CN103351896B - Method and device for removing water and heavy hydrocarbons from shale gas - Google Patents

Method and device for removing water and heavy hydrocarbons from shale gas Download PDF

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CN103351896B
CN103351896B CN201310224727.3A CN201310224727A CN103351896B CN 103351896 B CN103351896 B CN 103351896B CN 201310224727 A CN201310224727 A CN 201310224727A CN 103351896 B CN103351896 B CN 103351896B
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gas
heat exchanger
heavy hydrocarbon
tower
plate
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CN103351896A (en
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何振勇
宣永根
徐化周
李伟
刘学强
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Xindi Energy Engineering Technology Co Ltd
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Xindi Energy Engineering Technology Co Ltd
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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/0204—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
    • F25J3/0228—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
    • F25J3/0242—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of CnHm with 3 carbon atoms or more
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
    • F25J3/0247—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 4 carbon atoms or more
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • 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
    • F25J2200/04—Processes or apparatus using separation by rectification in a dual pressure main column system
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/70—Refluxing the column with a condensed part of the feed stream, i.e. fractionator top is stripped or self-rectified
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • 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
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/02—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum
    • F25J2205/04—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum in the feed line, i.e. upstream of the fractionation step
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/60—Processes or apparatus using other separation and/or other processing means using adsorption on solid adsorbents, e.g. by temperature-swing adsorption [TSA] at the hot or cold end
    • F25J2205/66—Regenerating the adsorption vessel, e.g. kind of reactivation gas
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2215/00—Processes characterised by the type or other details of the product stream
    • F25J2215/04—Recovery of liquid products
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2215/00—Processes characterised by the type or other details of the product stream
    • F25J2215/64—Propane or propylene
    • 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
    • F25J2220/00—Processes or apparatus involving steps for the removal of impurities
    • F25J2220/60—Separating impurities from natural gas, e.g. mercury, cyclic hydrocarbons
    • F25J2220/68—Separating water or hydrates
    • 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
    • F25J2270/18—External refrigeration with incorporated cascade 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
    • F25J2270/66—Closed external refrigeration cycle with multi component refrigerant [MCR], e.g. mixture of hydrocarbons
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/90—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration
    • F25J2270/902—Details about the refrigeration cycle used, e.g. composition of refrigerant, arrangement of compressors or cascade, make up sources, use of reflux exchangers etc.

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  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Separation By Low-Temperature Treatments (AREA)

Abstract

The invention provides a method and a device for removing water and heavy hydrocarbons from shale gas. The method comprises two parts including a process for removing the water and a process for removing the heavy hydrocarbons and treatment of the heavy hydrocarbons. Through use of the method, the water and the heavy hydrocarbons in the shale gas can be removed, and the heavy hydrocarbons can be further separated into usable liquefied petroleum gas (LPG) and by-products, such as light oil. The method is economically feasible, and has advanced process routes. The atmospheric dew point of the shale gas after removal of the water and the heavy hydrocarbons is reduced to less than or equal to -76 DEG C, and the C6 heavy hydrocarbon component and heavy hydrocarbon components that are heavier than the C6 heavy hydrocarbon component are removed to make the shale reach a LNG-dissoluble level. A cold-hot fluid heat-transfer route is reasonable in design, can realize the reasonable matching of cold quantity and heat quantity of fluids, so that the energy consumption of the device is reduced as far as possible.

Description

A kind of de-heavy hydrocarbon method of shale gas dehydration and device
Technical field
The invention provides the de-heavy hydrocarbon method of a kind of shale gas dehydration and device, remove moisture and heavy hydrocarbon from moisture containing the shale gas of heavy hydrocarbon, also can by-product liquefied petroleum gas (LPG) and light oil byproduct.
Background technology
Shale gas is the natural gas exploiting out from rammell, specifically, is natural gas main body is present in absorption or free state in mud stone, high-carbon mud stone, shale and aleuritic texture rock class interlayer, can be created on the various stages of organic origin.World's shale gas stock number is 457 tcms, and suitable with conventional gas stock number, wherein shale gas technically recoverable resources is 187 tcms, and economic worth is huge, has very large development potentiality.At present, the exploitation of China's shale gas is in gas reservoir exploration and tentatively exploits pilot phase.By in April, 2012, China determines 33 shale gas Favorable Areas altogether, shale gas completion 58 mouthfuls, wherein horizontal well 15 mouthfuls.Along with shale gas exploration right is progressively open to the public, the shale gas exploitation of Future Ten year will be rapidly developed.But shale gas is as an emerging unconventional energy resource, its treatment technology is also relatively less, along with the exploitation of new forms of energy, also day by day increases the development requirement of the treatment technology of shale gas.Because the composition of shale gas changes greatly, the moisture of the shale gas of the difference exploitation point namely in zonule and heavy hydrocarbons content change greatly, make to utilize existing device to become difficulty to the operation that shale gas carries out purifying.In view of the composition difference between shale gas and common natural gas is large, adopt the processing method of existing common natural gas and device cannot obtain qualified natural gas from shale gas to process shale gas.
Chinese patent CN103031168A proposes a kind of dehydration of producing liquefied natural gas from the mist being rich in methane and takes off heavy hydrocarbon technique, technique described in this patent adopts the composite bed of the adsorbents such as molecular sieve, activated alumina and water-fast silica gel to remove water in methane-riched gas mixture and heavy hydrocarbon, adopt the isobaric adsorption process of three towers, adsorption tower regeneration gas takes from process gas.Adopt multiple-hearth adsorption process, heavy hydrocarbon can by partial removal, and the degree removed depends on load and the regeneration level of adsorbent.But only adopt adsorbent that the content of heavy hydrocarbon can not be made to be reduced to very low requirement, especially when the heavy hydrocarbon amount needing to remove is larger, Cold box blocking and freezing may be caused because heavy hydrocarbon cannot be removed to reasonable depth, therefore usually adopt the de-heavy hydrocarbon of absorption to coordinate the technology of cryogenic separation.
Chinese patent CN103031169A proposes the method and apparatus of a kind of natural gas liquefaction and heavy hydrocarbon process, adopts self condensate liquid to wash heavy hydrocarbon.The raw natural gas of normal temperature directly enters heavy hydrocarbon scrubbing tower, and the heavy hydrocarbon washings such as warp cryogenic separation goes out in natural gas C3, C4, in natural gas, the heavy hydrocarbon of C6 and more than C6 is able to deep removal.Because this technique relies on the heavy hydrocarbon condensate liquid washing heavy hydrocarbon of natural gas self, therefore can the heavy hydrocarbons content of natural gas self directly has influence on heavy hydrocarbon remove system and normally run.For ensureing that suitable heavy hydrocarbon condensing liquid quantity maintains the continued operation of scrubbing tower, the precooling temperature of temperature adjustment controlling measurement natural gas can be taked on stream to adjust natural gas condensates amount.In addition, when heavy hydrocarbon condensing liquid quantity is less, also can introduces the heavy hydrocarbon in isopentane washing natural gas, reach heavy hydrocarbon condensation and the object removed by the vapor liquid equilibrium changing system, but a certain amount of isopentane consumption can be caused.Because needs are for the in good time switching flow of heavy hydrocarbons content in unstripped gas, traditional heavy hydrocarbon washing process operation is comparatively loaded down with trivial details.
Summary of the invention
Therefore, the invention provides a kind of brand-new dehydration being applicable to shale gas and take off heavy hydrocarbon method and device, moisture in shale gas and heavy hydrocarbon are removed, and heavy hydrocarbon component is separated into available liquefied petroleum gas (LPG) and light oil byproduct further, economically feasible, process route are advanced; Shale gas dew points at normal pressure after the de-heavy hydrocarbon that dewaters is down to≤and-76 DEG C, the heavy hydrocarbon component of C6 and more than C6 is removed to the soluble degree of LNG.
