US3635038A - Joint separation of acetylene and ethylene from cracked gases - Google Patents

Joint separation of acetylene and ethylene from cracked gases Download PDF

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US3635038A
US3635038A US825323A US3635038DA US3635038A US 3635038 A US3635038 A US 3635038A US 825323 A US825323 A US 825323A US 3635038D A US3635038D A US 3635038DA US 3635038 A US3635038 A US 3635038A
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acetylene
gas
ethylene
hydrocarbons
mixture
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Otto Nagel
Rolf Platz
Kurt Taglieber
Kurt Weinfurter
Dieter Wolf
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BASF SE
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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
    • F25J3/0271—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 H2/CO mixtures, i.e. of synthesis gas
    • 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
    • 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
    • F25J3/0238—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
    • F25J3/0242—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
    • 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
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/74—Refluxing the column with at least a part of the partially condensed overhead 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
    • 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
    • F25J2205/50—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
    • 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
    • F25J2270/04—Internal refrigeration with work-producing gas expansion loop
    • 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
    • F25J2270/12—External refrigeration with liquid vaporising loop

Definitions

  • ABSTRACT A gas mixture (obtained by thermal cracking of hydrocarbons followed by quenching of the cracked gas and freed from carbon dioxide and water) is separated into a gas mixture containing hydrogen, carbon monoxide and methane and another gas mixture containing ethylene, acetylene and higher hydrocarbons by (a) cooling the gas mixture which is at superatmospheric pressure in at least one condensation stage to a temperature which is above the solidification temperature of acetylene mixed with the other condensed constituents, (b) separating the condensate thus obtained and subdividing it in a rectifying column into a first mixture containing C hydrocarbons and a second mixture containing C and higher hydrocarbons, and (c) freeing the residual gas remaining from (a) from residual acetylene and ethylene in a scrubber by treatment with some of the mixture consisting of C and higher hydrocarbons from (b).
  • This invention relates to a process for separating gas mixtures which contain hydrogen, carbon monoxide, methane, ethylene, acetylene and higher hydrocarbons, said mixtures having been obtained by thermal cracking of hydrocarbons followed by quenching of the cracked gas.
  • gas mixtures containing hydrogen, carbon monoxide, methane, ethylene, acetylene and higher hydrocarbons and devoid of carbon dioxide and water which have been obtained by thermal cracking of hydrocarbons followed by quenching of the cracked gas can be separated into (i) a gas mixture containing hydrogen, carbon monoxide and methane which is practically devoid of other hydrocarbons and (ii) a mixture containing ethylene, acetylene and higher hydrocarbons which may be separated in further stages into the individual components, by a process wherein a.
  • the initial gas mixture which is under superatmospheric pressure preferably from 5 to 35 atmospheres gauge, is cooled in one or more condensation stages to a temperature which is above the solidification temperature of acetylene in admixture with other condensed constituents, preferably to -82 to -l C.;
  • thermal cracking includes the conventional cracking methods in which a gas mixture containing ethylene and acetylene is obtained. It includes in particular the cracking of crude oil or hydrocarbon fractions in a flame burning beneath the surface of the liquid (submerged flame). This method is described in detail in Chem. lng.technik 26, No. 5, page 253, and British Pat. No. 834,419, to which reference is made.
  • Preliminary separation of carbon dioxide and hydrogen sulfide may be carried out in known manner by scrubbing, for example with an aqueous solution of an alkali metal salt of an amino acid.
