US20110041550A1 - Process and apparatus for the separation of light-boiling components from hydrocarbon mixtures - Google Patents

Process and apparatus for the separation of light-boiling components from hydrocarbon mixtures Download PDF

Info

Publication number
US20110041550A1
US20110041550A1 US12/735,255 US73525508A US2011041550A1 US 20110041550 A1 US20110041550 A1 US 20110041550A1 US 73525508 A US73525508 A US 73525508A US 2011041550 A1 US2011041550 A1 US 2011041550A1
Authority
US
United States
Prior art keywords
condensation
temperature level
boiling fraction
stages
process according
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Abandoned
Application number
US12/735,255
Other languages
English (en)
Inventor
Johannes Menzel
Sascha Wenzel
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
ThyssenKrupp Industrial Solutions AG
Original Assignee
Uhde GmbH
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Uhde GmbH filed Critical Uhde GmbH
Assigned to UHDE GMBH reassignment UHDE GMBH ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: WENZEL, SASCHA, MENZEL, JOHANNES
Publication of US20110041550A1 publication Critical patent/US20110041550A1/en
Abandoned legal-status Critical Current

Links

Images

Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
    • 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
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C7/00—Purification; Separation; Use of additives
    • C07C7/09—Purification; Separation; Use of additives by fractional condensation
    • 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
    • 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
    • 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
    • F25J2200/02—Processes or apparatus using separation by rectification in a single pressure main column system
    • 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
    • F25J2200/50—Processes or apparatus using separation by rectification using multiple (re-)boiler-condensers at different heights of the column
    • 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
    • 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
    • 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
    • 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
    • F25J2270/60—Closed external refrigeration cycle with single component refrigerant [SCR], e.g. C1-, C2- or C3-hydrocarbons
    • 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
    • F25J2270/90—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration
    • 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
    • F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
    • F25J2290/40—Vertical layout or arrangement of cold equipments within in the cold box, e.g. columns, condensers, heat exchangers etc.