According to a first aspect of the invention, provide the method for the de-heavy hydrocarbon of a kind of shale gas dehydration, comprise dehydration procedure and de-heavy hydrocarbon and heavy hydrocarbon treatment process two parts; Dehydration procedure comprises and adopts isobaric absorbing process flow process to remove moisture content in raw material shale gas, purification shale gas after the de-heavy hydrocarbon that dewaters is as the regeneration gas (that is, the purification shale gas in de-heavy hydrocarbon and heavy hydrocarbon separation circuit after the de-heavy hydrocarbon that dewaters is as regeneration gas) in dehydration procedure; Shale gas after de-heavy hydrocarbon and heavy hydrocarbon treatment process comprise dehydration removes heavy hydrocarbon successively after plate-fin heat exchanger cooling in heavy hydrocarbon separator and heavy hydrocarbon scrubbing tower, the heavy hydrocarbon be removed enters stripping removing light component wherein in dethanizer successively, wherein from the light component of dethanizer in lighter hydrocarbons heat exchanger isolated with heavy hydrocarbon scrubbing tower tower top remove the shale gas heat exchange of heavy hydrocarbon after enter heavy hydrocarbon scrubbing tower and be separated again, wherein enter in rectifying column from the heavy constituent of dethanizer and isolate light oil and gas phase, this gas phase is cooled into liquefied petroleum gas; With from the isolated de-heavy hydrocarbon shale gas of heavy hydrocarbon scrubbing tower tower top after the heat exchange of lighter hydrocarbons heat exchanger, in part Returning plate fin heat exchanger, liquefaction obtains liquefied natural gas and namely to dewater the shale gas after de-heavy hydrocarbon, goes dehydration procedure as regeneration gas in part Returning plate fin heat exchanger after heat exchange; Shale gas dew points at normal pressure after the de-heavy hydrocarbon of dehydration is down to≤and-76 DEG C, the heavy hydrocarbon component of C6 and more than C6 is removed to the soluble degree of LNG, such as≤150ppm, preferably≤100ppm, more preferably≤80ppm, more preferably≤50ppm.
Preferably, dehydration procedure adopts the isobaric absorbing process flow processs of two towers, utilizes one or more in activated alumina, 3A molecular sieve or 4A molecular sieve as adsorbent, the water adsorption in raw material shale gas is got off.
Preferably, emptying or send to gas distributing system after process further after the regeneration gas regeneration ending of dehydration procedure.
In a preferred embodiment, dehydration procedure adopts the isobaric absorbing process flow processs of two towers, utilizes one or more in activated alumina, 3A molecular sieve or 4A molecular sieve etc. as adsorbent, the water adsorption in raw material shale gas is got off.
In a preferred embodiment, the flow process of the isobaric absorbing process of two towers that adopts of dehydration procedure is as follows:
Isobaric absorbing process adopts parallel two towers pattern, and wherein tower T1 is in adsorption process and another tower T2 is in regenerative process.For adsorption tower T1, illustrate that the isobaric absorbing process flow process of two towers is as follows:
A, adsorption process: unstripped gas enters the adsorption tower T1 being in adsorbed state from adsorption tower T1 top through valve V1A.Under the adsorption selection of adsorbent, component to be removed wherein and moisture are absorbed, and at the bottom of tower, are not gone out system by the gas adsorbed through valve V4A.When being arrived bed outlet by the mass-transfer zone forward position of adsorbing contaminant (being called absorption forward position) and reserving section, turn off unstripped gas inlet valve V1A and the unstripped gas outlet valve V4A of this adsorption tower T1, stop absorption, adsorbent bed starts to proceed to regenerative process.
The regeneration of adsorption tower T1 comprise carry out successively heating, cold blowing process.
B, heating process: regeneration gas is heated to after uniform temperature (such as 230 ~ 250 DEG C) through regeneration gas heater E1, enter adsorption tower T1 to heat, reverse purging is adsorbent bed, absorption impurity is on the sorbent desorbed completely, the adsorbent in T1 is regenerated; Go out the regeneration gas of adsorption tower T1 successively through valve V2A, regeneration gas cooler E2, point flow container V1, send to gas distributing system after emptying or further process after cooling, separatory, heating process terminates.
C, cold blowing process: after heating process terminates, regeneration gas heater E1 stops heating, and regeneration gas enters the adsorption tower T1 being in cold blowing process, and reverse purging is adsorbent bed, makes bed be down to uniform temperature (such as about 40 DEG C); Go out the regeneration gas of adsorption tower T1 successively through valve V2A, regeneration gas cooler E2, point flow container V1, send to gas distributing system after emptying or further process after cooling, separatory, cold blowing process terminates.
After this process, adsorption tower T1 just completes complete " adsorption-regeneration " circulation, for absorption is got ready next time.The absorption of adsorption tower T2 and regenerative process identical with adsorption tower T1, realizing, two cone pulley flow operations by controlling the action of different valve, reaching the object of continuous purification gas.
Shale gas after dehydration enters de-heavy hydrocarbon and heavy hydrocarbon separation circuit, enters heavy hydrocarbon separator, C3 that heavy hydrocarbon separator bottom be separated after being cooled to-60 ~-80 DEG C (preferably-65 ~-75 DEG C) in plate-fin heat exchanger +heavy hydrocarbon component enters in dethanizer after returning plate-fin heat exchanger re-heat to normal temperature, reclaims C3 +the light component (C1, C2 hydrocarbon etc.) carried in heavy hydrocarbon component, the isolated gas phase in heavy hydrocarbon separator top enters heavy hydrocarbon scrubbing tower, in heavy hydrocarbon scrubbing tower with dethanizer top gas phase cooled logistics mass-and heat-transfer, finally at the bottom of heavy hydrocarbon scrubber overhead, tower, obtain the light components such as C1, C2 and C3 respectively +heavy hydrocarbon component, the C1 that heavy hydrocarbon scrubbing tower tower top obtains, the light component temperature such as C2 about-60 ~-80 DEG C, enter after gas phase heat exchange that lighter hydrocarbons heat exchanger and deethanization tower top separate reclaims cold, part returns plate-fin heat exchanger liquefaction becomes liquefied natural gas (LNG), part returns plate-fin heat exchanger re-heat to normal temperature, (wherein the heavy hydrocarbon component of C6 and more than C6 is removed to the soluble degree of LNG to be the shale gas after the de-heavy hydrocarbon of dehydration, such as≤150ppm, preferably≤100ppm, more preferably≤80ppm, more preferably≤50ppm), separating a road goes dehydration procedure as regeneration gas, optionally separating another road goes outside battery limit (BL), heavy hydrocarbon wash tower bottoms liquid phase is pressurized to 2.0MPaA ~ 4.0MPaA(preferably 2.2 ~ 3.8MPaA through heavy hydrocarbon pump, more preferably 2.5 ~ 3.5MPaA, preferred 2.8 ~ 3.2MPaA further), then enter dethanizer and remove light component (being mainly C1, C2 hydrocarbon etc.) wherein, the light component that dethanizer top separates enters lighter hydrocarbons heat exchanger and the heat exchange of heavy hydrocarbon scrubber overhead gas phase and is cooled to-60 ~-80 DEG C (preferably-62 ~-78 DEG C, more preferably-65 ~-75 DEG C, preferably-68 ~-72 DEG C further), enters heavy hydrocarbon scrubbing tower, at the bottom of dethanizer tower, liquid phase (is mainly C3, C4, C5, C6 +mixture) be decompressed to 0.5MPaA ~ 2.0MPaA(through first throttle device and be preferably 0.7 ~ 1.8MPaA, be more preferably 1.0 ~ 1.5MPaA) after enter in the middle part of rectifying column, obtain the mixture of the components such as C3, C4 from tower top through rectifying, partial reflux (access road separately established by rectifying column), part extraction, be liquefied petroleum gas (LPG) product, be separated at the bottom of tower and obtain C5, C6 +etc. the mixture of component, after light oil cooler is cooled to normal temperature, be light oil byproduct.
