CN102596361A - Hydrocarbon gas processing - Google Patents

Hydrocarbon gas processing Download PDF

Info

Publication number
CN102596361A
CN102596361A CN2010800254949A CN201080025494A CN102596361A CN 102596361 A CN102596361 A CN 102596361A CN 2010800254949 A CN2010800254949 A CN 2010800254949A CN 201080025494 A CN201080025494 A CN 201080025494A CN 102596361 A CN102596361 A CN 102596361A
Authority
CN
China
Prior art keywords
flow
cooling
component
absorption plant
distillation
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.)
Granted
Application number
CN2010800254949A
Other languages
Chinese (zh)
Other versions
CN102596361B (en
Inventor
A·F·约翰克
W·L·刘易斯
J·D·威尔金森
J·T·林奇
H·M·赫德森
K·T·奎拉尔
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.)
Honeywell UOP LLC
Original Assignee
Ortloff Engineers Ltd
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
Priority claimed from US12/689,616 external-priority patent/US9021831B2/en
Application filed by Ortloff Engineers Ltd filed Critical Ortloff Engineers Ltd
Publication of CN102596361A publication Critical patent/CN102596361A/en
Application granted granted Critical
Publication of CN102596361B publication Critical patent/CN102596361B/en
Active legal-status Critical Current
Anticipated expiration legal-status Critical

Links

Images

Classifications

    • 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
    • F25J3/0209—Natural gas or substitute natural 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
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D5/00—Condensation of vapours; Recovering volatile solvents by condensation
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G5/00—Recovery of liquid hydrocarbon mixtures from gases, e.g. natural gas
    • C10G5/06—Recovery of liquid hydrocarbon mixtures from gases, e.g. natural gas by cooling or compressing
    • 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
    • F25J5/00—Arrangements of cold exchangers or cold accumulators in separation or liquefaction plants
    • 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
    • F25J2200/70—Refluxing the column with a condensed part of the feed stream, i.e. fractionator top is stripped or self-rectified
    • 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
    • F25J2210/00—Processes characterised by the type or other details of the feed stream
    • F25J2210/06—Splitting of the feed stream, e.g. for treating or cooling in different ways
    • 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
    • F25J2240/00—Processes or apparatus involving steps for expanding of process streams
    • F25J2240/02—Expansion of a process fluid in a work-extracting turbine (i.e. isentropic expansion), e.g. of the feed 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
    • F25J2270/12—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
    • 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.
    • 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
    • F25J2290/42—Modularity, pre-fabrication of modules, assembling and erection, horizontal layout, i.e. plot plan, and vertical arrangement of parts of the cryogenic unit, e.g. of the cold box

Abstract

A process and an apparatus are disclosed for the recovery of ethane, ethylene, propane, propylene, and heavier hydrocarbon components from a hydrocarbon gas stream in a compact processing assembly. The gas stream is cooled and divided into first and second streams. The first stream is further cooled to condense substantially all of it and is thereafter expanded to lower pressure and supplied as a feed between first and second absorbing means inside the processing assembly. The second stream is expanded to lower pressure and supplied as the bottom feed to the second absorbing means. A distillation vapor stream is collected from the upper region of the first absorbing means and directed into one or more heat exchange means inside the processing assembly to heat it while cooling the gas stream and the first stream. The heated distillation vapor stream is compressed to higher pressure and divided into a volatile residue gas fraction and a compressed recycle stream. The compressed recycle stream is cooled to condense substantially all of it by the distillation vapor stream in the one or more heat exchange means inside the processing assembly, and is thereafter expanded to lower pressure and supplied as top feed to the first absorbing means. A distillation liquid stream is collected from the lower region of the second absorbing means and directed into a heat and mass transfer means inside the processing assembly to heat it and strip out its volatile components while cooling the gas stream. The quantities and temperatures of the feeds to the first and second absorbing means are effective to maintain the temperature of the upper region of the first absorbing means at a temperature whereby the major portions of the desired components are recovered in the stripped distillation liquid stream.

