US1958553A - Method of separating the constituents of gaseous mixtures - Google Patents

Method of separating the constituents of gaseous mixtures Download PDF

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Publication number
US1958553A
US1958553A US639748A US63974832A US1958553A US 1958553 A US1958553 A US 1958553A US 639748 A US639748 A US 639748A US 63974832 A US63974832 A US 63974832A US 1958553 A US1958553 A US 1958553A
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United States
Prior art keywords
liquid
constituents
rectification
pipe
ethylene
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Expired - Lifetime
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US639748A
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English (en)
Inventor
Claude C Van Nuys
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Airco Inc
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Air Reduction Co Inc
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Filing date
Publication date
Priority to NL38731D priority Critical patent/NL38731C/xx
Priority to DENDAT753693D priority patent/DE753693C/de
Application filed by Air Reduction Co Inc filed Critical Air Reduction Co Inc
Priority to US639748A priority patent/US1958553A/en
Priority to GB27226/33A priority patent/GB414918A/en
Priority to FR762028D priority patent/FR762028A/fr
Application granted granted Critical
Publication of US1958553A publication Critical patent/US1958553A/en
Anticipated expiration legal-status Critical
Expired - Lifetime legal-status Critical Current

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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
    • F25J3/0252—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of hydrogen
    • 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
    • C07C7/04—Purification; Separation; Use of additives by distillation
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/0204—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the feed stream
    • F25J3/0219—Refinery gas, cracking gas, coke oven gas, gaseous mixtures containing aliphatic unsaturated CnHm or gaseous mixtures of undefined nature
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
    • F25J3/0233—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of CnHm with 1 carbon atom or more
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
    • F25J3/0238—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of CnHm with 2 carbon atoms or more
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
    • F25J3/0242—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
    • F25J2200/80—Processes or apparatus using separation by rectification using integrated mass and heat exchange, i.e. non-adiabatic rectification in a reflux exchanger or dephlegmator
    • 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

