CN102483299B - Appropriate hydrocarbon gas process - Google Patents

Appropriate hydrocarbon gas process Download PDF

Info

Publication number
CN102483299B
CN102483299B CN201080025489.8A CN201080025489A CN102483299B CN 102483299 B CN102483299 B CN 102483299B CN 201080025489 A CN201080025489 A CN 201080025489A CN 102483299 B CN102483299 B CN 102483299B
Authority
CN
China
Prior art keywords
stream
heat transfer
mass transfer
transfer apparatus
process equipment
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.)
Active
Application number
CN201080025489.8A
Other languages
Chinese (zh)
Other versions
CN102483299A (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
Priority claimed from US12/717,394 external-priority patent/US9080811B2/en
Priority claimed from US12/750,862 external-priority patent/US8881549B2/en
Priority claimed from US12/772,472 external-priority patent/US9933207B2/en
Application filed by Ortloff Engineers Ltd filed Critical Ortloff Engineers Ltd
Priority claimed from US12/781,259 external-priority patent/US9939195B2/en
Publication of CN102483299A publication Critical patent/CN102483299A/en
Application granted granted Critical
Publication of CN102483299B publication Critical patent/CN102483299B/en
Active legal-status Critical Current
Anticipated expiration legal-status Critical

Links

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
    • 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
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/0204—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the feed stream
    • F25J3/0219—Refinery gas, cracking gas, coke oven gas, gaseous mixtures containing aliphatic unsaturated CnHm or gaseous mixtures of undefined nature
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
    • F25J3/0233—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of CnHm with 1 carbon atom or more
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
    • F25J3/0238—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of CnHm with 2 carbon atoms or more
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/0295—Start-up or control of the process; Details of the apparatus used, e.g. sieve plates, packings
    • 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
    • F25J2200/30—Processes or apparatus using separation by rectification using a side column in a single pressure 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
    • F25J2200/78—Refluxing the column with a liquid stream originating from an upstream or downstream fractionator column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/80—Processes or apparatus using separation by rectification using integrated mass and heat exchange, i.e. non-adiabatic rectification in a reflux exchanger or dephlegmator
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • 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
    • F25J2210/12—Refinery or petrochemical off-gas
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • 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.

Landscapes

  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Chemical & Material Sciences (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Separation By Low-Temperature Treatments (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
  • Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)

Abstract

Disclose technique and the device for reclaiming heavy hydrocarbon component in compact process equipment from hydrocarbon stream.By air-flow cooling, condensation, and expand into lower pressure, and be supplied to the absorption plant of described process equipment inside as charging.From described absorption plant, collect distillate stream, and be directed at heat transfer and the mass transfer apparatus of described process equipment inside, with its volatile component of stripping while cooling blast.From heat transfer and mass transfer apparatus, collect distillation stream and be cooled to be enough to its condensation at least in part, thus forming the stream of residual vapor stream and condensation.The quantity of described charging and temperature are in certain temperature, reclaim the major part of required component in described steam stripped distillate stream thus.