Description

Appropriate hydrocarbon gas is handled
Technical field
The present invention relates to separate the technology and the device of gas containing hydrocarbon.The applicant is filed in the rights and interests of the U.S. Provisional Application formerly 61/186,361 on June 11st, 2009 according to the clause requirement of the 35th piece of 119 (e) joint of United States code.According to the clause of the 35th piece 120 of United States code joint, the U.S. that the applicant also requires to be filed on January 19th, 2010 partly continues the rights and interests of patent application 12/689,616.Assignee S.M.E.Products LP and Ortloff Engineers, Ltd. are the contracting parties of an effective joint study agreement before the application's invention is accomplished.
Can from multiple gases, reclaim ethene, ethane, propylene, propane and/or heavy hydrocarbon, these gases such as natural gas, refinery gas and the synthetic air that obtains by other hydrocarbon material (like coal, crude oil, naphtha, oil shale, Tar sands and brown coal).Natural gas has the methane and the ethane of larger proportion usually, and namely for methane and ethane account at least 50 moles of % of natural gas altogether.Natural gas also contains more a spot of relatively heavy hydrocarbon (like propane, butane, pentane etc.) and hydrogen, nitrogen, carbon dioxide and other gas.
Relate generally to of the present invention reclaims ethene, ethane, propylene, propane and heavy hydrocarbon from this air-flow.Air-flow to handling by the present invention carries out canonical analysis, and the result of approximate molar percentage is 90.3% methane, 4.0% ethane and other C 2Component, 1.7% propane and other C 3Component, 0.3% iso-butane, 0.5% normal butane and 0.8% pentane and above hydrocarbon, surplus person is made up of nitrogen and carbon dioxide.Sometimes also there is sulfurous gas.
Background technology
The cyclic fluctuation in history of natural gas and natural gas liquids thereof (NGL) both prices of composition makes ethane, ethene, propane, propylene and the heavy ends increment reduction as fluid product sometimes.The technology that this just causes the technology that needs exploitation can more effectively reclaim these products and can effectively reclaim with lower capital input.The existing technology that is used to separate these materials comprises based on the cooling of gas and refrigeration, oil absorbs and refrigeration oil absorbs technology.In addition, owing to the validity reason that can when expanding and from process gas, obtaining heat, produce the economical equipment of power, low temperature process is popularized.According to the rich degree (ethane, ethene and heavy hydrocarbons content) of bleed pressure, gas and the situation of required final products, can take each or their process integration in these technologies.
Low-temperature expansion technology generally is preferred at present for natural gas liquids recovery, because this technology can provide maximum simplicity, is easy to start, and flexible operation, efficient is good, and safety and reliability are good.United States Patent (USP) 3,292,380; 4,061,481; 4,140,504; 4,157,904; 4,171,964; 4,185,978; 4,251,249; 4,278,457; 4,519,824; 4,617,039; 4,687,499; 4,689,063; 4,690,702; 4,854,955; 4,869,740; 4,889,545; 5,275,005; 5,555,748; 5,566,554; 5,568,737; 5,771,712; 5,799,507; 5,881,569; 5,890,378; 5,983,664; 6,182,469; 6,578,379; 6,712,880; 6,915,662; 7,191,617; 7,219,513; The United States Patent(USP) No. of announcing again 33,408; And co-pending application 11/430,412; 11/839,693; 11/971,491 and 12/206,230 has described relevant technology (though description of the invention is in different technological conditions described in the United States Patent (USP) that is based in some cases and quotes).
Reclaim in the technology at typical low-temperature expansion, the feed stream under pressure is cooled through carrying out heat exchange with other process stream and/or external refrigeration source (like the propane compression refrigerating system).Along with gas is cooled, liquid can be condensed, and as containing some required C 2The highly pressurised liquid of+component is collected in one or more separators.According to the rich degree of gas and the situation of formed amount of liquid, can make highly pressurised liquid expand into lower pressure and fractionation.The gasification that during expansion of liquids, takes place causes the further cooling of materials flow.In some cases, in order further to reduce the temperature that comes from expansion, pre-cooled highly pressurised liquid is desirable before expanding.Comprise liquid and steam mixture expanded stream the distillation (demethanation device or deethanization device) tower in by fractionation.In tower, distillation expand cooling materials flow with remaining methane, nitrogen and other escaping gas as overhead vapours and required C as the bottom liquid product 2Component, C 3Component is separated with the heavy hydrocarbon component, perhaps with remaining methane, C 2Component, nitrogen and other escaping gas as overhead vapours with as the required C of bottom liquid product 3Component is separated with the heavy hydrocarbon component.
If feed gas does not have total condensation (generally being not have total condensation), then can remaining steam from partial condensation be divided into two materials flows.Make a part of steam reach lower pressure through do work decompressor or engine or expansion valve, under said lower pressure, because the further cooling of materials flow, more liquid is condensed.Pressure after the expansion operating pressure with destilling tower basically is identical.The steam that will produce by expanding-liquid merging offers tower as charging.
The remainder of steam is cooled to through carrying out heat exchange and condensation basically with other process stream (for example cold fractionator overhead cut).Some or all of highly pressurised liquids can steam partly merges cooling off before therewith.Through suitable expansion gear (like expansion valve) resulting cooled stream is expand into the operating pressure of demethanation device then.Between the phase of expansion, a part of liquid will gasify, and cause the cooling of total materials flow.Materials flow with rapid expanding offers the demethanation device as top fed then.Usually, merge as remaining methane product gas in the steam of rapid expanding materials flow part and the top separator section of demethanation device overhead vapours in fractionating column.Perhaps, can offer separator to cooling and the materials flow of expanding so that steam and flow to be provided.Steam and overhead fraction are merged, and charging offers tower as top drum with liquid.
In the ideal operation of this separating technology; The residual gas that leaves technology contains methane all basically in the feed gas; And there is not the heavy hydrocarbon component basically; The bottom fraction of leaving the demethanation device contains all basically heavy hydrocarbon components, and does not have methane or the bigger component of volatility basically.Yet in practice, because conventional demethanation device operates mainly as stripper, so can not reach desirable situation.Therefore the methane product of technology generally includes the steam of the top fractionation level section of leaving tower, together with the steam that does not stand any rectification step.C 2, C 3And C 4+ component generation considerable damage because top liquid charging contains these components and the heavy hydrocarbon component of a great deal of, causes the C of corresponding aequum in the steam 2Component, C 3Component, C 4Component and heavy hydrocarbon component are left the top fractionation level section of demethanation device.If can make the steam of rising and the C that can absorb quite in a large number in the steam 2Component, C 3Component, C 4The liquid (backflow) of component and heavy hydrocarbon component contacts, and then can reduce the loss of these required components widely.
In recent years, preferred hydrocarbon separating technology adopts top absorption plant section that the additional rectifying of rising steam is provided.The recycle stream of the residual gas that the reflux stream source of upper rectifying section normally provides under pressure.Usually through carrying out heat exchange the residual vaporous stream of recirculation is cooled to condensation basically with other process stream (for example cold fractionator overhead cut).Through suitable expansion gear (like expansion valve) materials flow of resulting condensation is basically expand into the operating pressure of demethanation device then.Between the phase of expansion, a part of liquid can gasify usually, causes the cooling of total materials flow.Materials flow with rapid expanding offers the demethanation device as top fed then.Usually, the steam of expanded stream partly with in the top separator section of demethanation device overhead vapours in fractionating column merges, as remaining methane product gas.Perhaps, can offer separator to cooling and the materials flow of expanding so that steam and flow to be provided so that after this steam and overhead fraction merging, and with liquid charging offers tower as top drum.The typical process scheme of this type is disclosed in the following document: United States Patent (USP) 4,889,545; 5,568,737; With 5,881,569, common application 11/430,412 co-pending and 11/971; 491 and Mowrey, E.Ross, " Efficient; High Recovery of Liquids from Natural Gas Utilizing a High Pressure Absorber ", Proceedings of the Eighty-First Annual Convention of the Gas Processors Association, Dallas; Texas, March 11-13,2002.
Summary of the invention
The present invention adopts new device more effectively to implement above-mentioned each step, and the number of packages of the equipment of use is less.This realizes in the following manner, up to the present single device product is combined in the middle of the common framework, thereby reduces the required ground block space of treatment plant and reduce the cost of investment of facility.Be unexpectedly, the applicant finds, and compacter layout has also reduced the power consumption that realizes that given recovery levels is required widely, thereby improved process efficiency and reduced the running cost of facility.In addition, compacter layout needing also to have avoided being used in the conventional plant design interconnecting most of pipeline of individual equipment product has further reduced cost of investment, and has avoided needing relevant flange pipe to connect.Because pipe flange is that (it is to have facilitated greenhouse gases and also possibly is the VOC that atmospheric ozone forms precursor that VOC) source of leaks avoids the use of the potential hazard that these flanges can reduce the atmospheric emission that destroys environment to potential hydrocarbon.
Have been found that the C that can obtain above 95% according to the present invention 2The rate of recovery.Similarly, do not requiring C 2Under the situation of component recovery, can keep C 3The rate of recovery surpasses 95%.In addition, compared with prior art, the present invention can make methane (or C with lower energy requirement 2Component) and light component and C 2(or C 3Component) realizes 100% separate basically with heavy ends, keep identical recovery levels simultaneously.Though the present invention can be applicable to lower pressure and warm temperature; But under the condition that require-50 ° of F [46 ℃] or colder NGL recovery tower overhead fraction temperature; Process feeds gas is 400 to 1500psia [2; 758 to 10,342kPa (a)] or higher scope in the time be particularly advantageous.
Invention is described
Fig. 2 illustrates the flow chart of the technology according to the present invention.Identical among feed gas composition of in the technology that Fig. 2 provides, being considered and condition and Fig. 1.Therefore, can Fig. 2 technology and Fig. 1 technology be compared so that advantage of the present invention to be described.
In the simulation of Fig. 2 technology, inlet gas gets into said device and is split into materials flow 32 and 33 two parts as materials flow 31.First is materials flow 32, the heat-exchange device in the upper area of the charging cooling section 118a of entering process equipment 118 inside.This heat-exchange device can comprise that blade adds the heat transfer unit (HTU) of tube type heat exchanger, heat-exchangers of the plate type, brazed aluminum type heat exchanger or other type, comprises multichannel and/or multioperation heat exchanger.Heat exchange between the configuration heat-exchange device flows with materials flow 32 that a passage that flows through said heat-exchange device is provided and the distillation steam that from the inner separator section 118b of process equipment 118, rises, said process equipment 118 is heated in the heat-exchange device in the lower area of charging cooling section 118a.Materials flow 32 is cooled when further adding the thermal distillation vapor stream, and materials flow 32a leaves said heat-exchange device with-25 ° of F [32 ℃].
Second portion is materials flow 33, heat transfer and mass transfer apparatus among the demethanation section 118e of entering process equipment 118 inside.This heat transfer and mass transfer apparatus can comprise that also blade adds the heat transfer unit (HTU) of tube type heat exchanger, heat-exchangers of the plate type, brazed aluminum type heat exchanger or other type, comprises multichannel and/or multioperation heat exchanger.Configuration heat transfer and mass transfer apparatus are to provide the heat exchange between the materials flow 33 of flowing through a said heat transfer and mass transfer apparatus passage and the distillation flow that from the absorber portion 118d of process equipment 118 inside, flows downward; Make materials flow 33 be cooled; The flow of heating distillation simultaneously was cooled to-47 ° of F [44 ℃] with materials flow 33a before it leaves heat transfer and mass transfer apparatus.Along with the distillation flow is heated, the one of which partial gasification forms the stripping steam, and said stripping steam is along with remaining liq continues to flow downward through heat transfer and mass transfer apparatus and to rising.Heat transfer and mass transfer apparatus provide the Continuous Contact between stripping steam and the distillation flow, so it also plays the effect that the mass transfer between vapor phase and the liquid phase is provided, the fluid product materials flow 44 of stripping methane and light component.
Materials flow 32a and 33a remerge and form materials flow 31a, and it gets into the separator section 118f of process equipment 118 inside under-32 ° of F [36 ℃] and 900psia [6,203kPa (a)], so steam (materials flow 34) separates with condensate liquid (materials flow 35).Separator section 118f has the internal head part or other installs so that itself and demethanation section 118e branch are opened, and makes that two sections in the process equipment 118 can be operated under different pressure.