Definitions

  • This invention relates to the separation and recovery of the constituents of gaseous mixtures, and particularly to the recovery of a constituent of intermediate boiling point in a condition of substantial purity by a continuous operation.
  • the invention may be utilized for the recovery of various constituents from complex gaseous mixtures, of which numerous examples are found in the art. It is especially useful in the recovery of products such as ethylene, which are produced admixed with various other hydrocarbon gases and hydrogen in the petroleum industry. By the application of the invention, ethylene can be recovered in a substantially pure condition and in an economical manner from various gaseous mixtures containing it.
  • Another object of the invention is to provide an eflicient method of producing the refrigerative effect necessary for the accomplishment of the desired separation.
  • the invention depends upon the treatment of the gaseous mixture by liquefaction and rectification, so that constituents having different boiling points are segregated.
  • the initial gaseous complex mixture after compressing to a suitable pressure and primary cooling by heat exchange with products of the method, is subjected to selective liquefaction with backward return of the liquefied constituents.
  • the initial mixture is separated into a liquid portion containing a substantial fraction of the constituents of intermediate boiling point and the major portion of the constituents whose boiling points are higher, and a gaseous fraction containing the balance of the constituents of the initial gaseous mixture.
  • the gaseous mixture resulting from the first step of the procedure is then subjected to further liquefaction with backward return of the liquid produced, thus effecting a further separation into liquid and gaseous fractions. These fractions are then further separated by rectification so as to produce an effluent consisting substantially of the constituents of lowest boiling point and a liquid containing substantially only constituents of intermediate and higher boiling points.
  • the liquid fraction from the rectification is then returned and subjected to rectification with the first fraction produced in the initial separation, the rectification being completed with liquid consisting substantially of the constituents of intermediate boiling point so as to produce an effluent consisting of that constituent in a substantially pure condition.
  • the residual liquid produced by the final rectification consists almost entirely of the constituents of higher boiling point.
  • the several fractions into which the gaseous mixture is thus separated are withdrawn continuously and are thus recovered and may be utilized for any desired purpose.
  • the major product is ethylene which has a boiling point intermediate between the boiling points of other constituents making up the initial gaseous mixture.
  • the remaining products recovered are usually hydrogen and V9.- rious hydrocarbon gases.
  • 5 and 6 indicate columns in which the selective liquefaction and rectification of the gaseous mix ure and the fractions thereof is accomplished.
  • the initial gaseous mixture comprising the several constituents is compressed in a suitable compresser (not shown) to the pressure which may be necessary,
  • the compressed gaseous mixture is introduced through a pipe '7 to an exchanger -8 wherein itis cooled by circulation about pipes 9, l0 and 11 through which the products oi the separation at a lower temperature are delivered.
  • the gaseous mixture thus cooled passes through a pipe 12 into a compartment 13 at the bottom of the column 5 and thence upwardly through pipes 14 which are surrounded by liquid produced in the rectification hereinafter described.
  • the gaseous mixture passing through the pipes 14 at a higher pressure than that of the surrounding liquid is subjected to partial liquefaction and the liquid produced fiows backwardlythrough the pipes and accumulates in the chamber 13. It consists of a large portion of the constituent of intermediate boiling point, for example, ethylene, and the major portion of a constituent or constituents having a higher boiling point.
  • the unliquefied residue is delivered 15 and passes through a pipe 16 into a compartment 17 at the bottom of the second column 6.
  • Liquid accumulating in the compartment 17 is delivered by a pipe 21, passes upwardly through an exchanger 22, thence through a pipe 23 and' pressure reducing valves 24 and is delivered through a pipe 25 into the rectifying section of the column 6, in which it flows downwardly over trays 26 of the type usually employed in rectification columns and in contact with rising vapors.
  • the gaseous fraction escaping through the pipe 20 passes through an exchanger 27, pipe 28 and condenser 29, within the rectification column, being thus condensed to a liquid which escapes through a pipe .30 to an exchanger 31 where the liquid may be sub-cooled.
  • the liquid passes then through a pipe 32, pressure reducing valve 33 and pipe 34 into the upper end of the rectification column and flows downwardly over the trays 26 therein in contact with rising vapors.
  • the efliuent escaping through the pipe 35 passes through the exchanger 31 where it serves to reduce the temperature 01' the liquid flowing in the opposite direction therethrough, thence through a pipe 3'! to the exchanger 27, thence through a pipe 38 to the exchanger 22, and finally through a pipe 39 which delivers it to the pipe 9 in the exchanger 8. It is withdrawn after giving up its cold in the exchanger system through a pipe 40 as one of the products or the operation.
  • Liquid accumulating in the compartment 13 at the bottom of the column 5 is withdrawn through a pipe 41 and, after passing through a pressure reducing valve 42, is delivered to a separator 43.
  • vapors may escape from the liquid, and such vapors may be delivered through a pipe '44 to an intermediate point in the column 6.
  • Uncondensed vapors leaving a condenser 48 to a head through pipe 47 and valve 46 pass through pipe to the separator 43, whence they pass out through pipe 44 to column 6 with the vapors previously mentioned.
  • the liquid from the separator 43 is delivered through a pipe 50 and valve 50a at an intermediate point in the rectification section of the column 5 wherein it flows downwardly over the usual trays 51 in contact with vapors rising through the column.