Description

Appropriate hydrocarbon gas process
Technical field
The present invention relates to the technique for separating of gas containing hydrocarbon and device.Applicant according to the U.S. Provisional Application the 61/186th compiled the 119th article of (e) money according to United States code the 35th and require to submit on June 11st, 2009, the rights and interests of No. 361.Applicant compiles according to according to United States code the 35th rights and interests that the 120th article also requires the part continuation application as following application: in the U.S. Patent application No.12/772 that on May 3rd, 2010 submits to, 472, in the U.S. Patent application No.12/750 that on March 31st, 2010 submits to, 862, in the U.S. Patent application No.12/717 that on March 4th, 2010 submits to, 394, in the U.S. Patent application No.12/689 that on January 19th, 2010 submits to, 616 and on February 17th, 2009 submit to U.S. Patent application No.12/372,604.Assignee S.M.E.Products LP and Ortloff Engineers, Ltd. are the both sides of joint study agreement, and this joint study agreement came into force before the invention of the application is made.
Can from multiple gases recovered ethylene, ethane, propylene, propane and/or heavy hydrocarbon, these gases are as natural gas, refinery gas and the synthesis air-flow that obtained by other hydrocarbon material (as coal, crude oil, naphtha, oil shale, Tar sands and brown coal).Natural gas has methane and the ethane of larger proportion usually, and namely for methane and ethane account at least 50 % by mole of natural gas altogether.Natural gas is also containing relatively a small amount of heavy hydrocarbon (as propane, butane, pentane etc.) and hydrogen, nitrogen, carbon dioxide and other gas.
Relate generally to of the present invention is recovered ethylene, ethane, propylene, propane and heavy hydrocarbon from this air-flow.Carry out canonical analysis to the air-flow that will process by the present invention, the result of approx. molar percentage is the methane of 90.3%, the ethane of 4.0% and other C 2component, 1.7% propane and other C 3component, the iso-butane of 0.3%, the normal butane of 0.5% and 0.8% pentane and above hydrocarbon, remaining person is made up of nitrogen and carbon dioxide.Sometimes also there is sulfurous gas.
Background technology
The price cyclic fluctuation in history of natural gas and natural gas liquids (NGL) both compositions thereof makes ethane, ethene, propane, propylene and heavy constituent reduce as the increment of fluid product sometimes.This oneself through causing for can be these products and provide the technique of more high-recovery, for providing the technique of high efficiente callback rate compared with Low investment cost and for the needs that can easily adapt to or regulate to change the technique of the specific components rate of recovery on a large scale.Existing technique for separating of these materials comprises based on the cooling of gas and refrigeration, oil absorbs and refrigeration oil absorbs technique.In addition, owing to expanding and produce the validity reason of idle reduction devices of power obtain heat from process gas while, low temperature process is being popularized.According to the rich degree (ethane, ethene and heavy hydrocarbons content) of bleed pressure, gas and the situation of required final products, the process integration of each or they in these techniques can be taked.
Low-temperature expansion technique is for being generally preferred at present natural gas liquids recovery, because this technique can provide maximum simplicity, be easy to start, flexible operation, efficiency is good, safety and reliability is 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) 33,408 announced again; And co-pending application 11/430,412; 11/839,693; 11/971,491; With 12/206,230 describe relevant technique (although description of the invention is being based on the process conditions different from described in the United States Patent (USP) quoted in some cases).
In typical low-temperature expansion recovery process, feed stream is under stress by carrying out heat exchange with other process stream and/or external refrigeration source (as propane compression refrigeration system) and be cooled.Along with gas is cooled, liquid can be condensed, and as the C needed for some 2the highly pressurised liquid of+component is collected in one or more separator.According to rich degree and the situation of the amount of liquid formed of gas, highly pressurised liquid can be made to expand into lower pressure and fractionation.The gasification occurred during expansion of liquids causes the further cooling of stream.In some cases, in order to reduce the temperature coming from expansion further, pre-cooled highly pressurised liquid is desirable before inflation.The expanded stream comprising the mixture of liquid and steam is fractionated in distillation (demethanation device or deethanization device) tower.In tower, distillation expand cooling stream using by residual methane, nitrogen and other escaping gas as overhead vapours with as C needed for bottoms liquid product 2component, C 3component is separated with heavy hydrocarbon component, or by residual methane, C 2component, nitrogen and other escaping gas are as overhead vapours and C needed for bottoms liquid product 3component is separated with heavy hydrocarbon component.
If feed gas does not have total condensation (being generally do not have total condensation), then steam remaining from partial condensation can be divided into two streams.Make a part of steam reach lower pressure by work expansion machine or engine or expansion valve, under described lower pressure, due to the further cooling of stream, more liquid is condensed.Pressure after expansion is substantially identical with the operating pressure of destilling tower.The vapor-liquid produced by expanding is merged and is supplied to tower as charging.
The remainder of steam is cooled to by carrying out heat exchange and condensation substantially with other process stream (such as cold fractionator overhead cut).Some or all of highly pressurised liquids can vapor portion merging therewith before cooling.Then by suitable expansion gear (as expansion valve) by the cooled stream that obtains expand into the operating pressure of demethanation device.Between the phase of expansion, a part of liquid will gasify, and cause the cooling of total stream.Then the stream of rapid expanding is supplied to demethanation device as its top feed.Usually, merge as residual methane gas product in the vapor portion of rapid expanding stream and the Upper separator section of demethanation device overhead vapours in fractionating column.Or, can to cool and the stream expanded is supplied to separator to provide steam and liquid stream.Steam and overhead fraction are merged, and liquid is supplied to tower as top drum charging.
In the ideal operation of this separating technology, the residual gas leaving technique contains methane substantially all in feed gas, and there is no heavy hydrocarbon component, the bottom fraction leaving demethanation device contains substantially all heavy hydrocarbon components, and there is no methane or the larger component of volatility.But in practice, because the demethanation device of routine operates mainly as stripper, desirable situation can not be reached.Therefore the methane product of technique generally includes the steam of the top fractionation level section leaving tower, together with the steam not standing any rectification step.C 3and C 4+ component generation considerable damage, because overhead-liquid charging contains these components and the heavy hydrocarbon component of a great deal of, causes the C of corresponding aequum in steam 3component, C 4component and heavy hydrocarbon component leave the top fractionation level section of demethanation device.If the steam of rising and the C that can absorb quite in a large number in steam can be made 3component, C 4component contacts with the liquid (backflow) of heavy hydrocarbon component, then can reduce the loss of component needed for these widely.
In recent years, preferred hydrocarbon separating technology adopts top absorption plant section to provide the additional rectifying of rising steam.It is a kind of that to produce the method for reflux stream to upper rectifying section be utilize sideing stream of the steam that rises on the bottom of tower.Because the C of higher concentration in steam 2component is lower in tower, and a large amount of liquid can condensation and do not raise its pressure in this side draw stream, is typically used only in the refrigeration be suitable in the cold steam leaving upper rectifying section.Mainly then this condensed fluid of liquid methane and ethane can be used to absorb C from the steam risen by upper rectifying section 3component, C 4component and heavy hydrocarbon component, and thus be captured in these from the valuable component in the bottoms liquid product of demethanation device.U.S. Patent No. 7,191,617 is an example of this type of technique.
Description of the prior art
Fig. 1 is that display adopts according to U.S. Patent No. 7, and the prior art of 191,617 reclaims C from natural gas 2the process chart for the treatment of plant's design of+component.In the simulation of this technique, inlet gas enters factory as stream 31 under 110 °F [43 DEG C] 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 by carrying out suitable pretreatment (not shown) to feed gas.In addition, usually dewater to prevent from forming hydrate (ice) under cryogenic to incoming flow.Solid drier is normally used for this object.
Incoming flow 31 is split into stream 32 and 33 two parts.Stream 32 is cooled to-32 °F [-36 DEG C] by carrying out heat exchange with cold residual gas stream 50a in heat exchanger 10, and stream 33 is cooled to-18 °F [-28 DEG C] by carrying out heat exchange with the demethanation device reboiler liquid (stream 43) of 50 °F [10 DEG C] and the tower side reboiler liquid (stream 42) of-36 °F [-38 DEG C] in a heat exchanger 11 simultaneously.Stream 32a and 33a remerges and forms stream 31a, and it enters separator 12 under-28 °F [-33 DEG C] and 893psia [6,155kPa (a)], and steam (stream 34) is separated with condensate liquid (stream 35) at this place.Separator liquid (stream 35) is expand into operating pressure (about 401psia [2 of fractionating column 18 by expansion valve 17,765kPa (a)]), thus before bottom tower intermediate feed point is supplied to fractionating column 18, stream 35a is cooled to-52 °F [-46 DEG C] at it.
Steam (stream 34) from separator 12 is split into stream 38 and 39 two streams.The stream 38 of the total steam containing about 32%, to pass through heat exchanger 13 with the mode of cold residual gas stream 50 in heat exchange relationship, is cooled to condensation substantially at this place.Then by expansion valve 14 by the operating pressure of the stream 38a rapid expanding of the condensation substantially of obtained-130 °F [-90 DEG C] to fractionating column 18.Between the phase of expansion, a part of stream gasification, causes the cooling of total stream.In the technique shown in Fig. 1, the expanded stream 38b leaving expansion valve 14 reaches the temperature of-140 °F [-96 DEG C], and is supplied to fractionating column 18 at upper column intermediate feed point.