Steam (materials flow 34) from separator section 118f is split into 36 and 39 two materials flows.The materials flow 36 that contains about 27% total steam merges with liquid separated (materials flow 35 is via materials flow 37), the heat-exchange device in the lower area of the charging cooling section 118a in the materials flow 38 entering process equipments 118 of merging.This heat-exchange device can comprise that equally blade adds the heat transfer unit (HTU) of tube type heat exchanger, heat-exchangers of the plate type, brazed aluminum type heat exchanger or other type, comprises multichannel and/or multioperation heat exchanger.Heat exchange between the configuration heat-exchange device flows with materials flow 38 that a passage that flows through said heat-exchange device is provided and the distillation steam that from separator section 118b, rises makes materials flow 38 when adding the thermal distillation vapor stream, be cooled to condensation basically.
Then through expansion valve 14 with the materials flow 38a rapid expanding of the condensation basically of resulting-138 ° of F [95 ℃] rectifying section 118c (absorption plant) and the operating pressure (about 400psia [2,758kPa (a)]) of absorber portion 118d (another absorption plant) in the process equipment 118.Between the phase of expansion, a part of materials flow may be gasified, and causes the cooling of total materials flow.In the technology shown in Fig. 2, the expanded stream 38b that leaves expansion valve 14 reaches the temperature of-139 ° of F [95 ℃], and is provided for the process equipment 118 between rectifying section 118c and the absorber portion 118d.Liquid among the materials flow 38b merges with the liquid that from rectifying section 118c, descends, and is directed to absorber portion 118d, and any steam merges with the steam that from absorber portion 118d, rises simultaneously, and is directed to rectifying section 118c.
Residue 73% steam (materials flow 39) from separator section 118f gets into acting decompressor 15, obtains mechanical energy by this part high pressure charging therein.Machine 15 expand into to constant entropy the operating pressure of absorber portion 118d basically with steam, and expanding through acting is cooled to approximately-99 temperature of ° F [73 ℃] with expanded stream 39a.After this expanded stream 39a of partial condensation offers the lower area of the absorber portion 118d in the process equipment 118 as charging.
The distillation steam stream 41c of recompression and cooling is split into two materials flows.A part is volatility residual gas products for materials flow 46.Another part is a recycle stream 45, and it gets into the heat-exchange device among the charging cooling section 118a in the process equipment 118.This heat-exchange device can comprise that also blade adds the heat transfer unit (HTU) of tube type heat exchanger, heat-exchangers of the plate type, brazed aluminum type heat exchanger or other type, comprises multichannel and/or multioperation heat exchanger.Heat exchange between the configuration heat-exchange device flows with materials flow 45 that a passage that flows through said heat-exchange device is provided and the distillation steam that from separator section 118b, rises makes materials flow 45 when adding the thermal distillation vapor stream, be cooled to condensation basically.
Basically the recycle stream 45a of condensation leaves the heat-exchange device among the charging cooling section 118a under-138 ° of F [95 ℃], and arrives the operating pressure of the rectifying section 118c in the process equipment 118 through expansion valve 22 rapid expanding.Between the phase of expansion, a part of materials flow gasification causes the cooling of total materials flow.In the technology shown in Fig. 2, the expanded stream 45b that leaves expansion valve 22 reaches the temperature of-146 ° of F [99 ℃], and is provided for the separator section 118b in the process equipment 118.Liquid separated is directed to rectifying section 118c therein, and remaining steam merges formation distillation steam stream with the steam that from rectifying section 118c, rises simultaneously, and said distillation steam stream is heated in cooling section 118a.
Rectifying section 118c and absorber portion 118d respectively comprise the absorption plant of being made up of following: certain combination of a plurality of column plates that are spaced vertically, one or more packed bed or column plate and filler.Column plate among rectifying section 118c and the absorber portion 118d and/or filler provide to the steam that rises and contact with necessity between the cold liquid of decline.The liquid of expanded stream 39a part with from absorber portion 118d to the liquid mixing that descends, the liquid of merging continues to enter into downwards in the middle of the demethanation section 118e.Stripping steam that from demethanation section 118e, rises and the steam of expanded stream 39a partly merge, and rise through absorber portion 118d with contact to the cold liquid that descends, thereby condensation and absorption most C2 component, C3 component and heavy ends from these steams.Any steam of steam that from absorber portion 118d, rises and expanded stream 38b partly merges; And rise through rectifying section 118c partly contacting with cold liquid to the expanded stream 45b that descends, thereby condensation with absorb remaining most of C2 component, C3 component and heavy ends in these steams.The liquid of expanded stream 38b part with from rectifying section 118c to the liquid mixing that descends, the liquid of merging continues to enter into downwards in the middle of the absorber portion 118d.
The distillate that flows downward in heat transfer the demethanation section 118e in process equipment 118 and the mass transfer apparatus by stripping methane and light component.Resulting fluid product (materials flow 44) leaves the lower area of demethanation section 118e, and leaves process equipment 118 with 65 ° of F [18 ℃].The distillation steam that from separator section 118b, rises stream heats up in charging cooling section 118a, and at this moment it provides cooling to materials flow 32,38 and 45, and is as discussed previously, and resulting distillation steam stream 41 leaves process equipment 118 with 105 ° of F [40 ℃].Divide two stage recompression distillation steam streams then, promptly by decompressor 15 Driven Compressor 16 with by additional drive power source compressor 20.In drain cooler 21, be cooled to 110 ° of F [43 ℃] with after forming materials flow 41c at materials flow 41b, extraction recycle stream 45 as discussed previously forms residual vaporous stream 46, and after this residual vaporous stream 46 flow to the sales gas pipeline under 915psia [6,307kPa (a)].
Provide the materials flow flow velocity of technology shown in Figure 2 and gathering of energy consumption in the following table:
Table II
(Fig. 2)
Stream flows gathers-pound-mol/hour [kg-moles/hour]
Figure BDA0000117899480000121
Figure BDA0000117899480000131
*(based on the flow velocity that does not round up)
The relatively demonstration of Table I and II, the present invention has kept the rate of recovery substantially the same with prior art.Yet further comparison sheet I and Table II show, realize that the employed power of product yield greatly reduces than prior art.With regard to organic efficiency (being defined as the ethane amount of per unit power recovery), the present invention is equivalent to surpass 6% than the improvement of Fig. 1 technology of prior art.
Improvement by the organic efficiency of Fig. 1 technology than prior art provided by the invention mainly is because two factors.At first, in process equipment 118, heat-exchange device in charging cooling section 118a and heat transfer and the compact Layout of mass transfer apparatus in demethanation section 118e eliminated by the pressure drop that interconnecting piping applied that is shown in the conventional treatment factory.The present invention as a result is compared with prior art the time; The feed gas that flow to decompressor 15 partly is in higher pressure, make power that the decompressor 15 among the present invention produces with higher outlet pressure can with decompressor 15 of the prior art lower outlet pressure following the power as much that can produce.Therefore, operation under can be in the fractionating column 18 than the prior art higher pressure of rectifying section 118c in the process equipment 118 of the present invention and absorber portion 118d keeps identical recovery level simultaneously.This higher operating pressure; Add distillation steam stream because the pressure drop of having got rid of due to the interconnecting piping reduces; The pressure that causes getting into the distillation steam stream of compressor 20 greatly improves, thereby reduced the present invention residual gas is returned to the required power of pipeline pressure.
Second; In demethanation section 118e, use heat transfer and mass transfer apparatus side by side to heat the distillate that leaves absorber portion 118d; Make resulting steam ability contact liq and its volatile component of stripping simultaneously, this is more efficient than the conventional destilling tower that use has outside reboiler.Volatile component by continuously from liquid stripping come out, reduced the concentration of volatile component in the stripping steam quickly, thereby improved steam stripping efficiency of the present invention.
Compared with prior art, the present invention also provides two other advantages except improving process efficiency.At first, the compact Layout of process equipment 118 of the present invention replaces five independent device products of the prior art ( heat exchanger 10,11 and 13 among Fig. 1 with single device product (process equipment 118 among Fig. 2); Separator 12; And fractionating column 18).Reduced the plot space requirement like this, and got rid of the interconnection pipeline, compared with prior art reduced treatment plant and utilized cost of investment of the present invention.The second, get rid of the interconnection pipeline and mean that the flange that utilizes treatment plant of the present invention to have connects far fewer than prior art, reduced source of leaks number potential in the factory.Hydrocarbon is VOC (VOC), and some of them are classified as greenhouse gases, and some of them possibly be the precursors that forms atmospheric ozone, this means that the present invention can reduce the potential hazard of the atmospheric emission that can destroy environment.
Other embodiment
Possibly tend under the certain situation directly provides flow 35 to the lower area of absorber portion 118d through materials flow 40, like Fig. 2,4, shown in 6 and 8.In this case, use suitable expansion gear (like expansion valve 17), resulting expansion flow 40a is offered the lower area (shown in dotted line) of absorber portion 118d as charging the operating pressure of expansion of liquids to absorber portion 118d.Steam (Fig. 2 and 6) in the part (materials flow 37) that possibly tend to make flow 35 under the certain situation and the materials flow 36 or merge the materials flow 38 that merges to form with the second portion 33a (Fig. 4 and 8) of cooling, and the remainder of flow 35 is sent to the lower area of absorber portion 118d through materials flow 40/40a.Possibly tend to make expansion flow 40a and expanded stream 39a (Fig. 2 and 6) or expanded stream 34a (Fig. 4 and 8) to merge under the certain situation, after this materials flow that merges offered the lower area of absorber portion 118d as single charging.
If feed gas is than rich, possibly among the demethanation section 118e of (shown in Fig. 5 and 9) other mass-transfer zone is set in (shown in Fig. 3 and 7) between expanded stream 39a and the expansion flow 40a or between expanded stream 34a and expansion flow 40a even as big as tending in liquid separated amount in the materials flow 35.In this case, can heat transfer and the mass transfer apparatus among the demethanation section 118e be configured in the upper and lower, make and can expansion flow 40a be incorporated between these two parts.Shown in dotted line; Possibly tend under the certain situation merge the materials flow 38 that merges to form with the steam (Fig. 3 and 7) in the part (materials flow 37) of flow 35 and the materials flow 36 or with the second portion 33a (Fig. 5 and 9) of cooling; Remainder (materials flow 40) with flow 35 expand into lower pressure simultaneously, and as providing between the top of heat transfer and the mass transfer apparatus of materials flow 40a in demethanation section 118e and the bottom.
Possibly tend to first and second part (materials flow 32a and 33a) of nonjoinder cooling under the certain situation, like Fig. 4,5, shown in 8 and 9.In this case, have only the 32a of first of cooling to be conducted to separator section 118f (Figure 4 and 5) or separator 12 (Fig. 8 and 9) in the process equipment 118, steam (materials flow 34) separates with the liquid (materials flow 35) of condensation at this place.Steam flow 34 gets into acting decompressor 15, and expand into to constant entropy the operating pressure of absorber portion 118d basically, and the materials flow 34a that expands then offers the lower area of the absorber portion 118d in the process equipment 118 as charging.Second portion 33a and the liquid separated (materials flow 35 is via materials flow 37) of cooling merges, and the materials flow 38 of merging is conducted to the heat-exchange device in the lower area of the interior charging cooling section 118a of process equipment 118, and is cooled to condensation basically.Basically the materials flow 38a of condensation is through the operating pressure of expansion valve 14 rapid expanding to rectifying section 118c and absorber portion 118d, and expanded stream 38b is provided for the process equipment 118 between rectifying section 118c and the absorber portion 118d then.Possibly tend under the certain situation only the part (materials flow 37) of flow 35 and the second portion 33a of cooling merged, remainder (materials flow 40) offers the lower area of absorber portion 118d via expansion valve 17.Possibly tend to all flows 35 delivered to the lower area of absorber portion 118d under other situation via expansion valve 17.
In some cases, possibly separate the incoming flow 31a of cooling or the 32a of first of cooling by the favourable external separator container that is to use, rather than comprise the separator section 118f in the process equipment 118.Shown in Fig. 6 and 7, can use separator 12 that the incoming flow 31a of cooling is separated into steam flow 34 and flow 35.Equally, shown in Fig. 8 and 9, can use separator 12 that the 32a of first of cooling is separated into steam flow 34 and flow 35.
According to the heavy hydrocarbon amount in the feed gas and the situation of feed gas pressure; The incoming flow 31a of the separator section 118f among entering Fig. 2 and 3 or the cooling of the separator 12 in Fig. 6 and 7 (or 32a of first of the cooling of separator section 118f in the entering Figure 4 and 5 or the separator 12 in Fig. 8 and 9) possibly not contain any liquid (because it is higher than its dew point, perhaps because it is higher than its cricondenbar).In this case; In materials flow 35 and 37, there is not liquid (shown in dotted line); Therefore have only in the materials flow 36 in steam (Fig. 2 and 3) from separator section 118f, the materials flow 36 and flow to materials flow 38 from the steam (Fig. 6 and 7) of separator 12 or the second portion 33a (Fig. 4,5,8 and 9) of cooling; Become the materials flow 38b of the condensation basically of expansion, offer the process equipment 118 between rectifying section 118c and the absorber portion 118d.In this case, can not need separator section 118f (Fig. 2 to 5) or separator 12 (Fig. 6 to 9) in the process equipment 118.