Cold needed for plate-fin heat exchanger by or provide primarily of refrigerant compression systems, refrigerant compression systems simultaneously for shale gas low temperature remove heavy hydrocarbon and purification shale gas liquefaction cold is provided; Described refrigerant compression systems adopts one-level or two-stage compression.
As a kind of concrete embodiment, coolant compressor adopts two-stage compression, by C1 ~ C5 and N 2in cold-producing mediums of one or more compositions enter the entrance of refrigerant compression systems, 0.6 ~ 1.8MPaA(preferably 0.8 ~ 1.6MPaA is compressed to through first paragraph, more preferably 1.0 ~ 1.4MPaA), enter first order cooler and be cooled to 30 DEG C ~ 45 DEG C (preferably 32 ~ 42 DEG C, more preferably 35 ~ 40 DEG C), enter first order gas-liquid separator again and carry out gas-liquid separation, the isolated gas in first order gas-liquid separator top continues the second segment entrance entering compressor, 1.2 ~ 5.4MPaA(preferably 1.5 ~ 5.0MPaA is compressed to through two sections, more preferably 2.0 ~ 4.5MPaA, preferred 2.5 ~ 4.0MPaA further), after the hot gas that the isolated liquid of first order gas-liquid separator bottom liquid phases end compresses outlet conduit with second segment after liquor pump pressurization converges, enter again in second-stage cooler and be cooled to 30 DEG C ~ 45 DEG C (preferably 32 ~ 42 DEG C, more preferably 35 ~ 40 DEG C), cooled cold-producing medium enters second level gas-liquid separator subsequently and carries out gas-liquid separation, the heat exchanger channels that bottom the top gas of second level gas-liquid separator and second level gas-liquid separator, isolated liquid enters plate-fin heat exchanger participates in heat exchange.
Preferably, first entered the liquid phase cryogen heat exchanger channels of plate-fin heat exchanger by the liquid of drawing bottom the gas-liquid separator of the second level, be chilled to about-30 DEG C ~-80 DEG C in advance wherein, after first cryogen throttling arrangement throttling to 0.2 ~ 0.8MPaA, enter cryogen separator;-135 DEG C ~-169 DEG C are cooled to by the gas phase cryogen heat exchanger channels of plate-fin heat exchanger by the vapor phase stream stock of the isolated cold-producing medium in gas-liquid separator top, the described second level, after second cryogen throttling arrangement throttling to 0.2 ~ 0.8MPaA, oppositely enter the other heat exchanger channels heat exchange of plate-fin heat exchanger again, provide cold for plate-fin heat exchanger and then turn back to coolant compressor first compression section.
Reboiler that is built-in, any pattern such as autoclave, heat siphon type is adopted at the bottom of the tower of dethanizer and rectifying column.
According to a second aspect of the invention, provide a kind of shale gas dehydration de-heavy hydrocarbon apparatus, its device comprises dewatering system and de-heavy hydrocarbon and heavy hydrocarbon treatment system;
Wherein
Dewatering system comprises: sorption drying device, a unstripped gas access road, a dehydrated feed gas exit passageway, a regeneration gas access road, a regeneration gas exit passageway;
De-heavy hydrocarbon and heavy hydrocarbon treatment system comprise: a heavy hydrocarbon separator, a heavy hydrocarbon scrubbing tower, a dethanizer, a rectifying column, a plate-fin heat exchanger, a lighter hydrocarbons heat exchanger, throttling arrangement, a light oil cooler and a heavy hydrocarbon pump;
Described plate-fin heat exchanger at least comprises following heat exchanger channels: the first heat exchanger channels, the second heat exchanger channels, the 3rd heat exchanger channels, the 4th heat exchanger channels and for providing the cryogen heat exchanger channels of cold for heat exchanger;
Described heavy hydrocarbon separator comprises a dehydrated feed gas access road, a heavy hydrocarbon exit passageway and a lighter hydrocarbons exit passageway;
Described heavy hydrocarbon scrubbing tower comprises a gas phase access road, a mixed phase access road, a gaseous phase outlet passage, a heavy hydrocarbon exit passageway;
Described dethanizer comprises the first liquid phase access road, second liquid phase access road, a gaseous phase outlet passage, a heavy hydrocarbon exit passageway;
Described rectifying column comprises a heavy hydrocarbon access road, a liquefied petroleum gas exit passageway, a light oil exit passageway;
Described lighter hydrocarbons heat exchanger at least comprises the first and second two heat exchanger channels; The arrival end of the first heat exchanger channels of lighter hydrocarbons heat exchanger and the gaseous phase outlet expanding channels of heavy hydrocarbon scrubbing tower, the port of export of the first heat exchanger channels of lighter hydrocarbons heat exchanger is divided into two-way, be connected with the arrival end of the first heat exchanger channels of described plate-fin heat exchanger and the arrival end of the second heat exchanger channels respectively, the arrival end of the second heat exchanger channels of lighter hydrocarbons heat exchanger and the gaseous phase outlet expanding channels of described dethanizer, the port of export of the second heat exchanger channels of lighter hydrocarbons heat exchanger is connected with the mixed phase access road of described heavy hydrocarbon scrubbing tower;
The port of export of the first heat exchanger channels of described plate-fin heat exchanger is divided into two-way, and a road connects the regeneration gas access road of dewatering system, and another road is gone outside battery limit (BL);
The port of export of the second heat exchanger channels of described plate-fin heat exchanger is connected to downstream pipe network (such as natural gas liquefaction system);
The arrival end of the 3rd heat exchanger channels of described plate-fin heat exchanger connects the dehydrated feed gas exit passageway of dewatering system, and the port of export connects the dehydrated feed gas access road of heavy hydrocarbon separator;
4th heat exchanger channels arrival end of plate-fin heat exchanger is connected with the heavy hydrocarbon exit passageway of heavy hydrocarbon separator; The port of export connects the second liquid phase access road of dethanizer,
The lighter hydrocarbons exit passageway of described heavy hydrocarbon separator is connected with the gas phase access road of heavy hydrocarbon scrubbing tower;
The heavy hydrocarbon exit passageway of described heavy hydrocarbon scrubbing tower is connected to the input of heavy hydrocarbon pump, and heavy hydrocarbon delivery side of pump connects the first liquid phase access road of dethanizer;
The heavy hydrocarbon exit passageway of described dethanizer is connected with the liquid phase access road of described rectifying column via a described throttling arrangement;
The liquefied petroleum gas exit passageway of described rectifying column is connected to liquefied petroleum gas product storage tank via an aftercooler; Light oil products storage tank is connected to after the light oil exit passageway connection light oil cooler of rectifying column.
The sorption drying device that dewatering system can adopt this area conventional, preferred isobaric sorption drying device, more preferably adopt the isobaric sorption drying device of two towers, preferably sorption drying device fills the adsorbent be selected from 3A or 4A molecular sieve, activated alumina further.Raw material shale gas, can by moisture removal to dew points at normal pressure≤-76 DEG C after described dewatering system dehydration.