  • Liquid from the lower part of the column 6 is delivered through a pipe 52 and valve 53 to the rectification section of the column 5, or, as an alternative, vapors may be withdrawn also from a lower level of the column 6, above the liquid therein. through a pipe 54 and delivered through a valve 55 to the rectification section of the column 5.
  • This product may be delivered through a pipe 57 to thepipe 11 in the exchanger 8 and may be withdrawn through a pipe 58 and delivered to a suitable receptacle for storage, or it may be otherwise employed.
  • a portion of the eilluent is diverted from the pipe 56 through a pipe 59, and, after passing through an exchanger 60, it is delivered by a pipe 61 to compresser 62 where the pressure is materially increased.
  • the compressed eflluent which may at this point be partially liquid is returned through a pipe 63 and the exchanger to a pipe 64 which delivers it to the condenser 48.
  • the unliquefied portion of this eflluent is partially liquefied in condenser 48 and is delivered through pipe 49 and pressure reducing valve 49d to the top of the rectii'ying section of the column 5.
  • the recti tying section is supplied continuously with a quantity oi liquid consisting substantially of the constituent of intermediate boiling point, for example, ethylene.
  • This liquid washes from the rising vapors all constituents of higher boiling point, which are thus returned to the liquid flowing downwardly through the column and accumulating therein about the pipes 14.
  • the latter liquid is partially vaporized in cooling the initial gaseous mixture in the pipes 14, and the balance, it any, is withdrawn through a pipe 65 and valve 65a which delivers it to the pipe 10 in the exchanger 8.
  • the lower end product of the rectification column 5, over and above that portion withdrawn in the liquid state through pipe 65, is
  • the method of separating and recovering ethylene from complex gaseous mixtures which comprises initially separating, by selective liquefaction and backward return of the liquid, a fraction containing ethylene and other constituents of higher boiling point, subjecting the balance of the gaseous mixture to further separation by selective liquefaction with backward return of the liquid followed by rectification so as to separate it into two portions, the first containing only constituents of boiling points lower than that of ethylene, and the second or lower product containing only ethylene and constituents of higher boiling points, withdrawing the vapors of lower boiling point as the upper eilluent from this rectification, subjecting the second or lower product of the rectification to further and combined rectification with the liquid product of the initial separation, and withdrawing as the upper effluent of the combined rectification a vapor consisting substantially of ethylene.
  • the method of separating and recovering ethylene from complex gaseous mixtures which comprises initially separating, by selective liquefaction and backward return of the liquid, a fraction containing ethylene and other constituents of higher boiling point, subjecting the balance of the gaseous mixture to further separation by selective liquefaction with backward return of the liquid followed by rectification of the liquid to separate constituents having boiling points lower than that of ethylene, withdrawing the vapors of lower boiling point, subjecting the remaining products of the rectification to further and combined rectification with the liquid product of the initial separation, withdrawing as the effluent of the combined rectification a vapor consisting substantially of ethylene, and liquefying and returning a portion of the effluent from the combined rectification to facilitate the separation of ethylene in a condition of substantial purity.
  • the method of separating and recovering ethylene from complex gaseous mixtures which comprises initially separating, by selective liquefaction and backward return of the liquid, a fraction containing ethylene and other constituents of higher boiling point, subjecting the balance of the gaseous mixture to further separation by selective liquefaction with backward return of the liquid followed by rectification of the liquid to separate constituents having boiling points lower than that of ethylene, withdrawing the vapors of lower boiling point, subjecting the remaining products of the rectification to further and combined rectification with the liquid product of the initial separation, withdrawing as the efliuent of the combined rectification a vapor consisting substantially of ethylene, and recompressing and liquefying and returning a portion of the effluent from the combined rectification to facilitate the separation of ethylene in a condition of substantial purity.
  • the steps of initially separating the gaseous mixture into liquid and gaseous fractions by selective liquefaction and backward return of the liquid conducting the liquid at reduced pressure to a compartment, separating vapors from the liquid in the compartment, subjecting the liquid to rectification, liquefying at least a portion of the gaseous fraction from the initial separation and utilizing the vapors from the compartment in a separate rectification of liquefied constituents of the gaseous fraction from the initial separation.
  • the method of separating and. recovering ethylene from complex gaseous mixtures which comprises initially separating, by selective liquefaction and backward return of the liquid, at fraction containing ethylene and other constituents of higher boiling point, subjecting the balance of the gaseous mixture to further separation by selective liquefaction and backward return of the liquid, followed by rectification of the liquid to separate constituents having boiling points lower than that of ethylene, withdrawing the vapors of the lower boiling point, subjecting the liquid product of the initial separation to reduced pressure and separating vapors therefrom, utilizing the vapors thus separated in a rectification of liquid resulting from the liquefaction of the gaseous fraction of the initial separation, and subjecting the liquid remaining after the separation of vapors therefrom to rectification.
  • the method of separating and recovering ethylene from complex gaseous mixtures which comprises initially separating, by selective liquefaction and backward return of the liquid, a frac-' tion containing ethylene and other constituents of higher boiling point, subjecting the balance of the gaseous mixture to further separation by selective liquefaction and backward return of the liquid, k