Feed gas condition, plant layout, existing equipment or other factors can show, decompressor 15 or to replace with the expansion gear (like expansion valve) that substitutes be feasible need not do work.Though be in specific expansion gear, to have described independent materials flow to expand, suitably can use alternative expansion gear under the situation.For example, condition can permit the acting of recycle stream (materials flow 45a) of part (materials flow 38a) or the condensation basically of the condensation basically of incoming flow to expand.
According to the present invention, can take to utilize external refrigeration to replenish the cooling to inlet gas that can obtain by distillation steam and flow, particularly under the situation of rich inlet gas.In this case; Heat transfer and mass transfer apparatus can be included in (or gathering-device among the separator section 118f; Do not contain under the situation of liquid at the incoming flow 31a that works as cooling or the 32a of first of cooling); Shown in the dotted line among Fig. 2 to 5, perhaps heat transfer and mass transfer apparatus can be included in the separator 12, shown in the dotted line among Fig. 6 to 9.This heat transfer and mass transfer apparatus can comprise that blade adds the heat transfer unit (HTU) of tube type heat exchanger, heat-exchangers of the plate type, brazed aluminum type heat exchanger or other type, comprises multichannel and/or multioperation heat exchanger.Configuration is conducted heat and mass transfer apparatus; In order to freezing materials flow that a passage that flows through said heat transfer and mass transfer apparatus is provided (for example; Propane) and the heat exchange between the steam of materials flow 31a (Fig. 2,3,6 and 7) that upwards flows or materials flow 32a (Fig. 4,5, the 8 and 9) part; Make refrigerator cooled vapor and the more liquid of condensation further, these liquid are to descending to become the partially liq that in materials flow 35, removes.Perhaps; Get into separator section 118f (Fig. 2 and 3) or separator 12 (Fig. 6 and 7) or materials flow 32a at materials flow 31a and get into separator section 118f (Figure 4 and 5) or separator 12 (Fig. 8 and 9) before; Can use conventional gas cooler, with refrigerant cools materials flow 32a, materials flow 33a and/or materials flow 31a.
Situation according to the C2 group component that will reclaim in the temperature of feed gas and Fu Du and the fluid product materials flow 44 possibly can not get enough heating by materials flow 33 and satisfy product specification so that leave the liquid of demethanation section 118e.In this case, heat transfer and mass transfer apparatus among the demethanation section 118e can comprise supply, with heat medium supplementary heating to be provided, shown in the dotted line among Fig. 2 to 9.Perhaps, can comprise other heat transfer and mass transfer apparatus in the lower area of demethanation section 118e, be used to provide supplementary heating, perhaps can heat it with heat medium before at the heat transfer and the mass transfer apparatus that materials flow 33 are offered among the demethanation section 118e.
Heat transfer unit (HTU) type cases according to the heat-exchange device of the top of selecting to be used for charging cooling section 118a and lower area might be combined in these heat-exchange devices in single multichannel and/or the multioperation heat transfer unit (HTU).In this case, in order to accomplish required cooling and heating, multichannel and/or multioperation heat transfer unit (HTU) will comprise the appropriate device that is used to distribute, separate and collect materials flow 32, materials flow 38, materials flow 45 and distillation steam stream.
Possibly tend in the upper area of demethanation section 118e, provide other mass transfer under the certain situation.In this case, mass transfer apparatus can be arranged in second portion 33a following and cooling that expanded stream 39a (Fig. 2,3,6 and 7) or expanded stream 34a (Fig. 4,5,8 and 9) get into the lower area part of absorber portion 118d leave demethanation section 118e heat transfer and mass transfer apparatus part above.
The less preferred selection of Fig. 2 of the present invention, 3,6 and 7 embodiment provides the separator flask of the 31a of first that is used to cool off, the separator flask of the second portion 32a that is used to cool off; Be incorporated in wherein the steam flow that separates forming steam flow 34, and be incorporated in the flow of wherein separating to form flow 35.Another less preferred selection of the present invention is cooled stream 37 in the independent heat-exchange device in charging cooling section 118a (rather than with materials flow 36 or materials flow 33a merge the materials flow 38 that to form merge with materials flow 37); In independent expansion gear, the expand materials flow of cooling, and the materials flow of expanding offered the zone line among the absorber portion 118d.
Recognize that the relative quantity of charging that is shown in each tributary of vapor feed separately depends on a number of factors, and comprises the amount and the available horsepower amount of the heat that gas pressure, feed gas are formed, can from charging, be extracted economically.More charging can improve the rate of recovery above absorber portion 118d, reduces the power that from expander, reclaims simultaneously, thereby has increased the horsepower requirement of recompression.Charging below the increase absorber portion 118d has reduced horsepower consumption, but also can reduce product recovery rate.
By the required utility consumption amount of technological operation, the present invention provides the recovery of improved C2 component, C3 component and heavy hydrocarbon component or C3 component and heavy hydrocarbon component.The improved form of expression of technological operation required drive consumption indicators can reduce for the power requirement of compression or recompression, the power requirement of external refrigeration reduces, the energy requirement of supplementary heating reduces or their combination.
Though described and it is believed that and be the preferred embodiment of the invention; But one of ordinary skill in the art would recognize that; Do not departing under the situation of the essence of the present invention that limits following claim; Can carry out other and further revise the present invention, for example make the present invention be applicable to different condition, feed type or other requirement.
Description of drawings
In order to understand the present invention better, with reference to following embodiment and accompanying drawing.With reference to accompanying drawing:
Fig. 1 is according to United States Patent(USP) No. 5,568, the flow chart of the natural gas processing plant of 737 prior art;
Fig. 2 is the flow chart according to natural gas processing plant of the present invention; And
Fig. 3 to 9 illustrates the flow chart of application of the present invention to the replacement device of natural gas flow.
The specific embodiment
In the explanation to above-mentioned figure, the summary sheet of the flow velocity that the representative processes condition is calculated is provided below.For convenience's sake, in the table that occurs in this article, flow speed value (mole/hour) has been rounded up to immediate integer.The total flow rate that is shown in the table comprises all non-hydrocarbon components, therefore common summation greater than hydrocarbon component materials flow flow velocity.The indication temperature is the approximation that is rounded up near the number of degrees.It should also be noted that the process design and calculation of carrying out for the technology of describing in the comparative drawings figs is based on such supposition, i.e. the not heat leak from the environment to technology or from technology to the environment.The quality of commercially available isolated material makes this become very reasonably hypothesis, and normally those skilled in the art can make.
For convenience's sake, with traditional English unit with International System of Units (SI) recording process parameter.Provide in the table the mole flow velocity can be interpreted as the pound-mol/hour or kilogram mole/hour.The energy consumption that is recorded as horsepower (HP) and/or thousand British thermal units/hour (MBTU/Hr) corresponding to said with pound-mol/hour be the mole flow velocity of unit.The energy consumption that is recorded as kilowatt (kW) corresponding to said with kg-moles/hour be the mole flow velocity of unit.
Description of the Prior Art
Fig. 1 shows to adopt according to United States Patent(USP) No. 5,568 that 737 prior art reclaims C from natural gas 2The process chart of treatment plant's design of+component.In the simulation of this technology, inlet gas is as materials flow 31 access to plant under 110 ° of F [43 ℃] and 915psia [6,307kPa (a)].If inlet gas contains certain density obstruction product stream sulfur-containing compound up to specification, then remove sulfur-containing compound through feed gas being carried out suitable preliminary treatment (not shown).In addition, usually incoming flow is dewatered to prevent under cryogenic conditions, forming hydrate (ice).Solid drier is normally used for this purpose.
Incoming flow 31 is split into materials flow 32 and 33 two parts.Materials flow 32 is cooled to-26 ° of F [32 ℃] through carrying out heat exchange with cold distillation steam stream 41a in heat exchanger 10, materials flow 33 is simultaneously carried out heat exchange through the tower side reboiler liquid (materials flow 42) with the demethanation device reboiler liquid (materials flow 43) of 41 ° of F [5 ℃] and-49 ° of F [45 ℃] and is cooled to-32 ° of F [35 ℃] in heat exchanger 11. Materials flow 32a and 33a remerge and form materials flow 31a, and it gets into separator 12 down at-28 ° of F [33 ℃] and 893psia [6,155kPa (a)], and steam (materials flow 34) separates with condensate liquid (materials flow 35) at this place.
Steam (materials flow 34) from separator 12 is split into 36 and 39 two materials flows.The materials flow 36 that contains total steam of about 27% merges with separator liquid (materials flow 35), and the materials flow 38 of merging through heat exchanger 13, is cooled to basically condensation at this place with the mode that is heat exchange relationship with cold distillation steam stream 41.Through expansion valve 14 the materials flow 38a rapid expanding of the condensation basically of resulting-139 ° of F [95 ℃] is arrived the operating pressure (approximately 396psia [2,730kPa (a)]) of fractionating column 18 then.Between the phase of expansion, a part of materials flow gasification causes the cooling of total materials flow.In the technology shown in Fig. 1, the expanded stream 38b that leaves expansion valve 14 reaches the temperature of-140 ° of F [95 ℃], and offers fractionating column 18 at the first tower intermediate feed point..
Residue 73% steam (materials flow 39) from separator 12 gets into acting decompressor 15, obtains mechanical energy by this part high pressure charging therein.Machine 15 expand into to constant entropy the tower operating pressure basically with steam, and expanding through acting is cooled to approximately-95 temperature of ° F [71 ℃] with expanded stream 39a.Typical commercially available decompressor can be obtained the general 80-85% of the merit that can from desirable constant entropy expansion, obtain in theory.The merit that obtains is often used for driving centrifugal compressor (as installing 16), and said centrifugal compressor for example can be used for recompressing the distillation steam stream (materials flow 41b) that is heated.After this expanded stream 39a of partial condensation offers fractionating column 18 as charging at the second tower intermediate feed point.
The distillation steam stream 41e of recompression and cooling is split into two materials flows.A part is volatility residual gas products for materials flow 46.Another part is a recycle stream 45, and it flow to heat exchanger 10, is cooled to-26 ° of F [32 ℃] at this place through carrying out heat exchange with cold distillation steam stream 41a.The recycle stream 45a of cooling flow to interchanger 13 then, is cooled to-139 ° of F [95 ℃] and condensation basically at this place through carrying out heat exchange with cold distillation steam stream 41.Basically the materials flow 45b of condensation expand into demethanation device operating pressure through suitable expansion gear (like expansion valve 22) then, causes total stream cools to-147 ° of F [99 ℃].Charging offers fractionating column 18 to the materials flow 45c that expands then as top drum.The steam part (if any) of materials flow 45c merges to form distillation steam stream 41 with the steam that from the top fractionation level section of tower, rises, and it is extracted out from the upper area of tower.
Demethanation device in the tower 18 is conventional destilling tower, and it includes certain combination of a plurality of column plates that are spaced vertically, one or more packed bed or column plate and filler.As common situation in natural gas processing plant, fractionating column can constitute by two sections.Upper segment 18a is a separator; The top fed of part gasification therein is split into its corresponding steam and liquid part; And the steam that wherein from bottom distillation or demethanation section 18b, rises and the steam of top fed partly merge the cold demethanation device overhead vapours (materials flow 41) of formation, and it leaves the top of tower with-144 ° of F [98 ℃].The demethanation section 18b of bottom comprises column plate and/or filler, and provides to the liquid that descends and contact with necessity between the steam of rising.Demethanation section 18b also comprises reboiler (like the reboiler and the tower side reboiler of previous description); The part of the liquid that its heating flows downward along tower and with its gasification so that the stripping steam to be provided; Said stripping steam upwards flows with the stripping fluid product along tower, the materials flow 44 of namely for methane and light component.
According to the mass ratio of methane in bottom product and ethane is 0.010: 1 typical specification, and fluid product materials flow 44 is at the bottom of leaving tower under 64 ° of F [18 ℃].Demethanation device vapor stream of top of the tower 41 passes through heat exchanger 13 upstream with feed gas of coming in and recycle stream; Be heated to-40 ° of F [40 ℃] (materials flow 41a) at this place; And, be heated to 104 ° of F [40 ℃] (materials flow 41b) at this place through heat exchanger 10.Divide two stage recompression distillation steam streams then.Phase I is by decompressor 15 Driven Compressor 16.Second stage is by additional drive power source compressor 20, and said compressor 20 is compressed to sales line pressure with residual gas (materials flow 41d).After in drain cooler 21, being cooled to 110 ° of F [43 ℃], materials flow 41e is divided into residual gas product (materials flow 46) and recycle stream 45, and is as discussed previously.Residual vaporous stream 46 flow to the sales gas pipeline under the 915psia [6,307kPa (a)] that is enough to satisfy pipeline requirement (general usually be inlet pressure).
Provide the materials flow flow velocity of technology shown in Figure 1 and gathering of energy consumption in the following table:
Table I
(Fig. 1)
Stream flow gathers-pound-mol/hour [kg-moles/hour]
Figure BDA0000117899480000081
Figure BDA0000117899480000082
*(based on the flow velocity s that does not round up)