  • This scrubbing in which most of the carbon dioxide together with most of the hydrogen sulfide is separated, may be followed by afterpurification from carbon dioxide.
  • This afterpurification is advantageously carried out by scrubbing with a dilute solution of an alkali metal hydroxide.
  • the cracked gas freed from carbon dioxide and hydrogen sulfide is dried before it is subjected to condensation. This drying may be carried out for example by scrubbing or saturation with methanol.
  • the cracked gas freed from carbon dioxide and hydrogen sulfide and treated in this way is cooled in one or more condensation stages to a temperature above the point at which acetylene separates as a solid, for example to from about to l20 C., the condensate containing C and higher hydrocarbons is separated and the residual gas which contains acetylene and ethylene is freed from acetylene and ethylene in a scrubber at superatmospheric pressure, advantageously at the pressure at which the cracked gas is formed, by scrubbing with the mixture of C and higher hydrocarbons obtained as described below.
  • FIG. 1 in which a denotes cracked gas, b cooler, c residual gas, d scrubber, e condensate, f laden scrubbing liquid, g distillation unit, and h scrubbing liquid
  • the gas mixture leaving the scrubbing column is advantageously supplied for the production of cold to an expansion machine for performing external work, in which it is expanded to practically atmospheric pressure, thereby cooled and then after cooling the scrubbing liquid for the scrubbing column is used for cooling the incoming cracked gas countercurrently.
  • the condensate and the bottoms product of the scrubber are released from pressure and also passed countercurrent to the incoming cracked gas through the condensation stages for cooling and condensation of the incoming cracked gas.
  • the mixture of vapor and liquid formed from the condensate by partial evaporation is'compressed to a pressure of from 10 to 20 atmospheres and separated in a rectifying column at pressures of for example 5 to 40 atmospheres gauge, preferably from 10 to 20 atmospheres gauge, into an overhead product containing C hydrocarbons and constituents of lower boiling point, and a bottoms product containing C hydrocarbons and constituents of higher boiling point, and according to one embodiment of the invention (see FIG. 2) liquid ethylene obtained in the subsequent separation of the overhead product into acetylene and ethylene is supplied as a reflux.
  • the overhead product is subjected for example to scrubbing with acetone.
  • Some of the mixture containing C hydrocarbons and constituents having a higher boiling point is withdrawn and serves as scrubbing liquid for the above-mentioned scrubbing of the residual gas.
  • the mixture of ethylene andacetylene obtained is not separated into its constituents but used direct as a mixture for further reactions.
  • the condensate consisting of C to C hydrocarbons after partial reevaporation, is separated in a rectifying column at a pressure of from 1.5 to 4 atmospheres absolute into a mixture of ethylene and acetylene as overhead product and a bottoms product containing C to C hydrocarbons.
  • the scrubbing liquid must not contain any carbon disulfide which has not been removed from the cracked gas by the hydrogen sulfide scrubbing.
  • the scrubbing liquid consisting substantially of C and higher hydrocarbons is advantageously not taken from the bottoms of the rectifying column but from a lateral stream withdrawn between the bottom and point of supply of the incoming mixture. In this way the sulfur compounds having a higher boiling point than the said hydrocarbons (essentially carbon disulfide) are removed with the bottoms product.
  • the scrubbing liquid withdrawn as a lateral stream is passed through the heat exchanger of the condensation stages and cooled to a temperature of from about 80 to l20 C. and then supplied to the scrubbing column.
  • EXAMPLE l A plant as shown diagrammatically in FIG. 2 is used. 10,000 m. (STP)/hour of cracked gas (obtained by an oxygen flame burning beneath the surface of a pool of oil) which has been scrubbed free from carbon dioxide and hydrogen sulfide and has been dried is introduced at a pressure of 8.5 atmospheres absolute and a temperature of +20 C. through line 1 into a heat exchanger 2.
  • the cracked gas has the following composition:
  • the cracked gas is cooled to C. and the condensate obtained is separated in a separator 3.
  • the residual gas which remains is passed through line 4 through a heat exchanger 5 in which it is cooled to 1 10 C. and freed from condensate in a 20 separator 6.