As preferred embodiment, wherein sorption drying device comprises:
First drying tower (T1) and the second drying tower (T2), both the first drying tower and the second drying tower are alternately in dry run and regenerative process,
Regeneration gas heater (E1),
Gas-liquid separator (V1), and
Regeneration gas cooler (E2),
Each drying tower have one or two or multiple adsorbent bed,
The carrier pipe of raw material shale gas is divided into two branch roads i.e. the first branch road and the second branch road, first branch road, via the ingress pipe of first valve (V1A), the first drying tower (T1), the first drying tower (T1) and the 4th valve (V4A), then leads to de-heavy hydrocarbon and heavy hydrocarbon treatment system by the dehydrated feed gas exit passageway of dewatering system, second branch road, via the ingress pipe of the 5th valve (V1B), the second drying tower (T2), the second drying tower (T2) and the 8th valve (V4B), then leads to de-heavy hydrocarbon and heavy hydrocarbon treatment system by the dehydrated feed gas exit passageway of dewatering system, between first drying tower (T1) and the 4th valve (V4A), draw arm and draw arm between second drying tower (T2) and the 8th valve (V4B), these two arms converge via after the 3rd valve (V3A) and the 7th valve (V3B) one end being connected to regeneration gas heater (E1) respectively, and the other end of regeneration gas heater (E1) is connected to de-heavy hydrocarbon and heavy hydrocarbon treatment system by the regeneration gas access road of dewatering system, between first drying tower (T1) and first valve (V1A), draw arm and draw arm between second drying tower (T2) and the 5th valve (V1B), these two arms converge via after second valve (V2A) and the 6th valve (V2B) respectively, via the importing end of regeneration gas cooler (E2), regeneration gas cooler (E2), the derivation end of regeneration gas cooler (E2) is connected to the ingress pipe of gas-liquid separator (V1), the top delivery line of gas-liquid separator (V1) is connected to dewatering system regeneration gas exit passageway.
Generally, the carrying out of each process is controlled by means of each program-controlled valve.
Preferably, each adsorbent bed of each drying tower loads one or more adsorbents be selected from 3A or 4A molecular sieve, activated alumina independently.
As an embodiment, the gaseous phase outlet passage of described rectifying column is first via described aftercooler with optionally via a rectifier column reflux tank, then two arms are separated, an arm is connected with liquefied petroleum gas product storage tank, and another arm, optional via a pump, be connected to the liquid phase access road that rectifying column is separately established.
Here, the liquid phase access road that rectifying column is separately established refers to except the liquid phase access road be connected with a described throttling arrangement, the rectifier column reflux liquid phase access road of setting.
The reboiler of any pattern can be adopted, such as built-in, autoclave, thermosyphon reboiler at the bottom of the tower of described dethanizer and/or described rectifying column.
Connection can be designed according to actual process demand for providing the cryogen heat exchanger channels of cold for plate-fin heat exchanger.As a preferred embodiment, 2 are had for providing the cryogen heat exchanger channels of cold for plate-fin heat exchanger, i.e. the 5th, the 6th heat exchanger channels, the 5th heat exchanger channels one end of plate-fin heat exchanger connects the cryogen exit passageway connection of refrigeration compression system, the other end is connected via the first cryogen throttling arrangement one end with the 6th heat exchanger channels, and the other end of the 6th heat exchanger channels is connected to the cryogen access road of refrigeration compression system;
As another preferred embodiment, 3 are had for providing the cryogen heat exchanger channels of cold for plate-fin heat exchanger, i.e. the 5th, the 6th, the 7th heat exchanger channels, the arrival end of described 5th heat exchanger channels and the arrival end of the 7th heat exchanger channels are connected with the gas phase end of the second level gas-liquid separator in described refrigerant compression systems and liquid phase end respectively via two pipelines, and the port of export of the 6th heat exchanger channels is connected to the cryogen access road of the first compression section via pipeline; The port of export of the 7th heat exchanger channels of described plate-fin heat exchanger returns the 6th heat exchanger channels via after the first cryogen throttling arrangement throttling; The port of export of the 5th heat exchanger channels of described plate-fin heat exchanger is connected via the arrival end of the second cryogen throttling arrangement with the 6th heat exchanger channels.Such as, as cold C1 ~ C5 and N 2when the azeotrope of composition provides, liquid phase cryogen enters the 7th heat exchanger channels of plate-fin heat exchanger, is chilled to about-30 DEG C ~-80 DEG C in advance wherein, returns the 6th heat exchanger channels of plate-fin heat exchanger after first cryogen throttling arrangement throttling to 0.2 ~ 0.8MPaA; The 5th heat exchanger channels that gas phase cryogen enters plate-fin heat exchanger is cooled to-135 DEG C ~-169 DEG C, after second cryogen throttling arrangement throttling to 0.2 ~ 0.8MPaA, oppositely enter the 6th heat exchanger channels heat exchange of plate-fin heat exchanger again, return cryogen after re-heat to uniform temperature and system is provided.
Preferably, the cold needed for plate-fin heat exchanger by or provide primarily of mixed-refrigerant cycle, azeotrope, such as, by C1 ~ C5 and N 2composition, is selected from C1, C2, C3, C4 and C5 alkane and N usually 2in four kinds, five kinds or six kinds, they are according to arbitrary volume ratio or according to the mixing of approximately equivalent volume ratio, and hybrid refrigeration cycle is simultaneously for shale gas low temperature removes heavy hydrocarbon and the liquefaction of purification shale gas provides cold.
As preferred embodiment, the liquor pump that described refrigerant compression systems comprises two-period form mixed working fluid compressor, the first order cooler be connected with first paragraph and the second segment of described two-period form mixed working fluid compressor respectively and second-stage cooler, the first order gas-liquid separator be connected with described first order cooler and second-stage cooler respectively and second level gas-liquid separator and is connected with first order gas-liquid separator
Described plate-fin heat exchanger for providing the cryogen heat exchanger channels of cold to comprise the 5th heat exchanger channels, the 6th heat exchanger channels and the 7th heat exchanger channels for heat exchanger, the arrival end of described 5th heat exchanger channels and the arrival end of the 7th heat exchanger channels are connected with the gas phase end of the second level gas-liquid separator in described refrigerant compression systems and liquid phase end respectively via two pipelines, and the port of export of the 6th heat exchanger channels is connected to the cryogen access road of the first compression section via pipeline;
The port of export of the 5th heat exchanger channels of described plate-fin heat exchanger is connected via the arrival end of the second cryogen throttling arrangement with the 6th heat exchanger channels, and the port of export of the 7th heat exchanger channels of described plate-fin heat exchanger returns the 6th heat exchanger channels via after the first cryogen throttling arrangement throttling;
The gas phase end of the first order gas-liquid separator wherein in two gas-liquid separators is connected with the second compression section of two-period form mixed working fluid compressor, and the liquid phase end of first order gas-liquid separator is connected to second-stage cooler after converging via the outlet conduit of liquor pump and the second compression section.
Here, pressure unit MPaA is MPa, absolute pressure.
" adsorption dry " and " dry adsorb " are used interchangeably in this application.Term " optionally " expression is with or without.
The unstripped gas used refers to raw material shale gas.In this application, C1, C2, C3, C4, C5, C6 etc. represent the hydro carbons (or paraffinic) of corresponding carbon number respectively.C3 in the application +refer to the hydro carbons (or paraffinic) more than containing three and three carbon numbers." be mainly " in this application and refer to more than 50wt%, preferred more than 70wt%, or preferred more than 80wt%, more preferably more than 90wt%, such as more than 95wt% is made up of this component.Such as " be mainly C1, C2 hydrocarbon etc. " and refer to more than 50wt%, preferred more than 70wt%, or preferred more than 80wt%, more preferably more than 90wt%, such as more than 95wt% is made up of C1, C2 hydrocarbon; At the bottom of dethanizer tower, liquid phase is mainly C3, C4, C5, C6 +mixture refer to more than the 50wt% of liquid phase at the bottom of dethanizer tower, preferred more than 70wt%, or preferably more than 80wt%, more preferably more than 90wt%, such as more than 95wt% is by C3, C4, C5, C6 +mixture form.