Claims (38)

1. one kind will contain methane, C 2Component, C 3Component becomes the technology of the less relatively cut of volatility residual gas cut and volatility with the flow separation of heavy hydrocarbon component, the less relatively cut of said volatility contains said C 2Component, C 3Component and heavy hydrocarbon component or said C 3The major part of component and heavy hydrocarbon component, wherein
(1) said airflow diversion is become first and second parts;
(2) cool off said first;
(3) cool off said second portion;
(4) first of said cooling and the second portion of said cooling are merged to form cooled gas flow;
(5) said cooled gas flow is split into first and second materials flows;
(6) said first materials flow of cooling is with its all condensations basically, and after this expand into lower pressure, thus with its further cooling;
(7) first materials flow that said expansion cooling is provided is as the charging between first and second absorption plant that in process equipment, is provided with, said first absorption plant be positioned at said second absorption plant above;
(8) said second materials flow is expand into said lower pressure, and offer said second absorption plant as bottom feed;
(9) from the upper area of said first absorption plant, collect distillation steam stream and heating, after this said distillation steam stream that is heated of discharging from said process equipment;
(10) the said distillation steam stream that is heated is compressed to higher pressure, and after this is split into the recycle stream of said volatility residual gas cut and compression;
(11) recycle stream of the said compression of cooling is with its all condensations basically;
(12) the recirculated compressed materials flow with said condensation basically expand into said lower pressure, and offers said first absorption plant as top fed;
(13) accomplish the said heating of said distillation steam stream in the one or more heat-exchange devices that in said process equipment, are provided with, thereby at least a portion in the step of providing (2), (6) and (11) is cooled off;
(14) from the lower area of said second absorption plant, collect the distillation flow; And heat in heat transfer in being arranged at said process equipment and the mass transfer apparatus; Thereby the cooling of at least a portion in the step of providing (3); The bigger component of stripping volatility from said distillation flow simultaneously, and after this be heated and steam stripped distillation flow is discharged from said process equipment as the less relatively cut of said volatility said; And
(15) make the quantity of the said incoming flow of said first and second absorption plants and temperature can be effectively remained on certain temperature with the temperature of the said upper area of said first absorption plant, reclaim the major part of the component in the less relatively cut of said volatility thus.
2. one kind will contain methane, C 2Component, C 3Component becomes the technology of the less relatively cut of volatility residual gas cut and volatility with the flow separation of heavy hydrocarbon component, the less relatively cut of said volatility contains said C 2Component, C 3Component and heavy hydrocarbon component or said C 3The major part of component and heavy hydrocarbon component, wherein
(1) said airflow diversion is become first and second parts;
(2) cool off said first;
(3) cool off said second portion;
(4) first of said cooling and the second portion of said cooling are merged to form the air-flow of partial condensation;
(5) air-flow with said partial condensation offers separator, and separates therein, thereby obtains steam flow and at least one flow;
(6) said steam flow is split into first and second materials flows;
(7) said first materials flow of cooling is with its all condensations basically, and after this expand into lower pressure, thus with its further cooling;
(8) first materials flow that said expansion cooling is provided is as the charging between first and second absorption plant that in process equipment, is provided with, said first absorption plant be positioned at said second absorption plant above;
(9) said second materials flow is expand into said lower pressure, and offer said second absorption plant as first bottom feed;
(10) at least a portion with said at least one flow expand into said lower pressure, and offers said second absorption plant as second bottom feed;
(11) from the upper area of said first absorption plant, collect distillation steam stream and heating, after this from said process equipment, discharge the said distillation steam stream that is heated;
(12) the said distillation steam stream that is heated is compressed to higher pressure, and after this is split into the recycle stream of said volatility residual gas cut and compression;
(13) recycle stream of the said compression of cooling is with its all condensations basically;
(14) the recirculated compressed materials flow with said condensation basically expand into said lower pressure, and offers said first absorption plant as top fed;
(15) accomplish the said heating of said distillation steam stream in the one or more heat-exchange devices that in said process equipment, are provided with, thereby at least a portion in the step of providing (2), (7) and (13) is cooled off;
(16) from the lower area of said second absorption plant, collect the distillation flow; And heat in heat transfer in being arranged at said process equipment and the mass transfer apparatus; Thereby the cooling of at least a portion in the step of providing (3); The bigger component of stripping volatility from said distillation flow simultaneously, and after this be heated and steam stripped distillation flow is discharged from said process equipment as the less relatively cut of said volatility said; And
(17) make the quantity of the said incoming flow of said first and second absorption plants and temperature can be effectively remained on certain temperature with the temperature of the said upper area of said first absorption plant, reclaim the major part of the component in the less relatively cut of said volatility thus.
3. one kind will contain methane, C 2Component, C 3Component becomes the technology of the less relatively cut of volatility residual gas cut and volatility with the flow separation of heavy hydrocarbon component, the less relatively cut of said volatility contains said C 2Component, C 3Component and heavy hydrocarbon component or said C 3The major part of component and heavy hydrocarbon component, wherein
(1) said airflow diversion is become first and second parts;
(2) cool off said first;
(3) cool off said second portion;
(4) first of said cooling and the second portion of said cooling are merged to form the air-flow of partial condensation;
(5) air-flow with said partial condensation offers separator, and separates therein, thereby obtains steam flow and at least one flow;
(6) said steam flow is split into first and second materials flows;
(7) at least a portion with said first materials flow and said at least one flow merges the materials flow that merges to form;
(8) materials flow of the said merging of cooling is with its all condensations basically, and after this expand into lower pressure, thus with its further cooling;
(9) the merging materials flow that said expansion cooling is provided is as the charging between first and second absorption plant that in process equipment, is provided with, said first absorption plant be positioned at said second absorption plant above;
(10) said second materials flow is expand into said lower pressure, and offer said second absorption plant as first bottom feed;
(11) any remainder with said at least one flow expand into said lower pressure, and offers said second absorption plant as second bottom feed;
(12) from the upper area of said first absorption plant, collect distillation steam stream and heating, after this from said process equipment, discharge the said distillation steam stream that is heated;
(13) the said distillation steam stream that is heated is compressed to higher pressure, and after this is split into the recycle stream of said volatility residual gas cut and compression;
(14) recycle stream of the said compression of cooling is with its all condensations basically;
(15) the recirculated compressed materials flow with said condensation basically expand into said lower pressure, and offers said first absorption plant as top fed;
(16) accomplish the said heating of said distillation steam stream in the one or more heat-exchange devices that in said process equipment, are provided with, thereby at least a portion in the step of providing (2), (8) and (14) is cooled off;
(17) from the lower area of said second absorption plant, collect the distillation flow; And heat in heat transfer in being arranged at said process equipment and the mass transfer apparatus; Thereby the cooling of at least a portion in the step of providing (3); The bigger component of stripping volatility from said distillation flow simultaneously, and after this be heated and steam stripped distillation flow is discharged from said process equipment as the less relatively cut of said volatility said; And
(18) make the quantity of the said incoming flow of said first and second absorption plants and temperature can be effectively remained on certain temperature with the temperature of the said upper area of said first absorption plant, reclaim the major part of the component in the less relatively cut of said volatility thus.
4. one kind will contain methane, C 2Component, C 3Component becomes the technology of the less relatively cut of volatility residual gas cut and volatility with the flow separation of heavy hydrocarbon component, the less relatively cut of said volatility contains said C 2Component, C 3Component and heavy hydrocarbon component or said C 3The major part of component and heavy hydrocarbon component, wherein
(1) said airflow diversion is become first and second parts;
(2) after this cooling of said first is also expand into lower pressure;
(3) the said second portion of cooling is with its all condensations basically, and after this expand into said lower pressure, thus with its further cooling;
(4) second portion that said expansion cooling is provided is as the charging between first and second absorption plant that in process equipment, is provided with, said first absorption plant be positioned at said second absorption plant above;
(5) first with said expansion cooling offers said second absorption plant as bottom feed;
(6) from the upper area of said first absorption plant, collect distillation steam stream and heating, after this from said process equipment, discharge the said distillation steam stream that is heated;
(7) the said distillation steam stream that is heated is compressed to higher pressure, and after this is split into the recycle stream of said volatility residual gas cut and compression;
(8) recycle stream of the said compression of cooling is with its all condensations basically;
(9) the recirculated compressed materials flow with said condensation basically expand into said lower pressure, and offers said first absorption plant as top fed;
(10) accomplish the said heating of said distillation steam stream in the one or more heat-exchange devices that in said process equipment, are provided with, thereby at least a portion in the step of providing (2), (3) and (8) is cooled off;
(11) from the lower area of said second absorption plant, collect the distillation flow; And heat in heat transfer in being arranged at said process equipment and the mass transfer apparatus; Thereby the cooling of at least a portion in the step of providing (3); The bigger component of stripping volatility from said distillation flow simultaneously, and after this be heated and steam stripped distillation flow is discharged from said process equipment as the less relatively cut of said volatility said; And
(12) make the quantity of the said incoming flow of said first and second absorption plants and temperature can be effectively remained on certain temperature with the temperature of the said upper area of said first absorption plant, reclaim the major part of the component in the less relatively cut of said volatility thus.
5. one kind will contain methane, C 2Component, C 3Component becomes the technology of the less relatively cut of volatility residual gas cut and volatility with the flow separation of heavy hydrocarbon component, the less relatively cut of said volatility contains said C 2Component, C 3Component and heavy hydrocarbon component or said C 3The major part of component and heavy hydrocarbon component, wherein
(1) said airflow diversion is become first and second parts;
(2) fully cool off said first with its partly condensation;
(3) first with said partial condensation offers separator, and separates therein, thereby obtains steam flow and at least one flow;
(4) the said second portion of cooling is with its all condensations basically, and after this expand into lower pressure, thus with its further cooling;
(5) second portion that said expansion cooling is provided is as the charging between first and second absorption plant that in process equipment, is provided with, said first absorption plant be positioned at said second absorption plant above;
(6) said steam flow is expand into said lower pressure, and offer said second absorption plant as first bottom feed;
(7) at least a portion with said at least one flow expand into said lower pressure, and offers said second absorption plant as second bottom feed;
(8) from the upper area of said first absorption plant, collect distillation steam stream and heating, after this from said process equipment, discharge the said distillation steam stream that is heated;
(9) the said distillation steam stream that is heated is compressed to higher pressure, and after this is split into the recycle stream of said volatility residual gas cut and compression;
(10) recycle stream of the said compression of cooling is with its all condensations basically;
(11) the recirculated compressed materials flow with said condensation basically expand into said lower pressure, and offers said first absorption plant as top fed;
(12) accomplish the said heating of said distillation steam stream in the one or more heat-exchange devices that in said process equipment, are provided with, thereby at least a portion in the step of providing (2), (4) and (10) is cooled off;
(13) from the lower area of said second absorption plant, collect the distillation flow; And heat in heat transfer in being arranged at said process equipment and the mass transfer apparatus; Thereby the cooling of at least a portion in the step of providing (4); The bigger component of stripping volatility from said distillation flow simultaneously, and after this be heated and steam stripped distillation flow is discharged from said process equipment as the less relatively cut of said volatility said; And
(14) make the quantity of the said incoming flow of said first and second absorption plants and temperature can be effectively remained on certain temperature with the temperature of the said upper area of said first absorption plant, reclaim the major part of the component in the less relatively cut of said volatility thus.
6. one kind will contain methane, C 2Component, C 3Component becomes the technology of the less relatively cut of volatility residual gas cut and volatility with the flow separation of heavy hydrocarbon component, the less relatively cut of said volatility contains said C 2Component, C 3Component and heavy hydrocarbon component or said C 3The major part of component and heavy hydrocarbon component, wherein
(1) said airflow diversion is become first and second parts;
(2) fully cool off said first with its partly condensation;
(3) first with said partial condensation offers separator, and separates therein, thereby obtains steam flow and at least one flow;
(4) cool off said second portion, and after this merge the materials flow that merges to form with at least a portion of said at least one flow;
(5) materials flow of the said merging of cooling is with its all condensations basically, and after this expand into lower pressure, thus with its further cooling;
(6) the merging materials flow that said expansion cooling is provided is as the charging between first and second absorption plant that in process equipment, is provided with, said first absorption plant be positioned at said second absorption plant above;
(7) said steam flow is expand into said lower pressure, and offer said second absorption plant as first bottom feed;
(8) any remainder with said at least one flow expand into said lower pressure, and offers said second absorption plant as second bottom feed;
(9) from the upper area of said first absorption plant, collect distillation steam stream and heating, after this from said process equipment, discharge the said distillation steam stream that is heated;
(10) the said distillation steam stream that is heated is compressed to higher pressure, and after this is split into the recycle stream of said volatility residual gas cut and compression;
(11) recycle stream of the said compression of cooling is with its all condensations basically;
(12) the recirculated compressed materials flow with said condensation basically expand into said lower pressure, and offers said first absorption plant as top fed;
(13) accomplish the said heating of said distillation steam stream in the one or more heat-exchange devices that in said process equipment, are provided with, thereby at least a portion in the step of providing (2), (5) and (11) is cooled off;
(14) from the lower area of said second absorption plant, collect the distillation flow; And heat in heat transfer in being arranged at said process equipment and the mass transfer apparatus; Thereby the cooling of at least a portion in the step of providing (4); The bigger component of stripping volatility from said distillation flow simultaneously, and after this be heated and steam stripped distillation flow is discharged from said process equipment as the less relatively cut of said volatility said; And
(15) make the quantity of the said incoming flow of said first and second absorption plants and temperature can be effectively remained on certain temperature with the temperature of the said upper area of said first absorption plant, reclaim the major part of the component in the less relatively cut of said volatility thus.
7. technology according to claim 2, wherein
(1) said heat transfer and mass transfer apparatus are arranged in the zone, upper and lower; And
(2) said process equipment is provided between the said top and lower area that at least a portion of the said expansion of said at least one flow enters into said heat transfer and mass transfer apparatus.
8. technology according to claim 3, wherein
(1) said heat transfer and mass transfer apparatus are arranged in the zone, upper and lower; And
(2) said process equipment is provided between the said top and lower area that any remainder of the said expansion of said at least one flow enters into said heat transfer and mass transfer apparatus.
9. technology according to claim 5, wherein
(1) said heat transfer and mass transfer apparatus are arranged in the zone, upper and lower; And
(2) said process equipment is provided between the said top and lower area that at least a portion of the said expansion of said at least one flow enters into said heat transfer and mass transfer apparatus.
10. technology according to claim 6, wherein
(1) said heat transfer and mass transfer apparatus are arranged in the zone, upper and lower; And
(2) said process equipment is provided between the said top and lower area that any remainder of the said expansion of said at least one flow enters into said heat transfer and mass transfer apparatus.
11. according to claim 2,3,5,6,7,8,9 or 10 described technologies, wherein said separator is arranged in the said process equipment.
12. technology according to claim 1, wherein
(1) gathering-device is arranged in the said process equipment;
(2) in the said gathering-device other heat transfer and mass transfer apparatus are set, said other heat transfer and mass transfer apparatus comprise one or more paths that are used for the external refrigeration medium;
(3) said cooled gas flow is offered said gathering-device, and be directed at said other heat transfer and mass transfer apparatus further to be cooled off by said external refrigeration medium; And