Residue 68% steam (stream 39) from separator 12 enters work expansion machine 15, obtains mechanical energy wherein by this part high pressure charging.Steam is expand into tower operating pressure to constant entropy by machine 15 substantially, and being expanded by acting is cooled to the temperature of approximately-94 °F [-70 DEG C] by expanded stream 39a.Typical commercially available decompressor can obtain the general 80-85% of the merit that can obtain from desirable constant entropy expansion in theory.The merit obtained is often used for driving centrifugal compressor (as device 16), and described centrifugal compressor such as can be used for recompressing the distillation steam stream (stream 50b) be heated.After this expanded stream 39a of partial condensation is supplied to fractionating column 18 as charging at bottom tower intermediate feed point.
Demethanation device in tower 18 is conventional destilling tower, its include multiple be spaced vertically column plate, one or more packed bed or column plate and filler certain combine.As usual situation in natural gas processing plant, fractionating column can be formed by two sections: top absorbs (rectifying) section 18a, it comprises column plate and/or filler, contact with to the necessity between the cold liquid declined to the expanded stream 38b risen and the vapor portion of 39a to provide, thus condensation absorb C 2component, C 3component and heavy constituent; With bottom stripping (demethanation) section 18b, it comprises column plate and/or filler, contacts with column plate and/or filler to provide the cold liquid to declining to the necessity between the steam risen.Demethanation section 18b also comprises reboiler (reboiler as previously described and tower side reboiler), it heats a part for the liquid flowed downward along tower and is gasified to provide stripping steam, the fluid product (stream 44) that described stripping steam upwards flows with stripping methane and light component along tower.Mass ratio according to methane in bottom product and ethane is the typical specification of 0.010: 1, and fluid product stream 44 leaves at the bottom of tower under 74 °F [23 DEG C].
A part (stream 45) for distillation steam is extracted out from the upper area of stripping section 18b.Then this stream is cooled to-134 °F [-92 DEG C] and partial condensation (stream 45a) by carrying out heat exchange with the cold demethanation device top stream 41 leaving demethanation device 18 with-139 °F [-95 DEG C] from-109 °F [-78 DEG C] at heat exchanger 20.Cold demethanation device top stream is along with it makes the cooling at least partially of stream 45 and condensation and be slightly warming up to-134 °F [-92 DEG C] (stream 41a).
Operating pressure (398psia [2,748kPa (a)]) in reflux splitter 21 is maintained the operating pressure a little less than demethanation device 18.This provide and cause distillation steam stream 45 to flow through heat exchanger 20, and from then on flow into the driving force of reflux splitter 21, wherein condensate liquid (stream 47) is separated with any uncooled steam (stream 46).Then stream 46 merges with the demethanation device top stream 41a of the intensification carrying out automatic heat-exchanger 20, to form the cold residual gas stream 50 of-134 °F [-92 DEG C].
Liquid stream 47 from reflux splitter 21 is drawn into operating pressure a little more than demethanation device 18 by pump 22, then stream 47a is supplied to demethanation device 18 as cold top drum charging (backflow).The C that this cold liquid backflow absorbs and condensation is risen from the upper rectification region of the absorber portion 18a of demethanation device 18 3component and heavy constituent.
Form the distillation steam stream (stream 41) of overhead fraction to heat up in heat exchanger 20, at this moment it as discussed previouslyly provides cooling to distilling stream 45, then merges with stream 46 and forms cold residual gas stream 50.Residual gas and the feed gas stream of coming in are upstream by heat exchanger 13,-46 °F [-44 DEG C] (stream 50a) is heated at this place, and by heat exchanger 10, be heated to 102 °F of [39 DEG C] (stream 50b) at this place, at this moment it as discussed previouslyly provides cooling.Then two stage recompression residual gas are divided.First stage drives compressor 16 by decompressor 15.Second stage drives compressor 23 by supplementing power source, and residual gas (stream 50d) is compressed to sales line pressure by described compressor 23.Be cooled to 110 °F [43 DEG C] in drain cooler 24 after, residual gas stream 50e is being enough to meet the 915psia [6,307kPa (a)] of pipeline requirements (usually general is inlet pressure) downstream to sales gas pipeline.
The stream flow velocity of technique shown in Fig. 1 and gathering of energy ezpenditure is provided in following table:
Table I
(Fig. 1)
Summary of the invention
The present invention adopts new device more effectively to implement above steps, and uses the number of packages of equipment less.This is achieved in the following ways, and is combined in the middle of common framework by up to the present single device product, thus reduces ground block space needed for treatment plant and reduce the cost of investment of facility.Surprisingly, applicant finds, and compacter layout also greatly reduces the power consumption realized needed for given recovery levels, thus improves process efficiency and reduce the running cost of facility.In addition, for most of pipeline of the individual equipment product that interconnects during compacter layout it also avoid and needs conventional plant to design, reduce further cost of investment, and avoid the flange pipe connection needing to be correlated with.Because pipe flange is that (it is facilitate greenhouse gases and also may be the VOC that atmospheric ozone forms precursor for potential hydrocarbon, VOC) source of leaks, avoids using these flanges can reduce the potential hazard of the atmospheric emission of welding.
The C that can obtain more than 99% is had been found that according to the present invention 3and C 4+ the rate of recovery, and without the need to demethanation device pumping reflux stream and at C 2the free of losses of component recovery aspect.The invention provides by C 2the C more than 99% can be maintained when the rate of recovery of component is regulated to low value by high level 3and C 4another advantage of+component recovery.In addition, compared with prior art, the present invention can make methane (or C with lower energy requirement 2component) and light component and C 2component (or C 3component) realize 100% be separated substantially with heavy constituent, keep identical recovery levels simultaneously.Although the present invention can be applicable to lower pressure and comparatively warm temperature, but when under the condition requiring-50 °F [-46 DEG C] or colder NGL recovery tower overhead fraction temperature, process feeds gas is at 400 to 1500psia [2,758 to 10,342kPa (a)] or higher scope in time be particularly advantageous.
Invention describes
Fig. 2 illustrates the flow chart according to present invention process.Identical with Fig. 1 of the feed gas composition considered in the technique that Fig. 2 provides and condition.Therefore, Fig. 2 technique and Fig. 1 technique can be compared advantage of the present invention is described.
In the simulation of Fig. 2 technique, inlet gas enters described device as stream 31 and is split into stream 32 and 33 two parts.Part I is stream 32, enters the heat-exchange device in the upper area of the charging cooling section 118a of process equipment 118 inside.This heat-exchange device can comprise the heat transfer unit (HTU) that blade adds tube type heat exchanger, heat-exchangers of the plate type, soldering aluminium profiles heat exchanger or other type, comprises multichannel and/or multioperation heat exchanger.Configuration heat-exchange device with provide the passage flowing through described heat-exchange device stream 32 and from the heat exchange between the residual gas stream the condensation segment 118b of process equipment 118 inside, heated in the heat-exchange device of described process equipment 118 in the lower area of charging cooling section 118a.Stream 32 is cooled while adding thermal distillation vapor stream further, and stream 32a leaves described heat-exchange device with-30 °F [-35 DEG C].
Part II is stream 33, enters the heat transfer in the stripping section 118e of process equipment 118 inside and mass transfer apparatus.This heat transfer and mass transfer apparatus also can comprise the heat transfer unit (HTU) that blade adds tube type heat exchanger, heat-exchangers of the plate type, soldering aluminium profiles heat exchanger or other type, comprise multichannel and/or multioperation heat exchanger.Configuration heat transfer and mass transfer apparatus are to provide the heat exchange between the stream 33 flowing through a described heat transfer and mass transfer apparatus passage and the distillate stream flowed downward from the absorber portion 118d of process equipment 118 inside, stream 33 is cooled, heat distillate stream simultaneously, before it leaves heat transfer and mass transfer apparatus, stream 33a is cooled to-42 °F [-41 DEG C].Along with distillate stream is heated, one partial gasification forms stripping steam, and described stripping steam continues to flow downward by heat transfer and mass transfer apparatus to rising along with remaining liq.To there is provided between stripping steam with distillate stream continuous contacts for heat transfer and mass transfer apparatus, and therefore it also plays the effect of the mass transfer provided between vapor phase and liquid phase, the fluid product stream 44 of stripping methane and light component.
Stream 32a and 33a remerges and forms stream 31a, it is at-34 °F [-37 DEG C] and 900psia [6,203kPa (a)] under enter the separator section 118f of process equipment 118 inside, so steam (stream 34) is separated with condensate liquid (stream 35).Separator section 118f has inner head or other device itself and stripping section 118e to be separated, and in process equipment 118 two sections can be operated at various pressures.
Stream 36 and 39 and stream 37 and 40 two streams are split into separately respectively from the steam (stream 34) of separator section 118f and liquid (stream 35).Stream 36 containing about 31% total steam merges with the stream 37 containing about 50% total steam, and the stream 38 of merging enters the heat-exchange device in the lower area of the charging cooling section 118a in process equipment 118.This heat-exchange device can comprise the heat transfer unit (HTU) that blade adds tube type heat exchanger, heat-exchangers of the plate type, soldering aluminium profiles heat exchanger or other type equally, comprises multichannel and/or multioperation heat exchanger.Configuration heat-exchange device with provide the passage flowing through described heat-exchange device stream 38 and from condensation segment 118b residual gas stream between heat exchange, make stream 38 heating residual gas stream while be cooled to condensation substantially.