Advantage of the present invention:
Moisture in shale gas and heavy hydrocarbon component remove by the method that 1, the present invention adopts, and heavy hydrocarbon component process are reclaimed, and obtain LPG and light oil byproduct, viable economically;
2, adopt two-tower process adsorption dewatering, comparatively three tower flow processs are simple, and save equipment investment;
3, by the isobaric absorbing process flow process of employing two tower, can by the moisture removal in shale gas to dew points at normal pressure≤-76 DEG C, preferably≤-78 DEG C, more preferably≤-80 DEG C;
4, compared to existing technology in the heavy hydrocarbon scrubbing tower washing flow that usually adopts, flow process of the present invention is stronger to the adaptability of heavy hydrocarbon component fluctuation in unstripped gas;
5, heavy hydrocarbon component removes thoroughly, and after process, heavy hydrocarbon component is C6 such as +deng heavy hydrocarbon component, be substantially removed, such as≤150ppm, preferably≤100ppm, more preferably≤80ppm, more preferably≤50ppm.
6, cold and hot fluid heat exchange highway route design is reasonable, realizes the Proper Match of fluid cold, heat, and plant energy consumption is reduced as far as possible.
Accompanying drawing explanation
Fig. 1 is the process chart of the de-heavy hydrocarbon of shale gas of the present invention dehydration;
Fig. 2 is a kind of process chart of refrigerant compression systems.
1, the shale gas 7 after the shale gas 5 after dewatering system 2, de-heavy hydrocarbon and heavy hydrocarbon treatment system 3, raw material shale gas 4, dehydration, the regeneration gas 6 completing regeneration, purification, regeneration gas 8, LNG9, LPG10, light oil
V1A/B, V2A/B, V3A/B, V4A/B, program-controlled valve V-1, first cryogen throttling arrangement V-2, second cryogen throttling arrangement V-3, throttling arrangement V1, gas-liquid separator V2, heavy hydrocarbon separator V3, rectifier column reflux tank V4, first order gas-liquid separator V5, second level gas-liquid separator E1, regeneration gas heater E2, regeneration gas cooler E3, plate-fin heat exchanger E4, lighter hydrocarbons heat exchanger E5, light oil cooler E6, deethanizer reboiler E7, rectifying column reboiler E8, rectifying tower top condenser E10, first order cooler E11, second-stage cooler T1, first drying tower T2, second drying tower T3, heavy hydrocarbon scrubbing tower T4, dethanizer T5, rectifying column P1, heavy hydrocarbon pump P2, rectifier column reflux pump P3, liquor pump C1, coolant compressor
Detailed description of the invention
Method of the present invention comprises dehydration procedure and de-heavy hydrocarbon and heavy hydrocarbon treatment process two parts; Dehydration procedure comprises and adopts isobaric absorbing process flow process to remove moisture content in shale gas, and the purification shale gas after the de-heavy hydrocarbon that dewaters is as regeneration gas; Shale gas after de-heavy hydrocarbon and heavy hydrocarbon treatment process comprise dehydration removes heavy hydrocarbon successively in heavy hydrocarbon separator and heavy hydrocarbon scrubbing tower, and the heavy hydrocarbon be removed enters stripping removing light component (being mainly C1, C2 hydrocarbon etc.) wherein in dethanizer successively, enters in rectifying column and be separated into LPG and light oil byproduct.Shale gas dew points at normal pressure after the de-heavy hydrocarbon that dewaters is down to≤and-76 DEG C, the heavy hydrocarbon component of C6 and more than C6 is removed to the soluble degree of LNG (such as≤150ppm, preferably≤100ppm, more preferably≤80ppm); And obtaining liquefied petroleum gas (LPG) and light oil byproduct simultaneously, economically feasible, process route are advanced.
See accompanying drawing 1, accompanying drawing 2, the method for the de-heavy hydrocarbon of shale gas dehydration provided by the invention is as follows:
Dewatering system 1 adopts the isobaric absorbing process flow process of two towers, the water adsorption in unstripped gas is got off.The flow process of the isobaric absorbing process of two towers that dewatering system 1 adopts is as follows:
Isobaric absorbing process adopts parallel two towers pattern, and wherein tower T1 is in adsorption process and another tower T2 is in regenerative process.For drying tower T1, illustrate that the isobaric absorbing process flow process of two towers is as follows:
A, adsorption process: raw material shale gas 3 enters through valve V1A self-desiccation tower T1 top the drying tower T1 being in adsorbed state.Under the adsorption selection of adsorbent, component to be removed wherein and moisture are absorbed, not by the gas that adsorbs at the bottom of tower through valve V4A duplicate removal hydrocarbon and heavy hydrocarbon treatment system.When being arrived bed outlet by the mass-transfer zone forward position of adsorbing contaminant (being called absorption forward position) and reserving section, turn off unstripped gas inlet valve V1A and the unstripped gas outlet valve V4A of this drying tower T1, stop absorption, adsorbent bed starts to proceed to regenerative process.
The regeneration of drying tower T1 comprise carry out successively heating, cold blowing process.
B, heating process: regeneration gas 4 is heated to after uniform temperature (such as 230 ~ 250 DEG C) through regeneration gas heater E1, enter drying tower T1 through valve V3A to heat, reverse purging is adsorbent bed, absorption impurity is on the sorbent desorbed completely, the adsorbent in T1 is regenerated; Go out the regeneration gas of drying tower T1 successively through valve V2A, regeneration gas cooler E2, gas-liquid separator V1 cooling, separatory, complete regeneration gas 5 emptying of regeneration or send to downstream pipe network after processing further, heating process terminates.
C, cold blowing process: after heating process terminates, regeneration gas heater E1 stops heating, and regeneration gas 4 enters the drying tower T1 being in cold blowing process, and reverse purging is adsorbent bed, makes bed be down to uniform temperature (such as about 40 DEG C); Go out the regeneration gas of drying tower T1 successively through valve V2A, regeneration gas cooler E2, gas-liquid separator V1 cooling, separatory, complete regeneration gas 5 emptying of regeneration or send to downstream pipe network after processing further, cold blowing process terminates.
After this process, drying tower T1 just completes complete " adsorption-regeneration " circulation, for absorption is got ready next time.
The absorption of drying tower T2 and regenerative process identical with drying tower T1, realizing, two cone pulley flow operations by controlling the action of different valve, reaching the object of continuous purification gas.Its process is as follows:
A, adsorption process: raw material shale gas 3 enters through valve V1B self-desiccation tower T2 top the drying tower T2 being in adsorbed state.Under the adsorption selection of adsorbent, component to be removed wherein and moisture are absorbed, not by the gas that adsorbs at the bottom of tower through valve V4B duplicate removal hydrocarbon and heavy hydrocarbon treatment system.When being arrived bed outlet by the mass-transfer zone forward position of adsorbing contaminant (being called absorption forward position) and reserving section, turn off unstripped gas inlet valve V1B and the unstripped gas outlet valve V4B of this drying tower T2, stop absorption, adsorbent bed starts to proceed to regenerative process.
The regeneration of drying tower T2 comprise carry out successively heating, cold blowing process.