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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)
  • Separation By Low-Temperature Treatments (AREA)
US639748A 1932-10-27 1932-10-27 Method of separating the constituents of gaseous mixtures Expired - Lifetime US1958553A (en)

Priority Applications (5)

Application Number Priority Date Filing Date Title
NL38731D NL38731C (fr) 1932-10-27
DENDAT753693D DE753693C (fr) 1932-10-27
US639748A US1958553A (en) 1932-10-27 1932-10-27 Method of separating the constituents of gaseous mixtures
GB27226/33A GB414918A (en) 1932-10-27 1933-10-03 Method of separating the constituents of gaseous mixtures
FR762028D FR762028A (fr) 1932-10-27 1933-10-06 Procédé de séparation des constituants de mélanges gazeux

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
US639748A US1958553A (en) 1932-10-27 1932-10-27 Method of separating the constituents of gaseous mixtures

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US1958553A true US1958553A (en) 1934-05-15

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US639748A Expired - Lifetime US1958553A (en) 1932-10-27 1932-10-27 Method of separating the constituents of gaseous mixtures

Country Status (5)

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US (1) US1958553A (fr)
DE (1) DE753693C (fr)
FR (1) FR762028A (fr)
GB (1) GB414918A (fr)
NL (1) NL38731C (fr)

Cited By (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2527623A (en) * 1944-10-23 1950-10-31 Arthur J Fausek Method of separating the constituents of gaseous mixtures
US2559132A (en) * 1948-02-12 1951-07-03 British Oxygen Co Ltd Fractional separation of air
US2582068A (en) * 1948-12-30 1952-01-08 Elliott Co Method and apparatus for separating gases
US2905732A (en) * 1955-04-04 1959-09-22 Phillips Petroleum Co Purification of butadiene by removing it from oxygen with an absorbent oil
US3098107A (en) * 1959-05-22 1963-07-16 Linde Eismasch Ag Method for producing ethylene
US3255171A (en) * 1961-08-26 1966-06-07 Basf Ag Purification of recycle ethylene in the high pressure polymerization of ethylene
US3444697A (en) * 1967-06-30 1969-05-20 Texaco Inc Distributed heat exchange fractionating column

Families Citing this family (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE2608404A1 (de) * 1976-03-01 1977-09-08 Linde Ag Verfahren und vorrichtung zur trennung von stoffgemischen durch rektifikation

Cited By (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2527623A (en) * 1944-10-23 1950-10-31 Arthur J Fausek Method of separating the constituents of gaseous mixtures
US2559132A (en) * 1948-02-12 1951-07-03 British Oxygen Co Ltd Fractional separation of air
US2582068A (en) * 1948-12-30 1952-01-08 Elliott Co Method and apparatus for separating gases
US2905732A (en) * 1955-04-04 1959-09-22 Phillips Petroleum Co Purification of butadiene by removing it from oxygen with an absorbent oil
US3098107A (en) * 1959-05-22 1963-07-16 Linde Eismasch Ag Method for producing ethylene
US3255171A (en) * 1961-08-26 1966-06-07 Basf Ag Purification of recycle ethylene in the high pressure polymerization of ethylene
US3444697A (en) * 1967-06-30 1969-05-20 Texaco Inc Distributed heat exchange fractionating column

Also Published As

Publication number Publication date
NL38731C (fr)
FR762028A (fr) 1934-04-03
GB414918A (en) 1934-08-16
DE753693C (fr)

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