Then by expansion valve 14 by the operating pressure (about 402psia [2,772kPa (a)]) of the stream 38a rapid expanding of the condensation substantially of obtained-128 °F [-89 DEG C] to the rectifying section 118c (absorption plant) in process equipment 118 and absorber portion 118d (another absorption plant).Between the phase of expansion, a part of stream may gasify, and causes the cooling of total stream.In the technique shown in Fig. 2, the expanded stream 38b leaving expansion valve 14 reaches the temperature of-139 °F [-95 DEG C], and is provided to the process equipment 118 between rectifying section 118c and absorber portion 118d.
Residue 69% steam (stream 39) from separator section 118f enters work expansion machine 15, obtains mechanical energy wherein by this part high pressure charging.Steam is expand into constant entropy the operating pressure of absorber portion 118d by machine 15 substantially, and being expanded by acting is cooled to the temperature of approximately-100 °F [-73 DEG C] by expanded stream 39a.After this expanded stream 39a of partial condensation is supplied to the lower area of the absorber portion 118d in process equipment 118 as charging, with the liquid comes into contact of upper area being supplied to absorber portion 118d.Expand into the operating pressure of the stripping section 118e in process equipment 118 by residue 50% liquid (stream 40) of expansion valve 17 self-separation device in future section 118f, thus stream 40a is cooled to-60 °F [-51 DEG C].Heat transfer in stripping section 118e and mass transfer apparatus are configured in upper and lower, make the heat transfer in inflation fluid stream 40a and mass transfer apparatus to be incorporated into the stripping section 118e between these two parts.
A part (the first distillation steam stream 45) for distillation steam is extracted out with-95 °F [-71 DEG C] from the upper area of stripping section 118e, and is directed at the heat-exchange device in the condensation segment 118b in process equipment 118.This heat-exchange device can comprise the heat transfer unit (HTU) that blade adds tube type heat exchanger, heat-exchangers of the plate type, soldering aluminium profiles heat exchanger or other type equally, comprises multichannel and/or multioperation heat exchanger.Configuration heat-exchange device, with the heat exchange between the after-fractionating steam stream providing the stream 45 of the passage flowing through described heat-exchange device and rise from the rectifying section 118c of process equipment 118 inside, makes after-fractionating steam stream be heated while cooling first distillation steam stream 45.Stream 45 is cooled to-134 °F [-92 DEG C] and condensation at least partly, and after this leaves heat-exchange device and be separated into its corresponding vapor phase and liquid phase.Vapor phase (if any) merges with the after-fractionating steam stream be heated leaving heat-exchange device, to be formed in the residual gas stream providing cooling in charging cooling section 118a, as discussed previously.Liquid phase (stream 48) is supplied to the upper area of the rectifying section 118c in process equipment 118 by gravity current as cold top drum charging (backflow).
Rectifying section 118c and absorber portion 118d respectively comprises by the following absorption plant formed: multiple be spaced vertically column plate, one or more packed bed or column plate and filler certain combination.Column plate in rectifying section 118c and absorber portion 118d and/or filler provide the steam to rising to contact with to the necessity between the cold liquid declined.The liquid part of expanded stream 39a mixes to the liquid declined with from absorber portion 118d, and the liquid of merging continues to enter into downwards in the middle of stripping section 118e.The stripping steam risen from stripping section 118e and the vapor portion of expanded stream 39a merge, and rise through absorber portion 118d with to the cold liquid comes into contact declined, thus from these steams condensation and absorb most C 2component, C 3component and heavy constituent.Any vapor portion of the steam risen from absorber portion 118d and expanded stream 38b merges, and rises through rectifying section 118c to contact with to the cold liquid declined (stream 48), thus from these steams condensation and absorb remaining most C 3component and heavy constituent.The liquid part of expanded stream 38b mixes to the liquid declined with from rectifying section 118c, and the liquid of merging continues to enter into downwards in the middle of absorber portion 118d.
The distillate that flows downward from the heat transfer the stripping section 118e in process equipment 118 and mass transfer apparatus is methane and light component by stripping.The fluid product (stream 44) obtained leaves the lower area of stripping section 118e and leaves process equipment 118 with 74 °F [23 DEG C].The after-fractionating steam stream risen from rectifying section 118c heats up in condensation segment 118b, and at this moment it provides cooling to stream 45, as discussed previously.The after-fractionating steam stream heated up merges with any steam be separated with the first distillation steam stream 45 of cooling, as discussed previously.The residual gas stream obtained heats in charging cooling section 118a, and at this moment it provides cooling to stream 32 and 38, as discussed previously, and residual gas stream 50 leaves process equipment 118 with 104 °F [40 DEG C].Then divide two stage recompression residual gas streams, namely drive compressor 16 by decompressor 15, and drive compressor 23 by supplementary power source.Be cooled to 110 °F [43 DEG C] in drain cooler 24 after, residual gas stream 50c is being enough to meet the 915psia [6,307kPa (a)] of pipeline requirements (usually general is inlet pressure) downstream to sales gas pipeline.
The stream flow velocity of technique shown in Fig. 2 and gathering of energy ezpenditure is provided in following table:
Table II
(Fig. 2)
The comparison display of Table I and II, compared with prior art, the present invention maintains substantially the same ethane recovery (85.00% of 85.03% pair of prior art), propane recovery is increased to 99.16% slightly from 99.11%, and maintains substantially the same butane+rate of recovery (99.99% of 99.98% pair of prior art).But further comparison sheet I and Table II display, realize the power that product yield uses and greatly reduce 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 improvement than Fig. 1 technique of prior art more than 5%.
By the improvement of the organic efficiency of Fig. 1 technique compared with prior art provided by the invention mainly due to two factors.First, in process equipment 118, heat-exchange device in charging cooling section 118a and condensation segment 118b and heat transfer and the compact Layout of mass transfer apparatus in stripping section 118e eliminate the pressure drop applied by the interconnecting piping seen in conventional treatment factory.Result is, under the residual gas flowing to compressor 16 is in higher pressure compared to existing technologies, under making the residual gas entering compressor 23 be in significantly higher pressure, thus decrease the present invention and residual gas is returned to power needed for pipeline pressure.
Second, in stripping section 118e, use heat transfer and mass transfer apparatus side by side to heat the distillate leaving absorber portion 118d, make obtained steam energy contact liq and its volatile component of stripping, this is more efficient with the conventional distil-lation tower of outside reboiler than use simultaneously.Volatile component by continuously from liquid stripping out, decrease the concentration of volatile component in stripping steam quickly, thus improve steam stripping efficiency of the present invention.
Compared with prior art, the present invention also to provide two other advantages except process efficiency except improving.First, the compact Layout of present invention process equipment 118 replaces eight independent device product (heat exchangers 10,11,13 and 20 in Fig. 1 of the prior art with single device product (process equipment 118 in Fig. 2); Separator 12; Reflux splitter 21; Reflux pump 22; And fractionating column 18).Which reduce plot space requirement and eliminate Interconnecting conduit, and avoiding the power consumption of reflux pump, compared with prior art decreasing treatment plant and utilize cost of investment of the present invention and running cost.The second, get rid of Interconnecting conduit and mean that the Flange joint utilizing treatment plant of the present invention to have is far fewer than prior art, decreases source of leaks number potential in factory.Hydrocarbon is VOC (VOC), and some of them are listed in greenhouse gases, and some of them may be the precursors forming atmospheric ozone, this means that the present invention can reduce the potential hazard of the atmospheric emission of energy welding.
Other embodiment
As in the early time to the description of the embodiment of the present invention shown in Fig. 2, the first distillation steam stream 45 by partly condensation, and the condensate obtained for from rise through process equipment 118 rectifying section 118c steam in absorb valuable C 3component and heavy constituent.But, the present invention is not limited thereto embodiment.Such as, maybe advantageously, when other design is considered to show that the part of steam or condensate should walk around rectifying section 118c and/or the absorber portion 118d of process equipment 118, only process a part for these steam by this way, or only a part for condensate is used as absorbent.May tend to the whole condensation in condensation segment 118b of the first distillation steam stream 45 under certain situation, but not partial condensation.May tend to the first distillation steam stream 45 under certain situation is side stream from whole steams of stripping section 118e, but not partial vapor sides stream.Should also be noted that the composition according to feed stream, may favourablely be use external refrigeration to provide part to cool to the first distillation steam stream 45 in condensation segment 118b.
When feed gas is poorer, the amount of the liquid be separated in stream 35 can be small enough to not need to arrange other mass-transfer zone in the stripping section 118e of between expanded stream 39a and expanded stream 40a (as shown in Fig. 2,4,6 and 8).In this case, the heat transfer in stripping section 118e and mass transfer apparatus can be configured to single section, expanded stream 40a be guided to above described heat transfer and mass transfer apparatus, as Fig. 3,5, shown in 7 and 9.May tend under certain situation expanded stream 40a and expanded stream 39a is merged, after this stream of merging is supplied to the lower area of absorber portion 118d as single charging.Whole liquid stream 35 may be tended under certain situation to be directly supplied to stripping section 118e via stream 40, or whole liquid stream 35 is merged via stream 37 and stream 36.In the previous case, without flowing in stream 37 (as shown in the dotted line in Fig. 2 to 9), only flow to stream 38 from the steam in the stream 36 of separator section 118f (Fig. 2 to 5) or separator 12 (Fig. 6 to 9).In the case of the latter, for stream 40 (as expansion valve 17), do not need expansion valve (as shown in the dotted line in Fig. 3,5,7 and 9).