B, heating process: regeneration gas 4 is heated to after uniform temperature (such as 230 ~ 250 DEG C) through regeneration gas heater E1, enter drying tower T2 through valve V3B to heat, reverse purging is adsorbent bed, absorption impurity is on the sorbent desorbed completely, the adsorbent in T2 is regenerated; Go out the regeneration gas of drying tower T2 successively through valve V2B, regeneration gas cooler E2, gas-liquid separator V1 cooling, separatory, complete regeneration gas 5 emptying of regeneration or send to downstream pipe network after processing further, heating process terminates.
C, cold blowing process: after heating process terminates, regeneration gas heater E1 stops heating, and regeneration gas 4 enters the drying tower T2 being in cold blowing process, and reverse purging is adsorbent bed, makes bed be down to uniform temperature (such as about 40 DEG C); Go out the regeneration gas of drying tower T2 successively through valve V2B, regeneration gas cooler E2, gas-liquid separator V1 cooling, separatory, complete regeneration gas 5 emptying of regeneration or send to downstream pipe network after processing further, cold blowing process terminates.
After this process, drying tower T2 just completes complete " adsorption-regeneration " circulation, for absorption is got ready next time.
The technological process of de-heavy hydrocarbon and heavy hydrocarbon treatment system 2 is as follows:
Shale gas 4 after dehydration enters de-heavy hydrocarbon and heavy hydrocarbon treatment system 2, at plate-fin heat exchanger E3(the 3rd heat exchanger channels) in be cooled to-60 ~-80 DEG C after enter heavy hydrocarbon separator V2, heavy hydrocarbon separator V2 bottom part from C3 +heavy hydrocarbon component returns plate-fin heat exchanger E3(the 4th heat exchanger channels) after re-heat to normal temperature, enter in dethanizer T4, reclaim C3 +c1, C2 hydrocarbon etc. carried in heavy hydrocarbon component, the isolated gas phase in heavy hydrocarbon separator V2 top enters heavy hydrocarbon scrubbing tower T3, and logistics mass-and heat-transfer cooled with dethanizer T4 top gas phase in heavy hydrocarbon scrubbing tower T3, finally obtains the light components such as C1, C2 and C3 respectively at the bottom of heavy hydrocarbon scrubbing tower T3 tower top, tower +heavy hydrocarbon component, the C1 that heavy hydrocarbon scrubbing tower T3 tower top obtains, the light component temperature such as C2 about-60 ~-80 DEG C, enter after cold is reclaimed in gas phase heat exchange that lighter hydrocarbons heat exchanger E4 and dethanizer T4 tower top separate and be divided into two-way, one tunnel returns plate-fin heat exchanger E3(second heat exchanger channels) liquefying becomes liquefied natural gas (LNG) 8, another road returns plate-fin heat exchanger E3(first heat exchanger channels) re-heat is to normal temperature, (heavy hydrocarbon component of C6 and more than C6 is removed to such as≤150ppm to be the purified gas after the de-heavy hydrocarbon of dehydration, preferably≤100ppm, more preferably≤80ppm), go dewatering system as regeneration gas 4 from wherein separating a road, all the other purified gas 6 go outside battery limit (BL), heavy hydrocarbon scrubbing tower T3 bottom liquid phases is pressurized to 2.0MPaA ~ 4.0MPaA through heavy hydrocarbon pump P1, then enters dethanizer T4 and removes light component (being mainly C1, C2 hydrocarbon etc.) wherein, the light component that dethanizer T4 top separates enters lighter hydrocarbons heat exchanger E4, is cooled to-60 ~-80 DEG C, enters heavy hydrocarbon scrubbing tower T3 with the heat exchange of heavy hydrocarbon scrubbing tower T3 top gaseous phase, at the bottom of dethanizer T4 tower, liquid phase (is mainly C3, C4, C5, C6 +mixture) enter in the middle part of rectifying column T5 after the 3rd throttling arrangement V-3 is decompressed to 0.5MPaA ~ 2.0MPaA, obtain the mixture of the components such as C3, C4 from tower top through rectifying, partial reflux, part extraction, be LPG product, at the bottom of tower be separated obtain C5, C6 +etc. the mixture of component, after light oil cooler E5 is cooled to normal temperature, be light oil byproduct.
Preferably, the cold needed for plate-fin heat exchanger E3 by or provide primarily of refrigerant compression systems, refrigerant compression systems simultaneously for shale gas low temperature remove heavy hydrocarbon and purification shale gas liquefaction cold is provided; Described refrigerant compression systems adopts one-level or two-stage compression.
As shown in Figure 2, as a kind of concrete embodiment, refrigerant compression systems comprises a coolant compressor C1, two cooler E10, E11, two gas-liquid separators V4, V5 and liquor pump P3; Coolant compressor adopts two-stage compression; Refrigerant compression systems has an access road, a gas phase cryogen exit passageway and a liquid phase cryogen exit passageway.
By C1 ~ C5 and N 2in cold-producing mediums of one or more compositions enter the entrance of refrigerant compression systems, 0.6 ~ 1.8MPaA is compressed to through first paragraph, enter first order cooler E10 and be cooled to 30 DEG C ~ 45 DEG C, enter first order gas-liquid separator V4 again and carry out gas-liquid separation, the isolated gas in first order gas-liquid separator V4 top continues the second segment entrance entering compressor, 1.2 ~ 5.4MPaA is compressed to through two sections, after the hot gas that the isolated liquid of first order gas-liquid separator V4 bottom liquid phases end compresses outlet conduit with second segment after liquor pump P3 pressurizes converges, enter again in second-stage cooler E11 and be cooled to 30 DEG C ~ 45 DEG C, cooled cold-producing medium enters second level gas-liquid separator V5 subsequently and carries out gas-liquid separation, the top gas of second level gas-liquid separator V5 enters the 5th heat exchanger channels participation heat exchange of plate-fin heat exchanger E3 subsequently, bottom the gas-liquid separator V5 of the second level, isolated liquid enters the 7th heat exchanger channels participation heat exchange of plate-fin heat exchanger E3,
As shown in Figures 1 and 2, the liquid refrigerant going out refrigerant compression systems enters the 7th heat exchanger channels of plate-fin heat exchanger E3 in accompanying drawing 1 through liquid phase cryogen exit passageway, be chilled to about-30 DEG C ~-80 DEG C in advance wherein, after first cryogen throttling arrangement V-1 throttling to 0.2 ~ 0.8MPaA, returned the 6th heat exchanger channels of plate-fin heat exchanger E3; The 5th heat exchanger channels that the gas refrigerant going out refrigerant compression systems enters plate-fin heat exchanger E3 in accompanying drawing 1 through gas phase cryogen exit passageway is cooled to-135 DEG C ~-169 DEG C, after second cryogen throttling arrangement V-2 throttling to 0.2 ~ 0.8MPaA, oppositely enter the 6th heat exchanger channels heat exchange of plate-fin heat exchanger E3 again, the access road through refrigerant compression systems after re-heat to normal temperature returns refrigerant compression systems.
Reboiler that is built-in, any pattern such as autoclave, heat siphon type can be adopted at the bottom of the tower of dethanizer T4 and rectifying column T5.
Here, pressure unit MPaA is MPa, absolute pressure.
Adopt the device except mix refrigerant compressibility technological process described in this patent, the technological process of cold is provided for plate-fin heat exchanger E3, also belong to the protection domain of this patent.