(4) said further cooled gas flow is split into said first and second materials flows.
13. technology according to claim 4, wherein
(1) gathering-device is arranged in the said process equipment;
(2) in the said gathering-device other heat transfer and mass transfer apparatus are set, said other heat transfer and mass transfer apparatus comprise one or more paths that are used for the external refrigeration medium;
(3) first with said cooling offers said gathering-device, and is directed at said other heat transfer and mass transfer apparatus further to be cooled off by said external refrigeration medium; And
(4) first with said further cooling expand into said lower pressure, and after this offers said second absorption plant as said bottom feed.
14. according to claim 2,3,5,6,7,8,9 or 10 described technologies, wherein
(1) establish other heat transfer and mass transfer apparatus in the said separator, said other heat transfer and mass transfer apparatus comprise one or more paths that are used for the external refrigeration medium;
(2) said steam flow is directed at said other heat transfer and mass transfer apparatus with by said external refrigeration medium cooling, thereby forms other condensate; And
(3) said condensate becomes the part of said at least one flow of separating therein.
15. technology according to claim 11, wherein
(1) establish other heat transfer and mass transfer apparatus in the said separator, said other heat transfer and mass transfer apparatus comprise one or more paths that are used for the external refrigeration medium;
(2) said steam flow is directed at said other heat transfer and mass transfer apparatus with by said external refrigeration medium cooling, thereby forms other condensate; And
(3) said condensate becomes the part of said at least one flow of separating therein.
16. according to claim 1,2,3,4,5,6,7,8,9,10,12 or 13 described technologies; Wherein said heat transfer and mass transfer apparatus comprise one or more paths that are used for external heating medium; To replenish the heating that provides by said second portion, be used for the said stripping of the bigger component of said volatility from said distillation flow.
17. technology according to claim 11; Wherein said heat transfer and mass transfer apparatus comprise one or more paths that are used for external heating medium; To replenish the heating that provides by said second portion, be used for the said stripping of the bigger component of said volatility from said distillation flow.
18. technology according to claim 14; Wherein said heat transfer and mass transfer apparatus comprise one or more paths that are used for external heating medium; To replenish the heating that provides by said second portion, be used for the said stripping of the bigger component of said volatility from said distillation flow.
19. technology according to claim 15; Wherein said heat transfer and mass transfer apparatus comprise one or more paths that are used for external heating medium; To replenish the heating that provides by said second portion, be used for the said stripping of the bigger component of said volatility from said distillation flow.
20. one kind is used for containing methane, C 2Component, C 3Component becomes the device of the less relatively cut of volatility residual gas cut and volatility with the flow separation of heavy hydrocarbon component,, the less relatively cut of said volatility contains said C 2Component, C 3Component and heavy hydrocarbon component or said C 3The major part of component and heavy hydrocarbon component comprises
(1) first part flow arrangement, it becomes first and second parts with said airflow diversion;
(2) heat-exchange device, it is arranged in the process equipment and is connected in said first part flow arrangement to receive said first and with its cooling;
(3) conduct heat and mass transfer apparatus, it is arranged in the said process equipment and is connected in said first part flow arrangement to receive said second portion and with its cooling;
(4) combined unit, it is connected in said heat-exchange device and said heat transfer and mass transfer apparatus, in order to the second portion of the first that receives said cooling and said cooling and form cooled gas flow;
(5) second part flow arrangements, it is connected in said combined unit to receive said cooled gas flow and it is split into first and second materials flows;
(6) said heat-exchange device further is connected in said second part flow arrangement, in order to receive said first materials flow and it is cooled to be enough to basically with its condensation;
(7) first expansion gears, it is connected in said heat-exchange device and expand into lower pressure with first materials flow that receives said condensation basically and with it;
(8) first and second absorption plants; Said first and second absorption plants are arranged in the said process equipment; And be connected in said first expansion gear; In order to first materials flow that receives said expansion cooling as the charging between said first and second absorption plant, said first absorption plant be positioned at said second absorption plant above;
(9) second expansion gears; It is connected in said second part flow arrangement; In order to receiving said second materials flow and it expand into said lower pressure, said second expansion gear further be connected in said second absorption plant with second materials flow that said expansion is provided as bottom feed to it;
(10) steam gathering-device, it is arranged in the said process equipment and is connected in said first absorption plant to receive the distillation steam stream from the upper area of said first absorption plant;
(11) said heat-exchange device further is connected in said steam gathering-device to receive said distillation steam stream and to be heated; Thereby the cooling of at least a portion in the step of providing (2) and (6), and after this from said process equipment, discharge the said distillation steam stream that is heated;
(12) compression set, it is connected in said process equipment to receive the said distillation steam stream that is heated and it is compressed to higher pressure;
(13) cooling device, it is connected in said compression set with the distillation steam stream that receives said compression and with its cooling;
(14) the 3rd part flow arrangements, it is connected in said cooling device, flows in order to the compression distillation steam that receives said cooling, and it is split into the recycle stream of said volatility residual gas cut and compression;
(15) said heat-exchange device further is connected in said the 3rd part flow arrangement, be cooled to be enough to basically its condensation in order to the recycle stream that receives said compression and with it, thus the heating of at least a portion in the step of providing (11);
(16) the 3rd expansion gears; It is connected in said heat-exchange device; Expand into said lower pressure in order to the recirculated compressed materials flow that receives said condensation basically and with it, said the 3rd expansion gear further be connected in said first absorption plant with recycle stream that said expansion is provided as top fed to it;
(17) fluid collection device, it is arranged in the said process equipment and is connected in said second absorption plant, in order to receive the distillation flow from the lower area of said second absorption plant;
(18) said heat transfer and mass transfer apparatus further are connected in said fluid collection device to receive said distillation flow and to be heated; Thereby the cooling of at least a portion in the step of providing (3); The bigger component of stripping volatility from said distillation flow simultaneously, and after this be heated and steam stripped distillation flow is discharged from said process equipment as the less relatively cut of said volatility said; With
(19) control device; It is adapted to regulate quantity and the temperature to the said incoming flow of said first and second absorption plants; Temperature with the said upper area of said first absorption plant remains on certain temperature, reclaims the major part of the component in the less relatively cut of said volatility thus.
21. one kind is used for containing methane, C 2Component, C 3Component becomes the device of the less relatively cut of volatility residual gas cut and volatility with the flow separation of heavy hydrocarbon component,, the less relatively cut of said volatility contains said C 2Component, C 3Component and heavy hydrocarbon component or said C 3The major part of component and heavy hydrocarbon component comprises
(1) first part flow arrangement, it becomes first and second parts with said airflow diversion;
(2) heat-exchange device, it is arranged in the process equipment and is connected in said first part flow arrangement to receive said first and with its cooling;
(3) conduct heat and mass transfer apparatus, it is arranged in the said process equipment and is connected in said first part flow arrangement to receive said second portion and with its cooling;
(4) combined unit, it is connected in said heat-exchange device and said heat transfer and mass transfer apparatus, in order to the second portion of the first that receives said cooling and said cooling and form the air-flow of partial condensation;
(5) separator, it is connected in said combined unit, separates into steam flow and at least one flow in order to the air-flow that receives said partial condensation and with it;
(6) second part flow arrangements, it is connected in said separator to receive said steam flow and it is split into first and second materials flows;
(7) said heat-exchange device further is connected in said second part flow arrangement, in order to receive said first materials flow and it is cooled to be enough to basically with its condensation;
(8) first expansion gears, it is connected in said heat-exchange device and expand into lower pressure with first materials flow that receives said condensation basically and with it;
(9) first and second absorption plants; Said first and second absorption plants are arranged in the said process equipment; And be connected in said first expansion gear; In order to first materials flow that receives said expansion cooling as the charging between said first and second absorption plant, said first absorption plant be positioned at said second absorption plant above;
(10) second expansion gears; It is connected in said second part flow arrangement; In order to receiving said second materials flow and it expand into said lower pressure, said second expansion gear further be connected in said second absorption plant with second materials flow that said expansion is provided as first bottom feed to it;
(11) the 3rd expansion gears; It is connected in said separator; Expand into said lower pressure in order at least a portion of receiving said at least one flow and with it, said the 3rd expansion gear further be connected in said second absorption plant with flow that said expansion is provided as second bottom feed to it;
(12) steam gathering-device, it is arranged in the said process equipment and is connected in said first absorption plant to receive the distillation steam stream from the upper area of said first absorption plant;
(13) said heat-exchange device further is connected in said steam gathering-device to receive said distillation steam stream and to be heated; Thereby the cooling of at least a portion in the step of providing (2) and (7), and after this from said process equipment, discharge the said distillation steam stream that is heated;
(14) compression set, it is connected in said process equipment to receive the said distillation steam stream that is heated and it is compressed to higher pressure;
(15) cooling device, it is connected in said compression set with the distillation steam stream that receives said compression and with its cooling;
(16) the 3rd part flow arrangements, it is connected in said cooling device, flows in order to the compression distillation steam that receives said cooling, and it is split into the recycle stream of said volatility residual gas cut and compression;
(17) said heat-exchange device further is connected in said the 3rd part flow arrangement, be cooled to be enough to basically its condensation in order to the recycle stream that receives said compression and with it, thus the heating of at least a portion in the step of providing (13);
(18) the 4th expansion gears; It is connected in said heat-exchange device; Expand into said lower pressure in order to the recirculated compressed materials flow that receives said condensation basically and with it, said the 4th expansion gear further be connected in said first absorption plant with recycle stream that said expansion is provided as top fed to it;
(19) fluid collection device, it is arranged in the said process equipment and is connected in said second absorption plant, in order to receive the distillation flow from the lower area of said second absorption plant;
(20) said heat transfer and mass transfer apparatus further are connected in said fluid collection device to receive said distillation flow and to be heated; Thereby the cooling of at least a portion in the step of providing (3); The bigger component of stripping volatility from said distillation flow simultaneously, and after this be heated and steam stripped distillation flow is discharged from said process equipment as the less relatively cut of said volatility said; With
(21) control device; It is adapted to regulate quantity and the temperature to the said incoming flow of said first and second absorption plants; Temperature with the said upper area of said first absorption plant remains on certain temperature, reclaims the major part of the component in the less relatively cut of said volatility thus.
22. one kind is used for containing methane, C 2Component, C 3Component becomes the device of the less relatively cut of volatility residual gas cut and volatility with the flow separation of heavy hydrocarbon component,, the less relatively cut of said volatility contains said C 2Component, C 3Component and heavy hydrocarbon component or said C 3The major part of component and heavy hydrocarbon component comprises
(1) first part flow arrangement, it becomes first and second parts with said airflow diversion;
(2) heat-exchange device, it is arranged in the said process equipment and is connected in said first part flow arrangement to receive said first and with its cooling;
(3) conduct heat and mass transfer apparatus, it is arranged in the said process equipment and is connected in said first part flow arrangement to receive said second portion and with its cooling;
(4) first combined units, it is connected in said heat-exchange device and said heat transfer and mass transfer apparatus, in order to the second portion of the first that receives said cooling and said cooling and form the air-flow of partial condensation;
(5) separator, it is connected in said first combined unit, separates into steam flow and at least one flow in order to the air-flow that receives said partial condensation and with it;
(6) second part flow arrangements, it is connected in said separator to receive said steam flow and it is split into first and second materials flows;
(7) second combined units, it is connected in said second part flow arrangement and said separator, in order at least a portion that receives said first materials flow and said at least one flow and the materials flow that forms merging;
(8) said heat-exchange device further is connected in said second combined unit, is cooled to be enough to basically with its condensation in order to the materials flow that receives said merging and with it;
(9) first expansion gears, it is connected in said heat-exchange device and expand into lower pressure with the merging materials flow that receives said condensation basically and with it;
(10) first and second absorption plants; Said first and second absorption plants are arranged in the said process equipment; And be connected in said first expansion gear; In order to the merging materials flow that receives said expansion cooling as the charging between said first and second absorption plant, said first absorption plant be positioned at said second absorption plant above;
(11) second expansion gears; It is connected in said second part flow arrangement; In order to receiving said second materials flow and it expand into said lower pressure, said second expansion gear further be connected in said second absorption plant with second materials flow that said expansion is provided as first bottom feed to it;
(12) the 3rd expansion gears; It is connected in said separator; Expand into said lower pressure in order to any remainder of receiving said at least one flow and with it, said the 3rd expansion gear further be connected in said second absorption plant with flow that said expansion is provided as second bottom feed to it;
(13) steam gathering-device, it is arranged in the said process equipment and is connected in said first absorption plant to receive the distillation steam stream from the upper area of said first absorption plant;
(14) said heat-exchange device further is connected in said steam gathering-device to receive said distillation steam stream and to be heated; Thereby the cooling of at least a portion in the step of providing (2) and (8), and after this from said process equipment, discharge the said distillation steam stream that is heated;
(15) compression set, it is connected in said process equipment to receive the said distillation steam stream that is heated and it is compressed to higher pressure;
(16) cooling device, it is connected in said compression set with the distillation steam stream that receives said compression and with its cooling;
(17) the 3rd part flow arrangements, it is connected in said cooling device, flows in order to the compression distillation steam that receives said cooling, and it is split into the recycle stream of said volatility residual gas cut and compression;
(18) said heat-exchange device further is connected in said the 3rd part flow arrangement, be cooled to be enough to basically its condensation in order to the recycle stream that receives said compression and with it, thus the heating of at least a portion in the step of providing (14);
(19) the 4th expansion gears; It is connected in said heat-exchange device; Expand into said lower pressure in order to the recirculated compressed materials flow that receives said condensation basically and with it, said the 4th expansion gear further be connected in said first absorption plant with recycle stream that said expansion is provided as top fed to it;
(20) fluid collection device, it is arranged in the said process equipment and is connected in said second absorption plant, in order to receive the distillation flow from the lower area of said second absorption plant;
(21) said heat transfer and mass transfer apparatus further are connected in said fluid collection device to receive said distillation flow and to be heated; Thereby the cooling of at least a portion in the step of providing (3); The bigger component of stripping volatility from said distillation flow simultaneously, and after this be heated and steam stripped distillation flow is discharged from said process equipment as the less relatively cut of said volatility said; With
(22) control device; It is adapted to regulate quantity and the temperature to the said incoming flow of said first and second absorption plants; Temperature with the said upper area of said first absorption plant remains on certain temperature, reclaims the major part of the component in the less relatively cut of said volatility thus.
23. one kind is used for containing methane, C 2Component, C 3Component becomes the device of the less relatively cut of volatility residual gas cut and volatility with the flow separation of heavy hydrocarbon component,, the less relatively cut of said volatility contains said C 2Component, C 3Component and heavy hydrocarbon component or said C 3The major part of component and heavy hydrocarbon component comprises
(1) first part flow arrangement, it becomes first and second parts with said airflow diversion;
(2) heat-exchange device, it is arranged in the said process equipment and is connected in said first part flow arrangement to receive said first and with its cooling;