In some cases, maybe advantageously use external separator container to be separated the incoming flow 31a of cooling, instead of comprise the separator section 118f in process equipment 118.As shown in Fig. 6 to 9, can use separator 12 that the incoming flow 31a of cooling is separated into steam stream 34 and liquid stream 35.
May tend under certain situation use the Part II (the stream 33a in Fig. 2 to 9) of cooling to replace the Part I (stream 36) of steam stream 34, to form stream 38, described stream 38 flow to the heat-exchange device in the lower area of charging cooling section 118a.In this case, only have the Part I of cooling (stream 32a) to be provided to separator section 118f (Fig. 2 to 5) or separator 12 (Fig. 6 to 9), and all obtained steam stream 34 is provided to work expansion machine 15.
According to the situation of the heavy hydrocarbon amount in feed gas and feed gas pressure, the incoming flow 31a entering the cooling of the separator section 118f in Fig. 3 and 5 or the separator 12 in Fig. 7 and 9 may not contain any liquid (because it is higher than its dew point, or because it is higher than its cricondenbar).In this case, stream 35 and 37 (shown in dotted line), therefore only have in stream 36 and flow to stream 38 from the steam (Fig. 7 and 9) from separator 12 in the steam (Fig. 3 and 5) of separator section 118f or stream 36, become the stream 38b of the condensation substantially of expansion, be supplied to the process equipment 118 between rectifying section 118c and absorber portion 118d.In this case, the separator section 118f in process equipment 118 (Fig. 3 and 5) or separator 12 (Fig. 7 and 9) can not be needed.
Feed gas condition, plant layout, existing equipment or other factors can show, without work expansion machine 15 or with the expansion gear (as expansion valve) substituted, to carry out replacing be feasible.Although be describe independent stream to expand in specific expansion gear, alternative expansion gear can be used in the appropriate case.Such as, condition can permit that the acting of the part (stream 38a) of the condensation substantially of incoming flow is expanded.
According to the present invention, can take to utilize external refrigeration to supplement the cooling to inlet gas that can be obtained by distillation steam and liquid stream, particularly when rich inlet gas.In this case, heat transfer and mass transfer apparatus can be included in separator section 118f (or in gas collector, when the incoming flow 31a when cooling is not containing liquid), as shown in the dotted line of Fig. 2 to 5, heat transfer and mass transfer apparatus can be included in separator 12, as shown in the dotted line in Fig. 6 to 9.This heat transfer and mass transfer apparatus can comprise the heat transfer unit (HTU) that blade adds tube type heat exchanger, heat-exchangers of the plate type, soldering aluminium profiles heat exchanger or other type, comprise multichannel and/or multioperation heat exchanger.Configuration heat transfer and mass transfer apparatus, in order to provide the freezing stream of the passage flowing through described heat transfer and mass transfer apparatus (such as, propane) and the vapor portion of stream 31a upwards flowed between heat exchange, make cold-producing medium cooled vapor the more liquid of condensation further, these liquid to decline to become the partially liq removed in stream 35.Or, before stream 31a enters separator section 118f (Fig. 2 to 5) or separator 12 (Fig. 6 to 9), conventional gas cooler can be used, with refrigerant cools stream 32a, stream 33a and/or stream 31a.
According to the C that will reclaim in the temperature of feed gas and Fu Du and fluid product stream 44 2the situation of group component, may can not get enough heating by stream 33 and meet product specification to make the liquid leaving stripping section 118e.In this case, the heat transfer in stripping section 118e and mass transfer apparatus can comprise supply, to provide supplementary heating with heat medium, as shown in the dotted line in Fig. 2 to 9.Or, other heat transfer and mass transfer apparatus can being comprised in the lower area of stripping section 118e, for providing supplementary heating, or can heat it with heat medium before heat transfer stream 33 is supplied in stripping section 118e and mass transfer apparatus.
According to the heat transfer unit (HTU) type cases selecting the heat-exchange device be used in the region, upper and lower of charging cooling section 118a and/or condensation segment 118b, likely these heat-exchange devices are combined in single multichannel and/or multioperation heat transfer unit (HTU).In this case, in order to complete required cooling and heating, multichannel and/or multioperation heat transfer unit (HTU) will comprise for the appropriate device of distributing, being separated with collecting stream 32, stream 38, stream 45 and any steam be separated with the stream 45 of cooling and after-fractionating steam stream.
May tend under certain situation provide other mass transfer in the upper area of stripping section 118e.In this case, above the heat transfer that mass transfer apparatus can be arranged in below lower area part that expanded stream 39a enters absorber portion 118d and the Part II 33a of cooling leaves stripping section 118e and mass transfer apparatus part.
The less preferred selection of the embodiment of Fig. 2 to 5 of the present invention is to provide the separator flask of the Part I 32a for cooling, the separator flask of Part II 33a for cooling, be incorporated in the steam stream that is wherein separated to form steam stream 34, and be incorporated in the liquid stream that is wherein separated to form liquid stream 35.Another less preferred selection of the present invention is cooled stream 37 (instead of merging stream 37 and stream 36 to be formed the stream 38 of merging) in the independent heat-exchange device in charging cooling section 118a, expand the stream cooled in independent expansion gear, and the stream of expansion is supplied to the zone line in absorber portion 118d.
In some cases, particularly as low-level C 2component recovery, by being taken, maybe advantageously provides backflow to the upper area of stripping section 118e.In this case, the liquid phase leaving the stream 45 of the cooling of heat-exchange device in condensation segment 118b can be divided into stream 48 and stream 49 two parts.Stream 48 is supplied to rectifying section 118c as its its top feed, stream 49 is supplied to the upper area of stripping section 118e simultaneously, make it before extraction first distillation steam stream 45, partly condensation can be carried out to the distillation steam in this section of process equipment 118.In some cases, the gravity current of stream 48 and 49 may be enough (Fig. 2,3,6 and 7), and needs in other cases to aspirate liquid phase (stream 47) (Fig. 4,5,8 and 9) with reflux pump 22.The relative quantity of the liquid phase be separated between stream 48 and 49 will depend on a number of factors, and comprise air pressure, feed gas composition, required C 2component recovery levels and available horsepower amount.When not assessing the concrete condition of embody rule of the present invention, usually optimal separation can not be estimated.Whole liquid phase may be tended under certain situation to be supplied to rectifying section 118c as its top feed with stream 48, and be not supplied to the upper area of stripping section 118e with stream 49, stream 49 is shown in dotted line.
Recognize, the relative quantity seeing the charging in each tributary of vapor feed separately depends on a number of factors, the amount of the heat comprise gas pressure, feed gas forms, can extracted economically from charging and available horsepower amount.Above absorber portion 118d, more charging can improve the rate of recovery, reduces the power reclaimed from expander simultaneously, thus adds the horsepower requirements of recompression.The charging increased below absorber portion 118d reduces horsepower consumption, but also can reduce product recovery rate.
By the utility consumption amount needed for technological operation, the invention provides the C of improvement 2component, C 3component and heavy hydrocarbon component or C 3the recovery of component and heavy hydrocarbon component.The form of expression of the improvement of technological operation required drive consumption indicators can reduce for compression or the power requirement recompressed, the power requirement of external refrigeration reduces, the power requirement that energy requirement reduces, tower boils again of supplementary heating reduces or their combination.
Although described believed as the preferred embodiment of the invention, but one of ordinary skill in the art would recognize that, when not departing from by essence of the present invention defined by the following claims, other and further amendment can be carried out to the present invention, such as, make the present invention be applicable to different condition, feed type or other requirement.
Accompanying drawing explanation
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 U.S. Patent No. 7, the flow chart of the natural gas processing plant of the prior art of 191,617;
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 the present patent application to the replacement device of natural gas flow.
Detailed description of the invention
In explanation below to above-mentioned figure, provide the summary sheet to the flow velocity that representative processes condition calculates.For convenience's sake, in the table occurred in this article, flow speed value (mol/hr) has been rounded up to immediate integer.The total flow rate be shown in table comprises all non-hydrocarbon components, is therefore usually greater than the summation of hydrocarbon component stream flow velocity.Indication temperature is rounded up to the approximation closest to the number of degrees.It should also be noted that as the technique described in comparative drawings figs and the process design and calculation of carrying out is based on such supposition, the heat leak namely not from environment to technique or from technique to environment.The quality of commercially available isolated material makes this become very reasonably to suppose, and normally those skilled in the art can make.
For convenience's sake, with traditional either English units with both recording process parameters of the International System of Units (SI).Mole flow velocity provided in table can be interpreted as pound-mol/hour or kilogram mol/hr.Be recorded as horsepower (HP) and/or thousand British thermal units/hour (MBTU/Hr) energy ezpenditure correspond to described by pound-mol/hour in units of mole flow velocity.Be recorded as kilowatt energy ezpenditure of (kW) correspond to described by kg-moles/hour in units of mole flow velocity.