Claims (14)

1. a method for the de-heavy hydrocarbon of shale gas dehydration, is characterized in that, the method comprises dehydration procedure and de-heavy hydrocarbon and heavy hydrocarbon treatment process two parts;
Dehydration procedure comprises and adopts isobaric absorbing process flow process to remove moisture content in raw material shale gas, and the purification shale gas after the de-heavy hydrocarbon that dewaters is as the regeneration gas in dehydration procedure; Shale gas after de-heavy hydrocarbon and heavy hydrocarbon treatment process comprise dehydration removes heavy hydrocarbon successively after plate-fin heat exchanger cooling in heavy hydrocarbon separator and heavy hydrocarbon scrubbing tower, the heavy hydrocarbon be removed enters stripping removing light component wherein in dethanizer successively, wherein from the light component of dethanizer in lighter hydrocarbons heat exchanger isolated with heavy hydrocarbon scrubbing tower tower top remove the shale gas heat exchange of heavy hydrocarbon after enter heavy hydrocarbon scrubbing tower and be separated again, wherein enter in rectifying column from the heavy constituent of dethanizer and isolate light oil and gas phase, this gas phase is cooled into liquefied petroleum gas; With from the isolated de-heavy hydrocarbon shale gas of heavy hydrocarbon scrubbing tower tower top after the heat exchange of lighter hydrocarbons heat exchanger, part to return in plate-fin heat exchanger liquefaction and obtaining liquefied natural gas and namely to dewater the shale gas after de-heavy hydrocarbon, and part returns in plate-fin heat exchanger goes dehydration procedure as regeneration gas after heat exchange; Shale gas dew points at normal pressure after the de-heavy hydrocarbon of dehydration is down to≤and-76 DEG C, the heavy hydrocarbon component of C6 and more than C6 is removed to the soluble degree of LNG.
2. the method for the de-heavy hydrocarbon of shale gas dehydration according to claim 1, it is characterized in that, dehydration procedure adopts the isobaric absorbing process flow processs of two towers, utilizes one or more in activated alumina, 3A molecular sieve or 4A molecular sieve as adsorbent, the water adsorption in raw material shale gas is got off.
3. the method for the de-heavy hydrocarbon of shale gas dehydration according to claim 1 and 2, is characterized in that, sends to gas distributing system after the regeneration gas regeneration ending of dehydration procedure after emptying or further process.
4. the method for the de-heavy hydrocarbon of shale gas dehydration according to claim 1 and 2, it is characterized in that, in de-heavy hydrocarbon and heavy hydrocarbon treatment process, the shale gas after dehydration enters heavy hydrocarbon separator after entering in plate-fin heat exchanger and being cooled to-60 ~-80 DEG C, the C3 that heavy hydrocarbon separator bottom is separated +heavy hydrocarbon component enters in dethanizer after returning plate-fin heat exchanger re-heat to normal temperature, reclaims C3 +the light component comprising C1, C2 hydrocarbon carried in heavy hydrocarbon component; The isolated gas phase in heavy hydrocarbon separator top enters heavy hydrocarbon scrubbing tower, in heavy hydrocarbon scrubbing tower with dethanizer top gas phase cooled logistics mass-and heat-transfer, finally at the bottom of heavy hydrocarbon scrubbing tower tower top, tower, obtain the light component and the C3 that comprise C1, C2 respectively +heavy hydrocarbon component; The light component comprising C1, C2 of the temperature that heavy hydrocarbon scrubber overhead obtains-60 ~-80 DEG C enters after gas phase heat exchange that lighter hydrocarbons heat exchanger and deethanization tower top separate reclaims cold, part returns plate-fin heat exchanger liquefaction becomes liquefied natural gas, part returns plate-fin heat exchanger re-heat to normal temperature, be the shale gas after the de-heavy hydrocarbon of dehydration, separating a road goes dehydration procedure as regeneration gas, optionally separates another road and goes outside battery limit (BL); Heavy hydrocarbon wash tower bottoms liquid phase is pressurized to 2.0 MPaA ~ 4.0 MPaA through heavy hydrocarbon pump, then enters dethanizer and removes the light component being mainly C1, C2 hydrocarbon wherein; The light component that dethanizer top separates enters lighter hydrocarbons heat exchanger and the heat exchange of heavy hydrocarbon scrubbing tower top gaseous phase is cooled to-60 ~-80 DEG C, enters heavy hydrocarbon scrubbing tower; Be mainly C3, C4, C5, C6 +mixture dethanizer tower at the bottom of liquid phase be decompressed to through throttling arrangement and enter in the middle part of rectifying column after 0.5 MPaA ~ 2.0 MPaA, be separated at the bottom of tower through rectifying and obtain light oil products and obtain gas phase from tower top, then this gas phase is cooled into liquefied petroleum gas.
5. the method for the de-heavy hydrocarbon of shale gas dehydration according to claim 1 and 2, it is characterized in that, cold needed for plate-fin heat exchanger by or provide primarily of refrigerant compression systems, refrigerant compression systems simultaneously for shale gas low temperature remove heavy hydrocarbon and purification shale gas liquefaction cold is provided;
By C1 ~ C5 and N 2in cold-producing mediums of one or more compositions enter the entrance of refrigerant compression systems, 0.6 ~ 1.8MPaA is compressed to through first paragraph, enter first order cooler and be cooled to 30 DEG C ~ 45 DEG C, enter first order gas-liquid separator again and carry out gas-liquid separation, the isolated gas in first order gas-liquid separator top continues the second segment entrance entering compressor, 1.2 ~ 5.4MPaA is compressed to through two sections, after the hot gas that the isolated liquid of first order gas-liquid separator bottom liquid phases end compresses outlet conduit with second segment after liquor pump pressurization converges, enter again in second-stage cooler and be cooled to 30 DEG C ~ 45 DEG C, cooled cold-producing medium enters second level gas-liquid separator subsequently and carries out gas-liquid separation, the cryogen heat exchanger channels that the isolated liquid of the top gas of second level gas-liquid separator and bottom enters plate-fin heat exchanger participates in heat exchange,
First entered the liquid phase cryogen heat exchanger channels of plate-fin heat exchanger by the liquid of drawing bottom the gas-liquid separator of the second level, be chilled to-30 DEG C ~-80 DEG C in advance wherein, after first throttle device throttling to 0.2 ~ 0.8MPaA, enter cryogen separator;-135 DEG C ~-169 DEG C are cooled to by the gas phase cryogen heat exchanger channels of plate-fin heat exchanger by the vapor phase stream stock of the isolated cold-producing medium in gas-liquid separator top, the described second level, after second throttling arrangement throttling to 0.2 ~ 0.8MPaA, oppositely enter the other heat exchanger channels heat exchange of plate-fin heat exchanger again, provide cold for plate-fin heat exchanger and then turn back to coolant compressor first compression section.
6. the method for the de-heavy hydrocarbon of shale gas dehydration according to claim 4, it is characterized in that, cold needed for plate-fin heat exchanger by or provide primarily of refrigerant compression systems, refrigerant compression systems simultaneously for shale gas low temperature remove heavy hydrocarbon and purification shale gas liquefaction cold is provided;
By C1 ~ C5 and N 2in cold-producing mediums of one or more compositions enter the entrance of refrigerant compression systems, 0.6 ~ 1.8MPaA is compressed to through first paragraph, enter first order cooler and be cooled to 30 DEG C ~ 45 DEG C, enter first order gas-liquid separator again and carry out gas-liquid separation, the isolated gas in first order gas-liquid separator top continues the second segment entrance entering compressor, 1.2 ~ 5.4MPaA is compressed to through two sections, after the hot gas that the isolated liquid of first order gas-liquid separator bottom liquid phases end compresses outlet conduit with second segment after liquor pump pressurization converges, enter again in second-stage cooler and be cooled to 30 DEG C ~ 45 DEG C, cooled cold-producing medium enters second level gas-liquid separator subsequently and carries out gas-liquid separation, the cryogen heat exchanger channels that the isolated liquid of the top gas of second level gas-liquid separator and bottom enters plate-fin heat exchanger participates in heat exchange,
First entered the liquid phase cryogen heat exchanger channels of plate-fin heat exchanger by the liquid of drawing bottom the gas-liquid separator of the second level, be chilled to-30 DEG C ~-80 DEG C in advance wherein, after first throttle device throttling to 0.2 ~ 0.8MPaA, enter cryogen separator;-135 DEG C ~-169 DEG C are cooled to by the gas phase cryogen heat exchanger channels of plate-fin heat exchanger by the vapor phase stream stock of the isolated cold-producing medium in gas-liquid separator top, the described second level, after second throttling arrangement throttling to 0.2 ~ 0.8MPaA, oppositely enter the other heat exchanger channels heat exchange of plate-fin heat exchanger again, provide cold for plate-fin heat exchanger and then turn back to coolant compressor first compression section.