(3) conduct heat and mass transfer apparatus, it is arranged in the said process equipment and is connected in said first part flow arrangement to receive said second portion and with its cooling;
(4) said heat-exchange device further is connected in said heat transfer and mass transfer apparatus, also further it is cooled to be enough to basically with its condensation in order to the second portion that receives said cooling;
(5) first expansion gears, it is connected in said heat-exchange device and expand into lower pressure with the second portion that receives said condensation basically and with it;
(6) first and second absorption plants; Said first and second absorption plants are arranged in the said process equipment; And be connected in said first expansion gear; In order to the second portion that receives said expansion cooling as the charging between said first and second absorption plant, said first absorption plant be positioned at said second absorption plant above;
(7) second expansion gears; It is connected in said heat-exchange device; Expand into said lower pressure in order to the first that receives said cooling and with it, said second expansion gear further be connected in said second absorption plant with first that said expansion cooling is provided as bottom feed to it;
(8) steam gathering-device, it is arranged in the said process equipment and is connected in said first absorption plant to receive the distillation steam stream from the upper area of said first absorption plant;
(9) said heat-exchange device further is connected in said steam gathering-device to receive said distillation steam stream and to be heated; Thereby the cooling of at least a portion in the step of providing (2) and (4), and after this from said process equipment, discharge the said distillation steam stream that is heated;
(10) compression set, it is connected in said process equipment to receive the said distillation steam stream that is heated and it is compressed to higher pressure;
(11) cooling device, it is connected in said compression set with the distillation steam stream that receives said compression and with its cooling;
(12) second part flow arrangements, it is connected in said cooling device, flows in order to the compression distillation steam that receives said cooling, and it is split into the recycle stream of said volatility residual gas cut and compression;
(13) said heat-exchange device further is connected in said second part flow arrangement, be cooled to be enough to basically its condensation in order to the recycle stream that receives said compression and with it, thus the heating of at least a portion in the step of providing (9);
(14) the 3rd expansion gears; It is connected in said heat-exchange device; Expand into said lower pressure in order to the recirculated compressed materials flow that receives said condensation basically and with it, said the 3rd expansion gear further be connected in said first absorption plant with recycle stream that said expansion is provided as top fed to it;
(15) fluid collection device, it is arranged in the said process equipment and is connected in said second absorption plant, in order to receive the distillation flow from the lower area of said second absorption plant;
(16) said heat transfer and mass transfer apparatus further are connected in said fluid collection device to receive said distillation flow and to be heated; Thereby the cooling of at least a portion in the step of providing (3); The bigger component of stripping volatility from said distillation flow simultaneously, and after this be heated and steam stripped distillation flow is discharged from said process equipment as the less relatively cut of said volatility said; With
(17) control device; It is adapted to regulate quantity and the temperature to the said incoming flow of said first and second absorption plants; Temperature with the said upper area of said first absorption plant remains on certain temperature, reclaims the major part of the component in the less relatively cut of said volatility thus.
24. one kind is used for containing methane, C 2Component, C 3Component becomes the device of the less relatively cut of volatility residual gas cut and volatility with the flow separation of heavy hydrocarbon component, the less relatively cut of said volatility contains said C 2Component, C 3Component and heavy hydrocarbon component or said C 3The major part of component and heavy hydrocarbon component comprises
(1) first part flow arrangement, it becomes first and second parts with said airflow diversion;
(2) heat-exchange device, it is arranged in the said process equipment and is connected in said first part flow arrangement to receive said first and it is cooled to be enough to its partial condensation;
(3) separator, it is connected in said heat-exchange device, separates into steam flow and at least one flow in order to the first that receives said partial condensation and with it;
(4) conduct heat and mass transfer apparatus, it is arranged in the said process equipment and is connected in said first part flow arrangement to receive said second portion and with its cooling;
(5) said heat-exchange device further is connected in said heat transfer and mass transfer apparatus, also further it is cooled to be enough to basically with its condensation in order to the second portion that receives said cooling;
(6) first expansion gears, it is connected in said heat-exchange device and expand into lower pressure with the second portion that receives said condensation basically and with it;
(7) first and second absorption plants; Said first and second absorption plants are arranged in the said process equipment; And be connected in said first expansion gear; In order to the second portion that receives said expansion cooling as the charging between said first and second absorption plant, said first absorption plant be positioned at said second absorption plant above;
(8) second expansion gears; It is connected in said separator; In order to receiving said steam flow and it expand into said lower pressure, said second expansion gear further be connected in said second absorption plant with steam flow that said expansion is provided as first bottom feed to it;
(9) the 3rd expansion gears; It is connected in said separator; Expand into said lower pressure in order at least a portion of receiving said at least one flow and with it, said the 3rd expansion gear further be connected in said second absorption plant with flow that said expansion is provided as second bottom feed to it;
(10) steam gathering-device, it is arranged in the said process equipment and is connected in said first absorption plant to receive the distillation steam stream from the upper area of said first absorption plant;
(11) said heat-exchange device further is connected in said steam gathering-device to receive said distillation steam stream and to be heated; Thereby the cooling of at least a portion in the step of providing (2) and (5), and after this from said process equipment, discharge the said distillation steam stream that is heated;
(12) compression set, it is connected in said process equipment to receive the said distillation steam stream that is heated and it is compressed to higher pressure;
(13) cooling device, it is connected in said compression set with the distillation steam stream that receives said compression and with its cooling;
(14) second part flow arrangements, it is connected in said cooling device, flows in order to the compression distillation steam that receives said cooling, and it is split into the recycle stream of said volatility residual gas cut and compression;
(15) said heat-exchange device further is connected in said second part flow arrangement, be cooled to be enough to basically its condensation in order to the recycle stream that receives said compression and with it, thus the heating of at least a portion in the step of providing (11);
(16) the 4th expansion gears; It is connected in said heat-exchange device; Expand into said lower pressure in order to the recirculated compressed materials flow that receives said condensation basically and with it, said the 4th expansion gear further be connected in said first absorption plant with recycle stream that said expansion is provided as top fed to it;
(17) fluid collection device, it is arranged in the said process equipment and is connected in said second absorption plant, in order to receive the distillation flow from the lower area of said second absorption plant;
(18) said heat transfer and mass transfer apparatus further are connected in said fluid collection device to receive said distillation flow and to be heated; Thereby the cooling of at least a portion in the step of providing (4); The bigger component of stripping volatility from said distillation flow simultaneously, and after this be heated and steam stripped distillation flow is discharged from said process equipment as the less relatively cut of said volatility said; With
(19) control device; It is adapted to regulate quantity and the temperature to the said incoming flow of said first and second absorption plants; Temperature with the said upper area of said first absorption plant remains on certain temperature, reclaims the major part of the component in the less relatively cut of said volatility thus.
25. one kind is used for containing methane, C 2Component, C 3Component becomes the device of the less relatively cut of volatility residual gas cut and volatility with the flow separation of heavy hydrocarbon component, the less relatively cut of said volatility contains said C 2Component, C 3Component and heavy hydrocarbon component or said C 3The major part of component and heavy hydrocarbon component comprises
(1) first part flow arrangement, it becomes first and second parts with said airflow diversion;
(2) heat-exchange device, it is arranged in the said process equipment and is connected in said first part flow arrangement to receive said first and it is cooled to be enough to its partial condensation;
(3) separator, it is connected in said heat-exchange device, separates into steam flow and at least one flow in order to the first that receives said partial condensation and with it;
(4) conduct heat and mass transfer apparatus, it is arranged in the said process equipment and is connected in said first part flow arrangement to receive said second portion and with its cooling;
(5) combined unit, it is connected in said heat transfer and mass transfer apparatus and said separator, in order to second portion and at least a portion of said at least one flow and the materials flow that formation merges that receives said cooling;
(6) said heat-exchange device further is connected in said combined unit, is cooled to be enough to basically with its condensation in order to the materials flow that receives said merging and with it;
(7) first expansion gears, it is connected in said heat-exchange device and expand into lower pressure with the merging materials flow that receives said condensation basically and with it;
(8) first and second absorption plants; Said first and second absorption plants are arranged in the said process equipment; And be connected in said first expansion gear; In order to the merging materials flow that receives said expansion cooling as the charging between said first and second absorption plant, said first absorption plant be positioned at said second absorption plant above;
(9) second expansion gears; It is connected in said separator; In order to receiving said steam flow and it expand into said lower pressure, said second expansion gear further be connected in said second absorption plant with steam flow that said expansion is provided as first bottom feed to it;
(10) the 3rd expansion gears; It is connected in said separator; Expand into said lower pressure in order to any remainder of receiving said at least one flow and with it, said the 3rd expansion gear further be connected in said second absorption plant with flow that said expansion is provided as second bottom feed to it;
(11) steam gathering-device, it is arranged in the said process equipment and is connected in said first absorption plant to receive the distillation steam stream from the upper area of said first absorption plant;
(12) said heat-exchange device further is connected in said steam gathering-device to receive said distillation steam stream and to be heated; Thereby the cooling of at least a portion in the step of providing (2) and (6), and after this from said process equipment, discharge the said distillation steam stream that is heated;
(13) compression set, it is connected in said process equipment to receive the said distillation steam stream that is heated and it is compressed to higher pressure;
(14) cooling device, it is connected in said compression set with the distillation steam stream that receives said compression and with its cooling;
(15) second part flow arrangements, it is connected in said cooling device, flows in order to the compression distillation steam that receives said cooling, and it is split into the recycle stream of said volatility residual gas cut and compression;
(16) said heat-exchange device further is connected in said second part flow arrangement, be cooled to be enough to basically its condensation in order to the recycle stream that receives said compression and with it, thus the heating of at least a portion in the step of providing (12);
(17) the 4th expansion gears; It is connected in said heat-exchange device; Expand into said lower pressure in order to the recirculated compressed materials flow that receives said condensation basically and with it, said the 4th expansion gear further be connected in said first absorption plant with recycle stream that said expansion is provided as top fed to it;
(18) fluid collection device, it is arranged in the said process equipment and is connected in said second absorption plant, in order to receive the distillation flow from the lower area of said second absorption plant;
(19) said heat transfer and mass transfer apparatus further are connected in said fluid collection device to receive said distillation flow and to be heated; Thereby the cooling of at least a portion in the step of providing (4); The bigger component of stripping volatility from said distillation flow simultaneously, and after this be heated and steam stripped distillation flow is discharged from said process equipment as the less relatively cut of said volatility said; With
(20) control device; It is adapted to regulate quantity and the temperature to the said incoming flow of said first and second absorption plants; Temperature with the said upper area of said first absorption plant remains on certain temperature, reclaims the major part of the component in the less relatively cut of said volatility thus.
26. device according to claim 21, wherein
(1) said heat transfer and mass transfer apparatus are arranged in the zone, upper and lower; And
(2) said process equipment is connected in said the 3rd expansion gear, in order to receiving the flow of said expansion, and between the said top of said heat transfer and mass transfer apparatus and lower area, it is guided.
27. device according to claim 22, wherein
(1) said heat transfer and mass transfer apparatus are arranged in the zone, upper and lower; And
(2) said process equipment is connected in said the 3rd expansion gear, in order to receiving the flow of said expansion, and between the said top of said heat transfer and mass transfer apparatus and lower area, it is guided.
28. device according to claim 24, wherein
(1) said heat transfer and mass transfer apparatus are arranged in the zone, upper and lower; And
(2) said process equipment is connected in said the 3rd expansion gear, in order to receiving the flow of said expansion, and between the said top of said heat transfer and mass transfer apparatus and lower area, it is guided.
29. device according to claim 25, wherein
(1) said heat transfer and mass transfer apparatus are arranged in the zone, upper and lower; And
(2) said process equipment is connected in said the 3rd expansion gear, in order to receiving the flow of said expansion, and between the said top of said heat transfer and mass transfer apparatus and lower area, it is guided.
30. according to claim 21,22,24,25,26,27,28 or 29 described devices, wherein said separator is arranged in the said process equipment.
31. device according to claim 20, wherein
(1) gathering-device is arranged in the said process equipment;
(2) in the said gathering-device other heat transfer and mass transfer apparatus are set, said other heat transfer and mass transfer apparatus comprise one or more paths that are used for the external refrigeration medium;
(3) said gathering-device is connected in said combined unit receiving said cooled gas flow, and it is directed at said other heat transfer and mass transfer apparatus further to be cooled off by said external refrigeration medium; And
(4) said second part flow arrangement is adapted to be connected with said gathering-device receiving said further cooled gas flow, and it is split into said first and second materials flows.
32. device according to claim 23, wherein
(1) gathering-device is arranged in the said process equipment;
(2) in the said gathering-device other heat transfer and mass transfer apparatus are set, said other heat transfer and mass transfer apparatus comprise one or more paths that are used for the external refrigeration medium;
(3) said gathering-device is connected in said heat-exchange device receiving the first of said cooling, and it is directed at said other heat transfer and mass transfer apparatus further to be cooled off by said external refrigeration medium; And
(4) said second expansion gear is adapted to be connected with said gathering-device; Expand into said lower pressure in order to the first that receives said further cooling and with it, said second expansion gear further be connected in said second absorption plant with the first of further cooling that said expansion is provided as said bottom feed to it;
33. according to claim 21,22,24,25,26,27,28 or 29 described devices, wherein
(1) establish other heat transfer and mass transfer apparatus in the said separator, said other heat transfer and mass transfer apparatus comprise one or more paths that are used for the external refrigeration medium;
(2) said steam flow is conducted to said other heat transfer and mass transfer apparatus with by said external refrigeration medium cooling, thereby forms other condensate; And
(3) said condensate becomes the part of said at least one flow of separating therein.
34. device according to claim 30, wherein
(1) establish other heat transfer and mass transfer apparatus in the said separator, said other heat transfer and mass transfer apparatus comprise one or more paths that are used for the external refrigeration medium;
(2) said steam flow is conducted to said other heat transfer and mass transfer apparatus with by said external refrigeration medium cooling, thereby forms other condensate; And
(3) said condensate becomes the part of said at least one flow of separating therein.
35. according to claim 20,21,22,23,24,25,26,27,28,29,31 or 32 described devices; Wherein said heat transfer and mass transfer apparatus comprise one or more paths that are used for external heating medium; To replenish the heating that provides by said second portion, be used for the said stripping of the bigger component of said volatility from said distillation flow.
36. device according to claim 30; Wherein said heat transfer and mass transfer apparatus comprise one or more paths that are used for external heating medium; To replenish the heating that provides by said second portion, be used for the said stripping of the bigger component of said volatility from said distillation flow.
37. device according to claim 33; Wherein said heat transfer and mass transfer apparatus comprise one or more paths that are used for external heating medium; To replenish the heating that provides by said second portion, be used for the said stripping of the bigger component of said volatility from said distillation flow.
38. device according to claim 34; Wherein said heat transfer and mass transfer apparatus comprise one or more paths that are used for external heating medium; To replenish the heating that provides by said second portion, be used for the said stripping of the bigger component of said volatility from said distillation flow.
CN201080025494.9A 2009-06-11 2010-03-04 Hydrocarbon gas processing Active CN102596361B (en)