Claims (34)

1. one kind will containing methane, C 2component, C 3component becomes the technique of the cut that volatile residual gas cut and volatility are relatively little with the flow separation of heavy hydrocarbon component, and the cut that described volatility is relatively little contains described C 2component, C 3component and heavy hydrocarbon component or described C 3the major part of component and heavy hydrocarbon component, wherein
(1) described airflow diversion is become the first and second parts;
(2) described Part I is cooled;
(3) described Part II is cooled;
(4) Part II of the Part I of described cooling and described cooling is merged to form the air-flow cooled;
(5) airflow diversion of described cooling is become the first and second streams;
(6) cool described first stream with by its all condensation substantially, and after this expand into lower pressure, thus it is cooled further;
(7) supply the first stream of described cooling of expanding as the charging between first and second absorption plant arranged in process equipment, described first absorption plant is positioned at above described second absorption plant;
(8) described second stream is expand into described in lower pressure, and be supplied to described second absorption plant as bottom feed;
(9) from the lower area of described second absorption plant, distillate stream is collected, and heat in the heat transfer be arranged in described process equipment and mass transfer apparatus, thus the cooling at least partially in step (3) is provided, the component that simultaneously strip volatile is larger from described distillate stream, and to be after this heated described and steam stripped distillate stream discharges from described process equipment as the cut that described volatility is relatively little;
(10) from the upper area of described heat transfer and mass transfer apparatus, the first distillation steam stream is collected, and be cooled to be enough to its condensation at least partially, thus form condensate stream and the residual vapor stream containing remaining any uncooled steam after described first distillation steam stream cooling;
(11) described first absorption plant is supplied to as its top feed at least partially using described condensate stream;
(12) from the upper area of described first absorption plant, collect after-fractionating steam stream and heat;
(13) the described after-fractionating steam stream that is heated and any described residual vapor stream are merged, to form the steam stream of merging;
(14) heat the steam stream of described merging, the steam stream after this merged from being heated described in described process equipment discharge is as described volatile residual gas cut;
(15) in the described heating being arranged at the steam stream completing described after-fractionating steam stream and described merging in the one or more heat-exchange devices in described process equipment, thus the cooling at least partially in step (2), (6) and (10) is provided; With
(16) make effectively the temperature of the described upper area of described first absorption plant to be remained on certain temperature to the quantity of the described incoming flow of described first and second absorption plants and temperature, reclaim the major part of the component in the relatively little cut of described volatility thus.
2. technique according to claim 1, wherein
A the Part II of the Part I of described cooling and described cooling merges with the air-flow of forming section condensation by ();
B the air-flow of described partial condensation is supplied to separator by (), and be separated wherein, thus obtains steam stream and at least one liquid stream;
C () is by the first and second streams described in described steam diverting flow one-tenth; With
D () expand into lower pressure at least partially by described at least one liquid stream, and to be supplied in below described second absorption plant and the described process equipment be positioned at above described heat transfer and mass transfer apparatus as charging.
3. technique according to claim 2, wherein
A () merges described first stream and described at least one liquid stream the stream forming merging at least partially;
After this b stream that () cools described merging with by its all condensation substantially, and expand into lower pressure, it is cooled further thus;
C () supplies the merging stream of described cooling of expanding as the charging between first and second described absorption plant;
(d) any remainder of described at least one liquid stream is expand into described in lower pressure, and to be supplied in below described second absorption plant and the described process equipment be positioned at above described heat transfer and mass transfer apparatus as described charging; With
E () is being arranged at the described heating of the steam stream completing described after-fractionating steam stream and described merging in the one or more heat-exchange devices in described process equipment, thus provide the cooling at least partially in step (2), (10) and (b).
4. technique according to claim 2, wherein said separator is arranged in described process equipment.
5. technique according to claim 3, wherein said separator is arranged in described process equipment.
6. technique according to claim 2, wherein
(1) described heat transfer and mass transfer apparatus are arranged in region, upper and lower; And
(2) between the described top entering into described heat transfer and mass transfer apparatus at least partially described process equipment being supplied to the described expansion of described at least one liquid stream and lower area.
7. technique according to claim 3, wherein
(1) described heat transfer and mass transfer apparatus are arranged in region, upper and lower; And
(2) between the described top that any remainder described process equipment being supplied to the described expansion of described at least one liquid stream enters into described heat transfer and mass transfer apparatus and lower area.
8. technique according to claim 4, wherein
(1) described heat transfer and mass transfer apparatus are arranged in region, upper and lower; And
(2) between the described top entering into described heat transfer and mass transfer apparatus at least partially described process equipment being supplied to the described expansion of described at least one liquid stream and lower area.
9. technique according to claim 5, wherein
(1) described heat transfer and mass transfer apparatus are arranged in region, upper and lower; And
(2) between the described top that any remainder described process equipment being supplied to the described expansion of described at least one liquid stream enters into described heat transfer and mass transfer apparatus and lower area.
10. technique according to claim 1, wherein
(1) gas collector is arranged in described process equipment;
(2) establish other heat transfer and mass transfer apparatus in described gas collector, described other heat transfer and mass transfer apparatus comprise one or more path for external refrigeration medium;
(3) air-flow of described cooling is supplied to described gas collector, and is directed at described other heat transfer and mass transfer apparatus to be cooled further by described external refrigeration medium; And
(4) airflow diversion of described further cooling is become described first and second streams.
11. techniques according to claim 2,3,4,5,6,7,8 or 9, wherein
(1) establish other heat transfer and mass transfer apparatus in described separator, described other heat transfer and mass transfer apparatus comprise one or more path for external refrigeration medium;
(2) by described steam conductance to described other heat transfer and mass transfer apparatus to be cooled by described external refrigeration medium, thus form other condensate; And
(3) described other condensate becomes a part for the described at least one liquid stream be separated wherein.
12. techniques according to claim 1,2,3,4,5,6,7,8,9 or 10, wherein
(1) stream of described condensation is split at least the first and second reflux stream;
(2) described first reflux stream is supplied to described first absorption plant as described its top feed; And
(3) described second reflux stream to be supplied in below described second absorption plant and the described process equipment be positioned at above described heat transfer and mass transfer apparatus as charging.
13. techniques according to claim 11, wherein
(1) stream of described condensation is split at least the first and second reflux stream;
(2) described first reflux stream is supplied to described first absorption plant as described its top feed; And
(3) described second reflux stream to be supplied in below described second absorption plant and the described process equipment be positioned at above described heat transfer and mass transfer apparatus as charging.
14. techniques according to claim 1,2,3,4,5,6,7,8,9 or 10, wherein said heat transfer and mass transfer apparatus comprise one or more path for external heating medium, to supplement the heating that provided by described Part II, for the larger component of described volatility from the described stripping described distillate stream.
15. techniques according to claim 11, wherein said heat transfer and mass transfer apparatus comprise one or more path for external heating medium, to supplement the heating that provided by described Part II, for the larger component of described volatility from the described stripping described distillate stream.
16. techniques according to claim 12, wherein said heat transfer and mass transfer apparatus comprise one or more path for external heating medium, to supplement the heating that provided by described Part II, for the larger component of described volatility from the described stripping described distillate stream.
17. techniques according to claim 13, wherein said heat transfer and mass transfer apparatus comprise one or more path for external heating medium, to supplement the heating that provided by described Part II, for the larger component of described volatility from the described stripping described distillate stream.
18. 1 kinds for will containing methane, C 2component, C 3component becomes the device of the cut that volatile residual gas cut and volatility are relatively little with the flow separation of heavy hydrocarbon component, and the cut that described volatility is relatively little contains described C 2component, C 3component and heavy hydrocarbon component or described C 3the major part of component and heavy hydrocarbon component, comprises
(1) first part flow arrangement, described airflow diversion is become the first and second parts by it;
(2) heat-exchange device, it to be arranged in process equipment and to be connected to described first part flow arrangement to receive described Part I and to be cooled;
(3) heat transfer and mass transfer apparatus, it to be arranged in described process equipment and to be connected to described first part flow arrangement to receive described Part II and to be cooled;
(4) first combined units, it is connected to described heat-exchange device and described heat transfer and mass transfer apparatus, in order to the Part I and described cooling that receive described cooling Part II and form the air-flow of cooling;
(5) second part flow arrangements, it is connected to described first combined unit to receive the air-flow of described cooling and to be split into the first and second streams;
(6) described heat-exchange device is connected to described second part flow arrangement further, in order to receive described first stream and to be cooled to be enough to substantially by its condensation;
(7) first expansion gears, it is connected to described heat-exchange device with the first stream of condensation substantially described in receiving and is expand into lower pressure;
(8) first and second absorption plants, described first and second absorption plants are arranged in described process equipment, and be connected to described first expansion gear, in order to receive the first stream of described cooling of expanding as to the charging between first and second absorption plant described, described first absorption plant is positioned at above described second absorption plant;