  • the residual gas has the following composition (in percent by volume):
  • inert gas 11,, CO, CH 95.76 ethylene 2.78
  • acetylene 1 46 1t passes through line 7 into a scrubber 8 where it is substantially freed from acetylene and ethylene by countercurrent treatment with a mixture consisting of 55 percent of C hydrocarbons, 39.5 percent of C hydrocarbons and 5.5 percent of C hydrocarbons introduced through line 9.
  • Gas and liquid are separated in separator 17, the pressure of the liquid is raised by a pump 18 and supplied through an ammonia-cooled heat exchanger 19 at 20 C. to a rectifying column 20.
  • the gas leaving separator 17 through line 21 is compressed by compressor 22 to 18 atmospheres absolute, cooled to 25 C. with ammonia in heat exchanger 23 and also supplied to the column 20.
  • the hydrocarbon mixture is separated into higher hydrocarbons and into a bottoms product containing sulfur compounds such as carbon disulfide.
  • liquid ethylene is supplied through line 24 and also gaseous ethylene partly through line 25 from outside the plant into the column 20.
  • the amount of 3,500 kg./hour of solvent required for the scrubber 8 is 5 withdrawn through line 26 from a tray lying between the bottoms and the point of supply of the C -C hydrocarbon mixture, precooled with water in heat exchanger 27, then after expansion to 8.5 atmospheres absolute passed by line 9 through heat exchangers 2 and 5 and thus cooled to -1 10 C., and passed into scrubber 8.
  • the mixture consisting of C hydrocarbons and higher hydrocarbons and a part of the sulfur compounds and which has been condensed out and separated from the cracked gas entering the plant is withdrawn from the plant from the bottom of the rectifying column 20 through line 28.
  • the reflux necessary for rectification is produced with a condenser 29 cooled with ammonia.
  • the mixture of C hydrocarbons (consisting substantially of acetylene and ethylene and containing only a few p.p.m. of higher hydrocarbons) leaving the condenser through line 30 is withdrawn from the plant, supplied to a scrubber and separated into the individual components.
  • EXAMPLE 2 For the production of a mixture of acetylene and ethylene according to P16. 3, 10,000 m. (STP) per hour of dried cracked gas (from which carbon dioxide and hydrogen sulfide have already been removed) is introduced through line 1 at a pressure of 8.5 atmospheres absolute and a temperature of +10 C. into a heat exchanger 2.
  • the cracked gas has the composition given in example 1.
  • After cooling to 20 C. in heat exchanger 2, the condensate formed is separated in a separator 3.
  • the gas is cooled to -1 10 C. in a heat exchanger 5 and freed from condensate in a separator 6.
  • the remaining gas has the composition given in example 1.
  • Residual acetylene and ethylene is scrubbed out in scrubber 8 with a C C fraction.
  • Connection of the scrubber and expansion turbine 11 is identical with the arrangement described in example 1.
  • the condensate collected in line 15 is heated to 0 C. in heat exchangers 5 and 2 to utilize sensible and evaporation heat.
  • After cooling with the overhead product from column 20 in heat exchanger 31, the supply to the column 20 is separated in a separator 17 into a liquid phase and a gas phase which are supplied to different trays according to their composition.
  • a process for separating a gas mixture containing hydrogen, carbon monoxide, methane, ethylene, acetylene and higher hydrocarbons which is devoid of carbon dioxide and water and which has been obtained by thermal cracking of a hydrocarbon followed by quenching of the cracked gas which process comprises a. cooling the initial gas mixture which is under superatmospheric pressure in at least one condensation stage to a temperature which is sufficient to condense the C and higher hydrocarbons but which is above the solidification temperature of acetylene in admixture with other condensed constituents;
  • step (c) freeing the residual uncond'ensed gas mixture of step (a) which still contains small amounts of acetylene and ethylene from said acetylene and ethylene in a scrubber by treatment with some of said second mixture containing C and higher hydrocarbons obtained as a liquid condensate from step (b), thereby obtaining a separate third gas mixture which contains hydrogen, carbon monoxide and methane and which is practically devoid of other hydrocarbons.
  • cooling under (a) is to from 82 to l20 C.