Definitions

  • the invention relates to a process and an apparatus for the separation of light-boiling components from a hydrocarbon stream, particularly for the separation of a C 2 fraction from a C 3 + fraction to be obtained as target product, e.g. in the dehydrogenation of light hydrocarbons, but also suitable for other separation tasks within the range of C 1 to C 4 .
  • distillation column is referred to and operated as a de-ethanizer because all substances of boiling points less or equal to that of ethane are separated overhead by this de-ethanizer.
  • the feed mixture Before entering the coldbox, the feed mixture is cooled down to approx. ⁇ 25° C.
  • the condensate gained is passed directly into the de-ethanizer. Vapours that have not condensed are further cooled to approx. ⁇ 90° C. in the coldbox, the product-enriched condensate thus obtained also being directed to the de-ethanizer after heat exchange.
  • the coldbox therefore performs a one-step rough separation.
  • the remaining vapour phase basically comprising uncondensable components, e.g. hydrogen, is depressurised after heat exchange in the flow entering the coldbox.
  • the light-boiling substances cool down to approx. ⁇ 110° C. due to the Joule-Thompson effect. This temperature level is used to partially condense the stream entering the coldbox.
  • the uncondensed light-boiling substances are basically free from C 3 + components.
  • Evaporating propane or propene can be used at ⁇ 30° C. as a cooling agent for cooling the feed mixture before it enters the coldbox, for operating the coldbox and for cooling the de-ethanizer.
  • the generation of cold for such a process is extremely expensive.
  • the aim of the invention is, therefore, to provide a process and an apparatus by which the consumption of cold can be reduced to a significant degree.
  • the aim of the invention is achieved according to the main claim by a process for the separation of a feed mixture
  • the distillation apparatus comprises three to five successive condensation stages, each of a different temperature level.
  • the condensation stage of the lowest temperature level is operated at a temperature between ⁇ 120° C. and ⁇ 70° C. and a pressure of at least 2 MPa absolute, preferably at least 3 MPa.
  • the mixture which leaves the distillation apparatus as lower-boiling fraction is depressurised, the mixture thereby cooling down further under exploitation of the Joule-Thompson-effect, and thus being used to cool the condensation stage with the lowest temperature level.
  • the depressurisation is performed by an expansion turbine.
  • the process is used for feed mixtures containing less than 2 mol-% each of carbon dioxide and water or water vapour.
  • the feed mixture used is a reaction mixture from the catalytic dehydrogenation of hydrocarbons.
  • the segment of the distillation apparatus through which that part of the feed mixture that has condensed in the condensation stage of the highest temperature level is passed to the outlet means for the higher-boiling fraction, is provided as a stripping section of the distillation apparatus.
  • feed mixtures of a relatively small content of components of low boiling point are preferably fed at a point below the condensation stage of the highest temperature level and feed mixtures of a relatively high content of components of low boiling point are preferably fed at a point above the condensation stage of the highest temperature level.
  • condensation stages are provided in the form of condensers.
  • condensation stages are cooled by cooling water, evaporating ammonia, propane, propene and/or by exploitation of the Joule-Thompson effect when depressurising process gases.
  • the heating device is operated by external waste heat.
  • the distillation apparatus consists of one single distillation column or consists of a cascade of several distillation columns in which condensers are installed between the distillation columns.
  • the distillation apparatus comprises 3, 4 or 5 successive condensers, each being operated at a different temperature level.
  • the intermediate condensers are operated at temperature levels of approx. +45° C., +15° C. and ⁇ 30° C., respectively, which is a further advantage of the invention.
  • the main part of the rising vapours in the column if used, therefore condenses before entering the column head condenser and flows downwards as liquid.
  • the coldness level necessary for operating the column head condenser about ⁇ 80° C., and the related condensation performance can be produced by depressurising the high-boiling substances within the apparatus itself, which is a further advantage of the invention.
  • FIG. 1 shows an embodiment of the inventive process, in which the distillation apparatus consists of one single distillation column and several intermediate condensers;
  • FIG. 2 shows an embodiment of the inventive process, in which the distillation apparatus comprises a stripping section and a rectifying section separately of each other;
  • FIG. 3 shows an embodiment of the inventive process, in which the distillation apparatus comprises three sections with intermediate condensers between these sections.
  • vaporous feed mixture 1 can be cooled down first to 15° C. in an ammonia vaporiser 2 , for example.
  • the obtained C 2 fraction 4 is cooled down further to about 10° C., making part of the vapour condense.
  • Vapour phase 5 and condensate 6 are fed separately into the distillation apparatus.
  • the inlet can also be above the condensation stage of the highest temperature level.
  • first condenser 9 which is designed as a two-piece condenser located above the feed tray, cooling water and ammonia being used one after the other as cooling agents. Further rising vapours are partly liquefied in second condenser 10 , which is operated with propane or propene as cooling agent so that only a small part of the vapours arrives at head condenser 11 .
  • the vapours not condensed in head condenser 11 constitute the C 2 fractions 12 and 13 which are depressurised after the condensation in expander 14 , hereby cooling down to about ⁇ 125° C.
  • This cooled vapour 15 is used as cooling agent for the cold side of head condenser 11 , where it heats up to about ⁇ 50° C.
  • C 2 fraction 4 is conveyed through heat exchanger 3 for cooling feed mixture 1 .
  • the liquid flows downwards in stripping column 16 and is partly evaporated again.
  • the non-evaporated part is drawn-off as a C 3 + product 8 at the bottom of stripping column 16 .
  • the vaporous light-boiling substances 17 flow into first condenser 9 , which is designed as a two-piece condenser, where they partly condense, cooling water and ammonia being used as cooling agents one after the other.
  • Condensate 18 and vapours 19 are given into rectification column 20 .
  • Part of the bottom product of rectification column 20 is used as reflux 21 for stripping column 16 .
  • vapours not being condensed in head condenser 11 constitute the C 2 fractions 12 and 13 which are depressurised after the condensation in expander 14 , hereby cooling down to about ⁇ 125° C.
  • This cooled vapour 15 is used as cooling agent for the cold side of head condenser 11 , where it heats up to about ⁇ 50° C. Subsequently this C 2 fraction 4 is conveyed through heat exchanger 3 for cooling feed mixture 1 .
  • first condenser 9 which is designed as a two-piece condenser, where they partly condense, cooling water and ammonia being used one after the other as cooling agents.
  • Condensate 18 and vapours 19 are given into first rectification column 22 . Part of the bottom product of first rectification column 22 is used as reflux for stripping column 16 .
  • Second condenser 10 which is operated with propane or propene as cooling agent, condensate and vapours are led into second rectification column 23 .
  • the bottom product of the second rectification column 23 serves as reflux for the first rectification column 22 , in this way only a small part of the vapours arrives at head condenser 11 .
  • Vapours not having condensed in head condenser 11 constitute C 2 fractions 12 and 13 which are depressurised after the condensation in expander 14 , hereby cooling down to about ⁇ 125° C.
  • This cooled vapour 15 is used as cooling agent for the cold side of head condenser 11 , where it heats up to about ⁇ 50° C. Subsequently this C 2 fraction 4 is conveyed through heat exchanger 3 for cooling feed mixture 1 .
  • this last variant involves the advantage that only the upper part of the second rectification column must be of a design resistant against low temperature and insulated more strongly against heat transfer, which is one of the advantages of the invention.
  • the propane refrigeration capacity is about 55% less so that the compressor capacity for the propane refrigeration circuit is about 50% less and the compressor can be of a correspondingly smaller size.