(9) second expansion gears, it is connected to described second part flow arrangement, in order to receive described second stream and pressure lower described in being expand into, described second expansion gear is connected to described second absorption plant further to provide the second stream of described expansion as the bottom feed to it;
(10) fluid collection device, it to be arranged in described process equipment and to be connected to described second absorption plant, in order to receive the distillate stream from the lower area of described second absorption plant;
(11) described heat transfer and mass transfer apparatus are connected to described fluid collection device further to receive described distillate stream and to be heated, thus the cooling at least partially in step (3) is provided, the component that simultaneously strip volatile is larger from described distillate stream, and to be after this heated described and steam stripped distillate stream discharges from described process equipment as the cut that described volatility is relatively little;
(12) first vapor collection devices, it to be arranged in described process equipment and to be connected to described heat transfer and mass transfer apparatus, in order to receive the first distillation steam stream of the upper area from described heat transfer and mass transfer apparatus;
(13) described heat-exchange device is connected to described first vapor collection device further, in order to receive described first distillation steam stream and to be cooled to be enough to its condensation at least partially, thus form condensate stream and the residual vapor stream containing remaining any uncooled steam after described first distillation steam stream cooling;
(14) described first absorption plant is connected to described heat-exchange device further, in order to receive described condensate stream at least partially as its top feed to it;
(15) second vapor collection devices, it to be arranged in described process equipment and to be connected to described first absorption plant to receive the after-fractionating steam stream from the upper area of described first absorption plant;
(16) described heat-exchange device is connected to described second vapor collection device further to receive described after-fractionating steam stream and to be heated, thus provides the cooling at least partially in step (13);
(17) second combined units, it is connected to described heat-exchange device, in order to the steam stream of the after-fractionating steam stream that is heated described in receiving and any described remnants, and forms the steam stream merged;
(18) described heat-exchange device is connected to described second combined unit further, in order to receive the steam stream of described merging and to be heated, thus the cooling at least partially in step (2) and (6) is provided, and after this described steam stream merged that is heated is discharged from described process equipment as described volatile residual gas cut; With
(19) control device, it is adapted to regulate the quantity to the described incoming flow of described first and second absorption plants and temperature, remain on certain temperature with the temperature of the described upper area by described first absorption plant, reclaim the major part of the component in the relatively little cut of described volatility thus.
19. devices according to claim 18, wherein
A () described first combined unit is applicable to receive the Part I of described cooling and the Part II of described cooling and the air-flow of forming section condensation;
B () separator is connected to described first combined unit, in order to receive the air-flow of described partial condensation and to be isolated into steam stream and at least one liquid stream;
C () described second part flow arrangement is connected to described separator to receive described steam stream and to be split into the first and second described streams; With
(d) the 3rd expansion gear be connected to described separator, in order to receive described at least one liquid stream at least partially and pressure lower described in being expand into, described 3rd expansion gear is connected to described process equipment further, using supply the described expansion of described at least one liquid stream at least partially as the charging of the top to the below of described second absorption plant and described heat transfer and mass transfer apparatus.
20. devices according to claim 19, wherein
(a) the 3rd combined unit be connected to described second part flow arrangement and described separator, in order to receive described first stream and described at least one liquid stream at least partially and form the stream merged;
B () described heat-exchange device is connected to described 3rd combined unit further, in order to receive the stream of described merging and to be cooled to be enough to substantially by its condensation;
C () described first expansion gear is connected to described heat-exchange device with the merging stream of condensation substantially described in receiving and is expand into lower pressure;
D the first and second absorption plants described in () are connected to described first expansion gear, in order to receive the merging stream of described cooling of expanding as to the described charging between first and second absorption plant described;
E () described 3rd expansion gear is connected to described separator, in order to receive any remainder of described at least one liquid stream and pressure lower described in being expand into, described 3rd expansion gear is connected to described process equipment further, the described charging using any remainder supplying the described expansion of described at least one liquid stream as the top to the below of described second absorption plant and described heat transfer and mass transfer apparatus; With
F () described heat-exchange device is connected to described second combined unit further, in order to receive the steam stream of described merging and to be heated, thus provide the cooling at least partially in step (2) and (b).
21. devices according to claim 19, wherein said separator is arranged in described process equipment.
22. devices according to claim 20, wherein said separator is arranged in described process equipment.
23. devices according to claim 19, wherein
(1) described heat transfer and mass transfer apparatus are arranged in region, upper and lower; And
(2) described process equipment is connected to described 3rd expansion gear, in order to receive the described expansion of described at least one liquid stream at least partially, and guides it between the described top and lower area of described heat transfer and mass transfer apparatus.
24. devices according to claim 20, wherein
(1) described heat transfer and mass transfer apparatus are arranged in region, upper and lower; And
(2) described process equipment is connected to described 3rd expansion gear, in order to receive any remainder of the described expansion of described at least one liquid stream, and guides it between the described top and lower area of described heat transfer and mass transfer apparatus.
25. devices according to claim 21, wherein
(1) described heat transfer and mass transfer apparatus are arranged in region, upper and lower; And
(2) described process equipment is connected to described 3rd expansion gear, in order to receive the described expansion of described at least one liquid stream at least partially, and guides it between the described top and lower area of described heat transfer and mass transfer apparatus.
26. devices according to claim 22, wherein
(1) described heat transfer and mass transfer apparatus are arranged in region, upper and lower; And
(2) described process equipment is connected to described 3rd expansion gear, in order to receive any remainder of the described expansion of described at least one liquid stream, and guides it between the described top and lower area of described heat transfer and mass transfer apparatus.
27. devices according to claim 18, wherein
(1) gas collector is arranged in described process equipment;
(2) establish other heat transfer and mass transfer apparatus in described gas collector, described other heat transfer and mass transfer apparatus comprise one or more path for external refrigeration medium;
(3) described gas collector is connected to described first combined unit to receive the air-flow of described cooling, and is directed at described other heat transfer and mass transfer apparatus to be cooled further by described external refrigeration medium; And
(4) described second part flow arrangement is adapted to the air-flow being connected to receive described further cooling with described gas collector, and is split into described first and second streams.
28. devices according to claim 19,20,21,22,23,24,25 or 26, wherein
(1) establish other heat transfer and mass transfer apparatus in described separator, described other heat transfer and mass transfer apparatus comprise one or more path for external refrigeration medium;
(2) by described steam conductance to described other heat transfer and mass transfer apparatus to be cooled by described external refrigeration medium, thus form other condensate; And
(3) described other condensate becomes a part for the described at least one liquid stream be separated wherein.
29. devices according to claim 18,19,20,21,22,23,24,25,26 or 27, wherein
(1) the 3rd part flow arrangement is connected to described heat-exchange device, in order to receive the stream of described condensation and to be split at least the first and second reflux stream;
(2) described first absorption plant is adapted to be connected with described 3rd part flow arrangement, in order to receive described first reflux stream as the described its top feed to it; And
(3) described heat transfer and mass transfer apparatus are adapted to be connected with described 3rd part flow arrangement, in order to receive described second reflux stream as its top feed to it.
30. devices according to claim 28, wherein
(1) the 3rd part flow arrangement is connected to described heat-exchange device, in order to receive the stream of described condensation and to be split at least the first and second reflux stream;
(2) described first absorption plant is adapted to be connected with described 3rd part flow arrangement, in order to receive described first reflux stream as the described its top feed to it; And
(3) described heat transfer and mass transfer apparatus are adapted to be connected with described 3rd part flow arrangement, in order to receive described second reflux stream as its top feed to it.
31. devices according to claim 18,19,20,21,22,23,24,25,26 or 27, wherein said heat transfer and mass transfer apparatus comprise one or more path for external heating medium, to supplement the heating that provided by described Part II, for the larger component of described volatility from the described stripping described distillate stream.
32. devices according to claim 28, wherein said heat transfer and mass transfer apparatus comprise one or more path for external heating medium, to supplement the heating that provided by described Part II, for the larger component of described volatility from the described stripping described distillate stream.
33. devices according to claim 29, wherein said heat transfer and mass transfer apparatus comprise one or more path for external heating medium, to supplement the heating that provided by described Part II, for the larger component of described volatility from the described stripping described distillate stream.
34. devices according to claim 30, wherein said heat transfer and mass transfer apparatus comprise one or more path for external heating medium, to supplement the heating that provided by described Part II, for the larger component of described volatility from the described stripping described distillate stream.
CN201080025489.8A 2009-06-11 2010-05-17 Appropriate hydrocarbon gas process Active CN102483299B (en)