Applications Claiming Priority (5)

Application Number Priority Date Filing Date Title
US18636109P 2009-06-11 2009-06-11
US61/186,361 2009-06-11
US12/689,616 2010-01-19
US12/689,616 US9021831B2 (en) 2009-02-17 2010-01-19 Hydrocarbon gas processing
PCT/US2010/026185 WO2010144163A1 (en) 2009-06-11 2010-03-04 Hydrocarbon gas processing

Publications (2)

Publication Number Publication Date
CN102596361A true CN102596361A (en) 2012-07-18
CN102596361B CN102596361B (en) 2015-06-03

Family

ID=43309149

Family Applications (1)

Application Number Title Priority Date Filing Date
CN201080025494.9A Active CN102596361B (en) 2009-06-11 2010-03-04 Hydrocarbon gas processing

Country Status (13)

Country Link
EP (1) EP2440311A1 (en)
JP (1) JP5552159B2 (en)
KR (1) KR101643796B1 (en)
CN (1) CN102596361B (en)
AU (1) AU2010259236B2 (en)
CA (1) CA2763698C (en)
CO (1) CO6480938A2 (en)
EA (1) EA022763B1 (en)
MX (1) MX2011013079A (en)
MY (1) MY162763A (en)
PE (1) PE20121168A1 (en)
TN (1) TN2011000624A1 (en)
WO (1) WO2010144163A1 (en)

Cited By (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN104069717A (en) * 2013-03-29 2014-10-01 张家港市苏承环保设备有限公司 Solvent separating and processing device
CN104792116A (en) * 2014-11-25 2015-07-22 中国寰球工程公司 System and technology for recycling ethane and light dydrocarbon above ethane from natural gas
CN105531552A (en) * 2013-09-11 2016-04-27 奥特洛夫工程有限公司 Hydrocarbon gas processing
CN108507277A (en) * 2018-04-28 2018-09-07 中国石油工程建设有限公司 A kind of the cold comprehensive utilization device and method of natural gas ethane recovery
CN110470102A (en) * 2018-05-11 2019-11-19 气体产品与化学公司 Modular L NG separator and flash gas heat exchanger
CN111033159A (en) * 2017-06-01 2020-04-17 奥特洛夫工程有限公司 Hydrocarbon gas processing

Families Citing this family (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP5870086B2 (en) * 2010-03-31 2016-02-24 オートロフ・エンジニアーズ・リミテッド Treatment of hydrocarbon gas
WO2015038289A1 (en) * 2013-09-11 2015-03-19 Ortloff Engineers, Ltd. Hydrocarbon gas processing
US11428465B2 (en) * 2017-06-01 2022-08-30 Uop Llc Hydrocarbon gas processing

Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN1169772A (en) * 1994-11-10 1998-01-07 埃尔考公司 Hydrocarbon gas processing method
US20080190136A1 (en) * 2007-02-09 2008-08-14 Ortloff Engineers, Ltd. Hydrocarbon Gas Processing
US20090107175A1 (en) * 2003-01-16 2009-04-30 Patel Sanjiv N Multiple Reflux Stream Hydrocarbon Recovery Process

Family Cites Families (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS546500B1 (en) * 1976-02-15 1979-03-29
UA76750C2 (en) * 2001-06-08 2006-09-15 Елккорп Method for liquefying natural gas (versions)
US6742358B2 (en) * 2001-06-08 2004-06-01 Elkcorp Natural gas liquefaction
WO2004076946A2 (en) * 2003-02-25 2004-09-10 Ortloff Engineers, Ltd Hydrocarbon gas processing
JP4551446B2 (en) * 2004-04-26 2010-09-29 オートロフ・エンジニアーズ・リミテッド Natural gas liquefaction

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN1169772A (en) * 1994-11-10 1998-01-07 埃尔考公司 Hydrocarbon gas processing method
CN100335854C (en) * 1994-11-10 2007-09-05 奥特洛夫工程有限公司 Hydrocarbon gas processing method
US20090107175A1 (en) * 2003-01-16 2009-04-30 Patel Sanjiv N Multiple Reflux Stream Hydrocarbon Recovery Process
US20080190136A1 (en) * 2007-02-09 2008-08-14 Ortloff Engineers, Ltd. Hydrocarbon Gas Processing

Cited By (10)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN104069717A (en) * 2013-03-29 2014-10-01 张家港市苏承环保设备有限公司 Solvent separating and processing device
CN105531552A (en) * 2013-09-11 2016-04-27 奥特洛夫工程有限公司 Hydrocarbon gas processing
CN105531552B (en) * 2013-09-11 2018-05-25 奥特洛夫工程有限公司 Hydrocarbon gas processing
CN104792116A (en) * 2014-11-25 2015-07-22 中国寰球工程公司 System and technology for recycling ethane and light dydrocarbon above ethane from natural gas
CN111033159A (en) * 2017-06-01 2020-04-17 奥特洛夫工程有限公司 Hydrocarbon gas processing
CN111033159B (en) * 2017-06-01 2021-10-08 环球油品公司 Hydrocarbon gas processing
CN108507277A (en) * 2018-04-28 2018-09-07 中国石油工程建设有限公司 A kind of the cold comprehensive utilization device and method of natural gas ethane recovery
CN110470102A (en) * 2018-05-11 2019-11-19 气体产品与化学公司 Modular L NG separator and flash gas heat exchanger
US10982898B2 (en) 2018-05-11 2021-04-20 Air Products And Chemicals, Inc. Modularized LNG separation device and flash gas heat exchanger
CN110470102B (en) * 2018-05-11 2022-03-04 气体产品与化学公司 Modular LNG separator and flash gas heat exchanger

Also Published As

Publication number Publication date
CA2763698A1 (en) 2010-12-16
AU2010259236B2 (en) 2015-11-05
EA022763B1 (en) 2016-02-29
EP2440311A1 (en) 2012-04-18
KR20120026607A (en) 2012-03-19
KR101643796B1 (en) 2016-07-29
WO2010144163A1 (en) 2010-12-16
AU2010259236A2 (en) 2012-06-07
MX2011013079A (en) 2012-02-01
CA2763698C (en) 2016-08-16
AU2010259236A1 (en) 2012-02-23
MY162763A (en) 2017-07-14
AU2010259236A8 (en) 2012-09-06
JP2012529620A (en) 2012-11-22
EA201270002A1 (en) 2012-07-30
TN2011000624A1 (en) 2013-05-24
WO2010144163A8 (en) 2012-04-19
CN102596361B (en) 2015-06-03
CO6480938A2 (en) 2012-07-16
JP5552159B2 (en) 2014-07-16
PE20121168A1 (en) 2012-08-30

Similar Documents

Publication Publication Date Title
CN102803880B (en) Hydrocarbon gas processing
KR101660082B1 (en) Hydrocarbon gas processing
CN102596361B (en) Hydrocarbon gas processing
CN102317725B (en) Hydrocarbon gas processing
US8881549B2 (en) Hydrocarbon gas processing
CN102575898A (en) Hydrocarbon gas processing
CN102460049B (en) Hydrocarbon gas processing
CN102695934B (en) Appropriate hydrocarbon gas process
CN102472573B (en) Hydrocarbon gas processing
CN102549366B (en) Hydrocarbon gas processing
CN102803881B (en) Appropriate hydrocarbon gas process
KR101758394B1 (en) Hydrocarbon gas processing
CN102483299B (en) Appropriate hydrocarbon gas process
CN102510987B (en) Hydrocarbon gas processing
CN102472574B (en) Hydrocarbon gas processing
KR20120139655A (en) Hydrocarbon gas processing
EP2553364A1 (en) Hydrocarbon gas processing

Legal Events

Date Code Title Description
C06 Publication
PB01 Publication
C10 Entry into substantive examination
SE01 Entry into force of request for substantive examination
C14 Grant of patent or utility model
GR01 Patent grant
TR01 Transfer of patent right

Effective date of registration: 20200109

Address after: Illinois, USA

Patentee after: UOP LLC

Address before: Texas, USA

Co-patentee before: SME PRODUCTS L.P.

Patentee before: Ortloff Engeneers Ltd.

TR01 Transfer of patent right