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  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Analytical Chemistry (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Water Supply & Treatment (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
US825323A 1968-05-16 1969-05-16 Joint separation of acetylene and ethylene from cracked gases Expired - Lifetime US3635038A (en)

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
DE1768460A DE1768460C2 (de) 1968-05-16 1968-05-16 Verfahren zur Gewinnung von Acetylen, Äthylen und höhere Kohlenwasserstoffe enthaltenden Gemischen aus Spaltgasen

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US (1) US3635038A (enrdf_load_stackoverflow)
AT (1) AT284070B (enrdf_load_stackoverflow)
BE (1) BE733158A (enrdf_load_stackoverflow)
CH (1) CH525697A (enrdf_load_stackoverflow)
DE (1) DE1768460C2 (enrdf_load_stackoverflow)
ES (1) ES367286A1 (enrdf_load_stackoverflow)
FR (1) FR2008664A7 (enrdf_load_stackoverflow)
GB (1) GB1257372A (enrdf_load_stackoverflow)
NL (1) NL6907467A (enrdf_load_stackoverflow)
SE (1) SE339070B (enrdf_load_stackoverflow)

Cited By (11)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4121917A (en) * 1975-09-09 1978-10-24 Union Carbide Corporation Ethylene production with utilization of LNG refrigeration
US4336045A (en) * 1981-06-29 1982-06-22 Union Carbide Corporation Acetylene removal in ethylene and hydrogen separation and recovery process
US4701190A (en) * 1985-11-07 1987-10-20 Linde Aktiengesellschaft Process for recovering methylacetylene and/or propadiene
US4714487A (en) * 1986-05-23 1987-12-22 Air Products And Chemicals, Inc. Process for recovery and purification of C3 -C4+ hydrocarbons using segregated phase separation and dephlegmation
US5035732A (en) * 1990-01-04 1991-07-30 Stone & Webster Engineering Corporation Cryogenic separation of gaseous mixtures
US5289676A (en) * 1991-10-23 1994-03-01 Bechtel Group, Inc. Efficient low temperature solvent removal of acid gases
US5300469A (en) * 1992-12-08 1994-04-05 Engelhard Corporation Composition for passivating vanadium in catalytic cracking and preparation thereof
US5421167A (en) * 1994-04-01 1995-06-06 The M. W. Kellogg Company Enhanced olefin recovery method
US5444176A (en) * 1992-10-28 1995-08-22 Exxon Chemical Patents Inc. Process for recovering olefins from cat-cracked gas without accumulating undesirable oxides of nitrogen
US5804689A (en) * 1995-01-30 1998-09-08 Linde Aktiengesellschaft Process for recovering acetylene from hydrocarbons by thermal cracking
US20070151276A1 (en) * 2006-01-04 2007-07-05 Flatplate, Inc. Gas-drying system

Families Citing this family (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CA1107190A (en) * 1979-12-06 1981-08-18 Donald D. Livingstone Hydrocarbon recovery
AU572890B2 (en) * 1983-09-20 1988-05-19 Costain Petrocarbon Ltd. Separation of hydrocarbon mixtures
GB2146751B (en) * 1983-09-20 1987-04-23 Petrocarbon Dev Ltd Separation of hydrocarbon mixtures
GB2224036B (en) * 1988-10-21 1992-06-24 Costain Eng Ltd Separation of gas & oil mixtures

Citations (10)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US1938991A (en) * 1928-08-22 1933-12-12 Robert G Wulff Method of separating acetylene from gaseous mixtures
US2134702A (en) * 1936-09-29 1938-11-01 Refinery Engineers Inc Separation of hydrocarbons
US2236966A (en) * 1938-06-10 1941-04-01 Du Pont Separation of acetylene from gas mixtures
US2236965A (en) * 1938-06-10 1941-04-01 Du Pont Chemical process and apparatus
US2270852A (en) * 1939-03-24 1942-01-27 British Oxygen Co Ltd Separating of gas mixtures
US2321666A (en) * 1940-02-08 1943-06-15 Carbide & Carbon Chem Corp Process for gas separation
US2775103A (en) * 1954-12-23 1956-12-25 Phillips Petroleum Co Hydrocarbon separation
CA573349A (en) * 1959-03-31 Wolfram Arthur Process for the separation of higher acetylene hydrocarbons
US3023842A (en) * 1958-08-05 1962-03-06 Kellogg M W Co Acetylene purification
US3062015A (en) * 1957-03-08 1962-11-06 Air Prod & Chem Separation of gaseous mixtures

Family Cites Families (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR835832A (fr) * 1937-04-03 1939-01-04 Ig Farbenindustrie Ag Procédé pour l'obtention d'oléfines en partant de mélanges gazeux en contenant
DE1568160A1 (de) * 1966-08-12 1970-01-02 Basf Ag Verfahren zur gemeinsamen Abtrennung von Acetylen und AEthylen aus Spaltgasen