Landscapes

  • 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)
  • Water Supply & Treatment (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Analytical Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
US12/735,255 2007-12-28 2008-12-22 Process and apparatus for the separation of light-boiling components from hydrocarbon mixtures Abandoned US20110041550A1 (en)

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
DE102007063347.7 2007-12-28
DE102007063347A DE102007063347A1 (de) 2007-12-28 2007-12-28 Verfahren zur Abtrennung von leichtsiedenden Komponenten aus einem Kohlenwasserstoffstrom
PCT/EP2008/011049 WO2009083227A2 (de) 2007-12-28 2008-12-22 Verfahren und vorrichtung zur abtrennung von leicht siedenden komponenten aus kohlenwasserstoffgemischen

Publications (1)

Publication Number Publication Date
US20110041550A1 true US20110041550A1 (en) 2011-02-24

Family

ID=40690838

Family Applications (1)

Application Number Title Priority Date Filing Date
US12/735,255 Abandoned US20110041550A1 (en) 2007-12-28 2008-12-22 Process and apparatus for the separation of light-boiling components from hydrocarbon mixtures

Country Status (12)

Country Link
US (1) US20110041550A1 (ru)
EP (1) EP2225007A2 (ru)
JP (1) JP2011508031A (ru)
KR (1) KR20100125228A (ru)
CN (1) CN101932368A (ru)
BR (1) BRPI0821955A2 (ru)
CA (1) CA2710776A1 (ru)
DE (1) DE102007063347A1 (ru)
EA (1) EA201070803A1 (ru)
MX (1) MX2010007195A (ru)
WO (1) WO2009083227A2 (ru)
ZA (1) ZA201004516B (ru)

