethane. At these dilutions, ethane can be evaporated at 50-100 p.s.i.g. at temperatures of 100 F. to -l50 PI, thus making refrigeration available at these low temperatures equal to the latent heat of the ethane evaporated. Without the diluting gas, ethane would evaporate at only 68 F. to 38" F., corresponding to 50 and 100 p.s.i.g., seriously degenerating the available refrigeration to a less attractive level.
  • a particularly advantageous arrangement is to precool the liquid ethane to as low a temperature as possible by heat exchange prior to mixing with the cold light gas stream.
  • the ethane is to be flashed into a 100 to 150 F. gas stream, it is most advantageous to preoool the ethane as near as possible to the 100 F. to 150 F. range. This will make the maximum use of "ice Refrigeration Available at 120 F. or Lower Due to lb. Moles of Liquid Ethane Temperature of Ethane Before Flashing into F. Ta Gas
  • the amount of heat which has to be abstracted from the liquid ethane prior to flashing is equal to that gained by the refrigeration capacity below 120" F.
  • this precooling is at a much higher temperature level than the 120" F. refrigeration increase, so that a net gain is achieved resulting in appreciable power savings.
  • the principal and preferred use of this system is in the separation of valuable ethylene from a gas containing ethylene in combination with methane and hydrogen.
  • effluent gases from hydrocarbon steam cracking processes e.g. C streams can be more efficiently separated according to the present invention.
  • the present invention aids in the recovery of propylene and other light hydrocarbons from the hydrogen-methane tail gas without the need for expensive equipment such as turbo-expanders or ethylene refrigeration.
  • the temperature at the top of the demethanizer in such a process will ordinarily be of the order of 112 F.
  • Such low temperatures are required in order to avoid an excessive loss of C hydrocarbons in the efiluent gas and to attain these temperatures, ethane or ethylene refrigeration rather than only propylene refrigeration is required.
  • the temperature at the top of the demethanizer may be maintained at about 0 to 20 F., but at these temperatures large quantities of propylene are taken overhead.
  • the overhead stream must be processed in either of two ways: 1) the gas may be separately cooled with ethane or ethylene refrigeration to condense the propylene, or (2) the gas may be cooled by refrigeration provided by sending the overhead gas through turbo expansion engines and using merely recycled propylene refrigeration.
  • a feed stream of C and ligher components obtained for example from steam cracking is supplied at a temperature of 35 F. to F., e.g. 25 F. through line l to the middle part of the absorber 2 operated at 300 to 600 p.s.i.a., specifically 420 p.s.i.a.
  • This feed stream may contain, for example, 224 mols/hr. H 365 mole/hr. CH 428 mols/hr. ethylene, 104 mols/hr. ethane, 282 mols/hr. propylene, 21 mcls/hr.
  • a propylene lean oil stream supplied from a deethanizer as will be described is introduced at a temperature of to 35 F., e.g. F. through line 3 to the overhead stream from the absorber.
  • the amount of this lean oil stream may be for the above example, 650 lb. mols/ hr.
  • From the bottom of the tower the demethanized C stream is removed through line 4, a part of said stream being supplied through line 5, reboiler 6 and line 7 back to the tower and the remainder being passed through line 8 at a temperature of 60 to 90 F., e.g. 80 F. to deethanizer 9.
  • This deethanizer is operated at a pressure of 300 to 600 p.s.i.g., e.g. 370 p.s.i.g. From the bottom of the deethanizer a propylene stream (containing also the small amounts of propane present in the C cut) is passed through line 10, part of the stream being passed back to the column through line 11, reboiler 12 and line 13, and of the remainder, part being passed back to column 2 and the remainder being taken oil as product through line 14.