Patent Citations (10)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CA573349A (en) * 1959-03-31 Wolfram Arthur Process for the separation of higher acetylene hydrocarbons
US1938991A (en) * 1928-08-22 1933-12-12 Robert G Wulff Method of separating acetylene from gaseous mixtures
US2134702A (en) * 1936-09-29 1938-11-01 Refinery Engineers Inc Separation of hydrocarbons
US2236966A (en) * 1938-06-10 1941-04-01 Du Pont Separation of acetylene from gas mixtures
US2236965A (en) * 1938-06-10 1941-04-01 Du Pont Chemical process and apparatus
US2270852A (en) * 1939-03-24 1942-01-27 British Oxygen Co Ltd Separating of gas mixtures
US2321666A (en) * 1940-02-08 1943-06-15 Carbide & Carbon Chem Corp Process for gas separation
US2775103A (en) * 1954-12-23 1956-12-25 Phillips Petroleum Co Hydrocarbon separation
US3062015A (en) * 1957-03-08 1962-11-06 Air Prod & Chem Separation of gaseous mixtures
US3023842A (en) * 1958-08-05 1962-03-06 Kellogg M W Co Acetylene purification

Cited By (14)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4121917A (en) * 1975-09-09 1978-10-24 Union Carbide Corporation Ethylene production with utilization of LNG refrigeration
US4336045A (en) * 1981-06-29 1982-06-22 Union Carbide Corporation Acetylene removal in ethylene and hydrogen separation and recovery process
US4701190A (en) * 1985-11-07 1987-10-20 Linde Aktiengesellschaft Process for recovering methylacetylene and/or propadiene
US4714487A (en) * 1986-05-23 1987-12-22 Air Products And Chemicals, Inc. Process for recovery and purification of C3 -C4+ hydrocarbons using segregated phase separation and dephlegmation
US5035732A (en) * 1990-01-04 1991-07-30 Stone & Webster Engineering Corporation Cryogenic separation of gaseous mixtures
US5289676A (en) * 1991-10-23 1994-03-01 Bechtel Group, Inc. Efficient low temperature solvent removal of acid gases
US5444176A (en) * 1992-10-28 1995-08-22 Exxon Chemical Patents Inc. Process for recovering olefins from cat-cracked gas without accumulating undesirable oxides of nitrogen
AU704763B2 (en) * 1992-10-28 1999-05-06 Exxon Chemical Patents Inc. Process for recovering olefins from cat-cracked gas without accumulating undesirable oxides of nitrogen
US5384041A (en) * 1992-12-08 1995-01-24 Engelhard Corporation Composition for passivating vanadium in catalytic cracking and preparation thereof
US5300469A (en) * 1992-12-08 1994-04-05 Engelhard Corporation Composition for passivating vanadium in catalytic cracking and preparation thereof
US5421167A (en) * 1994-04-01 1995-06-06 The M. W. Kellogg Company Enhanced olefin recovery method
US5804689A (en) * 1995-01-30 1998-09-08 Linde Aktiengesellschaft Process for recovering acetylene from hydrocarbons by thermal cracking
US20070151276A1 (en) * 2006-01-04 2007-07-05 Flatplate, Inc. Gas-drying system
US7343755B2 (en) 2006-01-04 2008-03-18 Flatplate, Inc. Gas-drying system

Also Published As

Publication number Publication date
SE339070B (enrdf_load_stackoverflow) 1971-09-27
GB1257372A (enrdf_load_stackoverflow) 1971-12-15
ES367286A1 (es) 1971-04-01
CH525697A (de) 1972-07-31
DE1768460B1 (de) 1972-05-31
AT284070B (de) 1970-08-25
FR2008664A7 (enrdf_load_stackoverflow) 1970-01-23
DE1768460C2 (de) 1973-01-04
BE733158A (enrdf_load_stackoverflow) 1969-11-13
NL6907467A (enrdf_load_stackoverflow) 1969-11-18

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