Cited By (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20120255325A1 (en) * 2011-04-08 2012-10-11 Pilot Energy Solutions, Llc Single-Unit Gas Separation Process Having Expanded, Post-Separation Vent Stream
US20220397339A1 (en) * 2021-06-09 2022-12-15 L'Air Liquide Société Anonyme pour l'Etude et l'Exploitation des Procédés Georges Claude Process for separating and liquefying methane and co2 comprising the withdrawal of vapour from an intermediate stage of the distillation column
US20220397345A1 (en) * 2021-06-09 2022-12-15 L'Air Liquide Société Anonyme pour l'Etude et l'Exploitation des Procédés Georges Claude Cryogenic purification of biogas with withdrawal at an intermediate stage and external solidification of carbon dioxide
US11946691B2 (en) 2021-06-09 2024-04-02 L'Air Liquide, Société Anonyme pour l'Etude et l'Exploitation de Procédés Georges Claude Cryogenic purification of biogas with pre-separation and external solidification of carbon dioxide
US11976879B2 (en) 2021-06-09 2024-05-07 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Process for the separation and liquefaction of methane and carbon dioxide with pre-separation upstream of the distillation column
US12018886B2 (en) 2021-06-09 2024-06-25 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Process for the separation and liquefaction of methane and carbon dioxide with solidification of carbon dioxide outside the distillation column

Families Citing this family (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2969746B1 (fr) 2010-12-23 2014-12-05 Air Liquide Condensation d'un premier fluide a l'aide d'un deuxieme fluide
RU2703249C1 (ru) * 2015-12-18 2019-10-15 Бектел Гидрокарбон Текнолоджи Солушенз, Инк. Системы и способы для извлечения целевых легких углеводородов из газообразных отходов рафинирования с использованием турбодетандера в оконечной части систем
US20190204008A1 (en) * 2016-08-25 2019-07-04 Sabic Global Technologies B.V. Above cryogenic separation process for propane dehydrogenation reactor effluent
CN109722267A (zh) * 2017-10-31 2019-05-07 珠海市启夏能源科技有限公司 一种塔罐组合式凝析油气化系统及其生产工艺
CN111545086B (zh) * 2020-05-27 2021-11-09 新疆大学 一种可逆开关型泡沫体系及其制备方法

Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3444696A (en) * 1967-02-10 1969-05-20 Stone & Webster Eng Corp Demethanization employing different temperature level refrigerants
US4163652A (en) * 1976-03-26 1979-08-07 Snamprogetti S.P.A. Refrigerative fractionation of cracking-gases in ethylene production plants
GB2205933A (en) * 1987-06-12 1988-12-21 Costain Petrocarbon Separation of hydrocarbon mixtures
US5253479A (en) * 1990-07-06 1993-10-19 Tpl S.P.A. Method and apparatus for recovery of ethylene and propylene from gas produced by the pyrolysis of hydrocarbons
US5361589A (en) * 1994-02-04 1994-11-08 Air Products And Chemicals, Inc. Precooling for ethylene recovery in dual demethanizer fractionation systems
US6560989B1 (en) * 2002-06-07 2003-05-13 Air Products And Chemicals, Inc. Separation of hydrogen-hydrocarbon gas mixtures using closed-loop gas expander refrigeration
US20070062216A1 (en) * 2003-08-13 2007-03-22 John Mak Liquefied natural gas regasification configuration and method

Patent Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3444696A (en) * 1967-02-10 1969-05-20 Stone & Webster Eng Corp Demethanization employing different temperature level refrigerants
US4163652A (en) * 1976-03-26 1979-08-07 Snamprogetti S.P.A. Refrigerative fractionation of cracking-gases in ethylene production plants
GB2205933A (en) * 1987-06-12 1988-12-21 Costain Petrocarbon Separation of hydrocarbon mixtures
US5253479A (en) * 1990-07-06 1993-10-19 Tpl S.P.A. Method and apparatus for recovery of ethylene and propylene from gas produced by the pyrolysis of hydrocarbons
US5361589A (en) * 1994-02-04 1994-11-08 Air Products And Chemicals, Inc. Precooling for ethylene recovery in dual demethanizer fractionation systems
US6560989B1 (en) * 2002-06-07 2003-05-13 Air Products And Chemicals, Inc. Separation of hydrogen-hydrocarbon gas mixtures using closed-loop gas expander refrigeration
US20070062216A1 (en) * 2003-08-13 2007-03-22 John Mak Liquefied natural gas regasification configuration and method