  • the liquid propylene passed back to absorption tower 2 is passed through line 15 to cooler 16 where its temperature is reduced to 0 to 20 F., e.g. 5 F. From the cooler the liquid propylene is passed through line 17 to join the vapors taken overhead from tower 2 through line 18.
  • the combined stream is passed through line 19 to condenser 20 where the temperatureis reduced to l5 to 35 F., e.g. 20 F.
  • the cooled stream is passed through line 21 to separator 22 and the separated liquid is recycled to the column through line 3.
  • the overhead gases from separator 22, are passed through line 23 to cooler 24, where the temperature of the gas is reduced to 80 to 120 F., e.g. 105 F.
  • cooler 24 From cooler 24 the gases are supplied through line 25 to Joule-Thompson expansion valve 26 where the pressure is reduced to 50 to 150 p.s.i.g., e.g. 100 p.s.i.g. Reduced pressure and liquid gas at a temperature of l00 to 150 F., eg. 130 F.
  • the C stream is passed through line 34 to condenser 35, a part of the stream being refluxed back to the column through line 36 and the remainder being passed through line 37 to ethylene separation column 38.
  • This column may operate in the range of 75 to 400 p.s.i.g. From this column the ethylene stream is passed overhead through line 39 to condenser 40, a suitable reflux stream being returned through line 4-1 and the remainder being passed to product through line 42.
  • a particularly attractive alternate is to use the liquid propylene from the .J oule-Thompson recovery drum 28, i.e. line 29, to cool the liquid ethane prior to flashing through valve 50.
  • the stream in line 29 is at F. and the ethane fed to valve 50 at 23 F.
  • the temperature of the liquid ethane fed to valve 50 can be lowered to l00 F. to 1l0 F.
  • this will make an additional 230,000 B.t.u./hr. of low temperature refrigeration available in the 100 F. to 130 F. temperature range.
  • An improved process for utilizing at low temperatures the refrigeration available in a high pressure liquid ethane stream which comprises flashing the liquid ethane stream at a temperature in the range of 0 to F. and from a pressure in the range of 75 to 400 p.s.i.g. to a pressure in the range of 50 to 150 p.s.i.g. in the presence of a cool lighter gaseous stream supplied at a temperature below 80 F. and utilizing the combined stream to effect refrigeration of another stream.
  • An improved demethanization process which comprises passing a C3- stream containing hydrogen and methane to an absorption tower operated at a pressure of 300 .to 600 p.s.i.g. supplying a liquid propylene lean oil to the top of said tower to absorb materials heavier than methane from said C stream, expanding the overhead stream from said tower to a pressure in the range of 50 to 150 p.s.i.g. to effect cooling of said stream, further cooling said expanded stream to a temperature below 80 F., and expanding a liquid ethane stream at a temperature of to 150 F. in the presence of the cooled expanded overhead vapor stream from said tower from a pressure in the range of 75 to 400 p.s.i.g. to a pressure in the range of 50 to 150 p.s.i.g. to effect vaporization of the liquid ethane stream and further cooling of the combined stream and utilizing the combined stream to effect refrigeration of another stream.
  • liquid propylene is separated by distillation from the liquid propylene oil containing absorbed materials heavier than methane, a part of the liquid propylene separated is passed back to the absorption tower as the propylene lean oil supplied to said tower, liquid ethane is separated by distillation from the overhead vapors from said distillation separation of liquid propylene, and at least a major part of the liquid ethane separated is passed to the liquid ethane expansion.