Applications Claiming Priority (13)

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
US12/717,394 US9080811B2 (en) 2009-02-17 2010-03-04 Hydrocarbon gas processing
US12/717,394 2010-03-04
US12/750,862 US8881549B2 (en) 2009-02-17 2010-03-31 Hydrocarbon gas processing
US12/750,862 2010-03-31
US12/772,472 2010-05-03
US12/772,472 US9933207B2 (en) 2009-02-17 2010-05-03 Hydrocarbon gas processing
US12/781,259 US9939195B2 (en) 2009-02-17 2010-05-17 Hydrocarbon gas processing including a single equipment item processing assembly
PCT/US2010/035121 WO2010144217A1 (en) 2009-06-11 2010-05-17 Hydrocarbon gas processing
US12/781,259 2010-05-17

Publications (2)

Publication Number Publication Date
CN102483299A CN102483299A (en) 2012-05-30
CN102483299B true CN102483299B (en) 2015-10-21

Family

ID=56291174

Family Applications (1)

Application Number Title Priority Date Filing Date
CN201080025489.8A Active CN102483299B (en) 2009-06-11 2010-05-17 Appropriate hydrocarbon gas process

Country Status (14)

Country Link
EP (1) EP2440869A1 (en)
JP (1) JP5753535B2 (en)
KR (1) KR101687851B1 (en)
CN (1) CN102483299B (en)
AR (1) AR077079A1 (en)
AU (1) AU2010259129A1 (en)
BR (1) BRPI1011526A2 (en)
CA (1) CA2764144C (en)
CO (1) CO6480935A2 (en)
EA (1) EA027815B1 (en)
MX (1) MX355018B (en)
MY (1) MY158312A (en)
PE (1) PE20121305A1 (en)
WO (1) WO2010144217A1 (en)

Families Citing this family (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EA023919B1 (en) * 2010-03-31 2016-07-29 Ортлофф Инджинирс, Лтд. Hydrocarbon gas processing
EP3044528A1 (en) * 2013-09-11 2016-07-20 Ortloff Engineers, Ltd 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
US6516631B1 (en) * 2001-08-10 2003-02-11 Mark A. Trebble Hydrocarbon gas processing
CN1969160A (en) * 2003-02-25 2007-05-23 奥特洛夫工程有限公司 Hydrocarbon gas processing

Family Cites Families (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS546500B1 (en) * 1976-02-15 1979-03-29
US4889545A (en) * 1988-11-21 1989-12-26 Elcor Corporation Hydrocarbon gas processing
AU9491401A (en) * 2000-10-02 2002-04-15 Elcor Corp Hydrocarbon gas processing
UA76750C2 (en) * 2001-06-08 2006-09-15 Елккорп Method for liquefying natural gas (versions)
US6560989B1 (en) * 2002-06-07 2003-05-13 Air Products And Chemicals, Inc. Separation of hydrogen-hydrocarbon gas mixtures using closed-loop gas expander refrigeration
US7159417B2 (en) * 2004-03-18 2007-01-09 Abb Lummus Global, Inc. Hydrocarbon recovery process utilizing enhanced reflux streams
MXPA06011644A (en) * 2004-04-26 2007-01-23 Ortloff Engineers Ltd Natural gas liquefaction.
US8919148B2 (en) * 2007-10-18 2014-12-30 Ortloff Engineers, Ltd. Hydrocarbon gas processing

Patent 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
US6516631B1 (en) * 2001-08-10 2003-02-11 Mark A. Trebble Hydrocarbon gas processing
CN1969160A (en) * 2003-02-25 2007-05-23 奥特洛夫工程有限公司 Hydrocarbon gas processing

Also Published As

Publication number Publication date
KR101687851B1 (en) 2016-12-19
EA027815B1 (en) 2017-09-29
AU2010259129A9 (en) 2014-12-18
MX355018B (en) 2018-04-02
PE20121305A1 (en) 2012-10-08
CO6480935A2 (en) 2012-07-16
JP5753535B2 (en) 2015-07-22
AU2010259129A2 (en) 2012-05-03
KR20120027488A (en) 2012-03-21
EA201270005A1 (en) 2012-06-29
AR077079A1 (en) 2011-07-27
AU2010259129A1 (en) 2012-02-23
EP2440869A1 (en) 2012-04-18
CN102483299A (en) 2012-05-30
JP2012529623A (en) 2012-11-22
BRPI1011526A2 (en) 2016-03-29
WO2010144217A1 (en) 2010-12-16
MX2011013068A (en) 2012-02-01
CA2764144C (en) 2017-10-24
CA2764144A1 (en) 2010-12-16
MY158312A (en) 2016-09-30

Similar Documents

Publication Publication Date Title
CN102803880B (en) Hydrocarbon gas processing
CN102741634B (en) Hydrocarbon gas processing
CN102317725B (en) Hydrocarbon gas processing
CN102596361B (en) Hydrocarbon gas processing
TWI477595B (en) Hydrocarbon gas processing
CN102460049B (en) Hydrocarbon gas processing
CN105531552A (en) Hydrocarbon gas processing
CN102549366B (en) Hydrocarbon gas processing
CN102695934B (en) Appropriate hydrocarbon gas process
CN102472573B (en) Hydrocarbon gas processing
CN102483299B (en) Appropriate hydrocarbon gas process
CN102803881B (en) Appropriate hydrocarbon gas process
KR101758394B1 (en) Hydrocarbon gas processing
CN102510987B (en) Hydrocarbon gas processing
KR101676069B1 (en) Hydrocarbon gas processing
KR101714101B1 (en) Hydrocarbon gas processing
CN102472574B (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: 20200110

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