Cited By (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20120255325A1 (en) * 2011-04-08 2012-10-11 Pilot Energy Solutions, Llc Single-Unit Gas Separation Process Having Expanded, Post-Separation Vent Stream
US10852060B2 (en) * 2011-04-08 2020-12-01 Pilot Energy Solutions, Llc Single-unit gas separation process having expanded, post-separation vent stream
US20220397339A1 (en) * 2021-06-09 2022-12-15 L'Air Liquide Société Anonyme pour l'Etude et l'Exploitation des Procédés Georges Claude Process for separating and liquefying methane and co2 comprising the withdrawal of vapour from an intermediate stage of the distillation column
US20220397345A1 (en) * 2021-06-09 2022-12-15 L'Air Liquide Société Anonyme pour l'Etude et l'Exploitation des Procédés Georges Claude Cryogenic purification of biogas with withdrawal at an intermediate stage and external solidification of carbon dioxide
US11946691B2 (en) 2021-06-09 2024-04-02 L'Air Liquide, Société Anonyme pour l'Etude et l'Exploitation de Procédés Georges Claude Cryogenic purification of biogas with pre-separation and external solidification of carbon dioxide
US11976879B2 (en) 2021-06-09 2024-05-07 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Process for the separation and liquefaction of methane and carbon dioxide with pre-separation upstream of the distillation column
US12018886B2 (en) 2021-06-09 2024-06-25 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Process for the separation and liquefaction of methane and carbon dioxide with solidification of carbon dioxide outside the distillation column

Also Published As

Publication number Publication date
WO2009083227A2 (de) 2009-07-09
BRPI0821955A2 (pt) 2015-06-23
ZA201004516B (en) 2011-03-30
EA201070803A1 (ru) 2011-02-28
EP2225007A2 (de) 2010-09-08
CA2710776A1 (en) 2009-07-09
KR20100125228A (ko) 2010-11-30
CN101932368A (zh) 2010-12-29
WO2009083227A3 (de) 2009-09-17
JP2011508031A (ja) 2011-03-10
DE102007063347A1 (de) 2009-07-02
WO2009083227A9 (de) 2009-11-05
MX2010007195A (es) 2010-09-30

Similar Documents

Publication Publication Date Title
US20110041550A1 (en) Process and apparatus for the separation of light-boiling components from hydrocarbon mixtures
US8182654B2 (en) Heat pump for high purity bottom product
US10315971B2 (en) Process for recovering heat from a hydrocarbon separation
US20060218968A1 (en) High propane recovery process and configurations
SA110310707B1 (ar) معالجة غاز هيدروكربونى
US20110036120A1 (en) Method and apparatus for recovering and fractionating a mixed hydrocarbon feed stream
US20100101273A1 (en) Heat Pump for High Purity Bottom Product
MX2007000242A (es) Configuraciones y metodos para la separacion de condensados de gas a partir de mezclas de hidrocarburos a alta presion.
CA2517261C (en) Improved distillation sequence for the purification and recovery of hydrocarbons
JP5793139B2 (ja) 炭化水素ガス処理
US11066346B2 (en) Method and system for obtaining one or more olefins
US10487271B2 (en) Process for improving propylene recovery from FCC recovery unit
US10415879B2 (en) Process for purifying natural gas and liquefying carbon dioxide
JP2013525722A (ja) 炭化水素ガス処理
US11060037B2 (en) Method for purifying a gas rich in hydrocarbons
US6487876B2 (en) Method for providing refrigeration to parallel heat exchangers
RU2570540C1 (ru) Способ низкотемпературной переработки газа и установка для его осуществления (варианты)
WO1998046950A9 (en) Process based mixed refrigerants for ethylene plants
Key et al. Process and apparatus for C 2 recovery
MXPA96004439A (es) Componente ligero lavado en intercambiadores decalor de placa de aletas

Legal Events

Date Code Title Description
STCB Information on status: application discontinuation

Free format text: ABANDONED -- FAILURE TO RESPOND TO AN OFFICE ACTION