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  • Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Analytical Chemistry (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Water Supply & Treatment (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Separation By Low-Temperature Treatments (AREA)
US105144D 1961-04-24 1961-04-24 Low temperature refrigeration in ethylene plants Expired - Lifetime US3192732A (en)

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Cited By (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3262278A (en) * 1963-08-19 1966-07-26 Exxon Research Engineering Co Increased ethylene recovery by ethane addition
US3902329A (en) * 1970-10-28 1975-09-02 Univ California Distillation of methane and hydrogen from ethylene
DE3040777A1 (de) * 1980-10-29 1982-05-27 Linde Ag, 6200 Wiesbaden Verfahren zur gewinnung niedermolekularer olefine
US4401450A (en) * 1980-09-11 1983-08-30 Linde Aktiengesellschaft Economic recovery of ethylene and/or propylene from low concentration feeds
US4897098A (en) * 1986-10-16 1990-01-30 Enterprise Products Company Fractionation system for stabilizing natural gasoline
US5520724A (en) * 1992-05-27 1996-05-28 Linde Aktiengesellschaft Process for the recovery of low molecular weight C2+ hydrocarbons from a cracking gas
US20170248364A1 (en) * 2014-09-30 2017-08-31 Dow Global Technologies Llc Process for increasing ethylene and propylene yield from a propylene plant
US20170261257A1 (en) * 2016-03-14 2017-09-14 Kellogg Brown & Root Llc Heat pump on c2 splitter bottom to unload propylene refrigeration

Citations (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US1325667A (en) * 1919-12-23 Refrigerant and process of making the same
US2028432A (en) * 1934-03-19 1936-01-21 Alco Products Inc Combined rectification and refrigeration process
US2573341A (en) * 1946-12-19 1951-10-30 Lummus Co Production of ethylene
US2731810A (en) * 1949-01-04 1956-01-24 Qjivaiiov snoonilnod
US2777305A (en) * 1953-12-28 1957-01-15 Phillips Petroleum Co Separation and recovery of ethylene
US2804488A (en) * 1954-12-27 1957-08-27 Phillips Petroleum Co Separation and recovery of ethylene
US2813920A (en) * 1953-07-03 1957-11-19 Phillips Petroleum Co Production of ethylene
US2915881A (en) * 1953-12-07 1959-12-08 Koppers Co Inc Separation of gases

Family Cites Families (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2933901A (en) * 1955-12-19 1960-04-26 Phillips Petroleum Co Separation of fluid mixtures

Patent Citations (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US1325667A (en) * 1919-12-23 Refrigerant and process of making the same
US2028432A (en) * 1934-03-19 1936-01-21 Alco Products Inc Combined rectification and refrigeration process
US2573341A (en) * 1946-12-19 1951-10-30 Lummus Co Production of ethylene
US2731810A (en) * 1949-01-04 1956-01-24 Qjivaiiov snoonilnod
US2813920A (en) * 1953-07-03 1957-11-19 Phillips Petroleum Co Production of ethylene
US2915881A (en) * 1953-12-07 1959-12-08 Koppers Co Inc Separation of gases
US2777305A (en) * 1953-12-28 1957-01-15 Phillips Petroleum Co Separation and recovery of ethylene
US2804488A (en) * 1954-12-27 1957-08-27 Phillips Petroleum Co Separation and recovery of ethylene

Cited By (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3262278A (en) * 1963-08-19 1966-07-26 Exxon Research Engineering Co Increased ethylene recovery by ethane addition
US3902329A (en) * 1970-10-28 1975-09-02 Univ California Distillation of methane and hydrogen from ethylene
US4401450A (en) * 1980-09-11 1983-08-30 Linde Aktiengesellschaft Economic recovery of ethylene and/or propylene from low concentration feeds
DE3040777A1 (de) * 1980-10-29 1982-05-27 Linde Ag, 6200 Wiesbaden Verfahren zur gewinnung niedermolekularer olefine
US4897098A (en) * 1986-10-16 1990-01-30 Enterprise Products Company Fractionation system for stabilizing natural gasoline
US5520724A (en) * 1992-05-27 1996-05-28 Linde Aktiengesellschaft Process for the recovery of low molecular weight C2+ hydrocarbons from a cracking gas
US20170248364A1 (en) * 2014-09-30 2017-08-31 Dow Global Technologies Llc Process for increasing ethylene and propylene yield from a propylene plant
US10808999B2 (en) * 2014-09-30 2020-10-20 Dow Global Technologies Llc Process for increasing ethylene and propylene yield from a propylene plant
US20170261257A1 (en) * 2016-03-14 2017-09-14 Kellogg Brown & Root Llc Heat pump on c2 splitter bottom to unload propylene refrigeration

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Publication number Publication date
GB978578A (en) 1964-12-23
DE1201857B (de) 1965-09-30

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