7. the method for the de-heavy hydrocarbon of shale gas according to claim 1 and 2 dehydration, is characterized in that, adopts the reboiler of built-in, autoclave or heat siphon type at the bottom of the tower of dethanizer and rectifying column.
8. a device for the de-heavy hydrocarbon of shale gas dehydration, is characterized in that: described device comprises dewatering system and de-heavy hydrocarbon and heavy hydrocarbon treatment system;
Wherein
Dewatering system comprises: sorption drying device, a unstripped gas access road, a dehydrated feed gas exit passageway, a regeneration gas access road, a regeneration gas exit passageway;
De-heavy hydrocarbon and heavy hydrocarbon treatment system comprise: a heavy hydrocarbon separator, a heavy hydrocarbon scrubbing tower, a dethanizer, a rectifying column, a plate-fin heat exchanger, a lighter hydrocarbons heat exchanger, throttling arrangement, a light oil cooler and a heavy hydrocarbon pump;
Described plate-fin heat exchanger at least comprises following heat exchanger channels: the first heat exchanger channels, the second heat exchanger channels, the 3rd heat exchanger channels, the 4th heat exchanger channels and for providing the cryogen heat exchanger channels of cold for heat exchanger;
Described heavy hydrocarbon separator comprises a dehydrated feed gas access road, a heavy hydrocarbon exit passageway and a lighter hydrocarbons exit passageway;
Described heavy hydrocarbon scrubbing tower comprises a gas phase access road, a mixed phase access road, a gaseous phase outlet passage, a heavy hydrocarbon exit passageway;
Described dethanizer comprises the first liquid phase access road, second liquid phase access road, a gaseous phase outlet passage, a heavy hydrocarbon exit passageway;
Described rectifying column comprises a heavy hydrocarbon access road, a liquefied petroleum gas exit passageway, a light oil exit passageway;
Described lighter hydrocarbons heat exchanger at least comprises the first and second two heat exchanger channels; The arrival end of the first heat exchanger channels of lighter hydrocarbons heat exchanger and the gaseous phase outlet expanding channels of heavy hydrocarbon scrubbing tower, the port of export of the first heat exchanger channels of lighter hydrocarbons heat exchanger is divided into two-way, be connected with the arrival end of the first heat exchanger channels of described plate-fin heat exchanger and the arrival end of the second heat exchanger channels respectively, the arrival end of the second heat exchanger channels of lighter hydrocarbons heat exchanger and the gaseous phase outlet expanding channels of described dethanizer, the port of export of the second heat exchanger channels of lighter hydrocarbons heat exchanger is connected with the mixed phase access road of described heavy hydrocarbon scrubbing tower;
The port of export of the first heat exchanger channels of described plate-fin heat exchanger is divided into two-way, and a road connects the regeneration gas access road of dewatering system, and another road is gone outside battery limit (BL);
The port of export of the second heat exchanger channels of described plate-fin heat exchanger is connected to downstream pipe network natural gas liquefaction system;
The arrival end of the 3rd heat exchanger channels of described plate-fin heat exchanger connects the dehydrated feed gas exit passageway of dewatering system, and the port of export connects the dehydrated feed gas access road of heavy hydrocarbon separator;
4th heat exchanger channels arrival end of plate-fin heat exchanger is connected with the heavy hydrocarbon exit passageway of heavy hydrocarbon separator; The port of export connects the second liquid phase access road of dethanizer,
The lighter hydrocarbons exit passageway of described heavy hydrocarbon separator is connected with the gas phase access road of heavy hydrocarbon scrubbing tower;
The heavy hydrocarbon exit passageway of described heavy hydrocarbon scrubbing tower is connected to the input of heavy hydrocarbon pump, and heavy hydrocarbon delivery side of pump connects the first liquid phase access road of dethanizer;
The heavy hydrocarbon exit passageway of described dethanizer is connected with the liquid phase access road of described rectifying column via First throttling arrangement;
The liquefied petroleum gas exit passageway of described rectifying column is connected to liquefied petroleum gas product storage tank via an aftercooler; Light oil products storage tank is connected to after the light oil exit passageway connection light oil cooler of rectifying column.
9. shale gas dehydration de-heavy hydrocarbon apparatus according to claim 8, is characterized in that, described dewatering system adopts the isobaric absorption drying system of two towers.
10. shale gas dehydration de-heavy hydrocarbon apparatus according to claim 9, it is characterized in that, the sorption drying device of described dewatering system comprises:
First drying tower (T1) and the second drying tower (T2), both the first drying tower and the second drying tower are alternately in dry run and regenerative process,
Regeneration gas heater (E1),
Gas-liquid separator (V1), and
Regeneration gas cooler (E2),
Each drying tower have one or two or multiple adsorbent bed,
The carrier pipe of raw material shale gas is divided into two branch roads i.e. the first branch road and the second branch road, first branch road is via first valve (V1A), the ingress pipe of the first drying tower (T1), first drying tower (T1) and the 4th valve (V4A), then de-heavy hydrocarbon and heavy hydrocarbon treatment system is led to by the dehydrated feed gas exit passageway of dewatering system, second branch road is via the 5th valve (V1B), the ingress pipe of the second drying tower (T2), second drying tower (T2) and the 8th valve (V4B), then de-heavy hydrocarbon and heavy hydrocarbon treatment system is led to by the dehydrated feed gas exit passageway of dewatering system, between the first drying tower (T1) and the 4th valve (V4A), draw arm and draw arm between the second drying tower (T2) and the 8th valve (V4B), these two arms converge via after the 3rd valve (V3A) and the 7th valve (V3B) one end being connected to regeneration gas heater (E1) respectively, and the other end of regeneration gas heater (E1) is connected to de-heavy hydrocarbon and heavy hydrocarbon treatment system by the regeneration gas access road of dewatering system, between the first drying tower (T1) and first valve (V1A), draw arm and draw arm between the second drying tower (T2) and the 5th valve (V1B), these two arms converge via after second valve (V2A) and the 6th valve (V2B) respectively, via the importing end of regeneration gas cooler (E2), regeneration gas cooler (E2), the derivation end of regeneration gas cooler (E2) is connected to the ingress pipe of gas-liquid separator (V1), the top delivery line of gas-liquid separator (V1) is connected to dewatering system regeneration gas exit passageway.
11. devices according to Claim 8 described in-10 any one, is characterized in that: the adsorbent in described sorption drying device is selected from the adsorbent in 3A or 4A molecular sieve, activated alumina.
12. devices according to Claim 8 described in-10 any one, it is characterized in that: the gaseous phase outlet passage of described rectifying column is first via aftercooler with optionally via a rectifier column reflux tank, then two arms are separated, an arm is connected with liquefied petroleum gas product storage tank, and another arm, optional via a pump, what be connected to rectifying column separately establishes liquid phase access road.
13. devices according to Claim 8 described in-10 any one, is characterized in that: adopt built-in, autoclave or thermosyphon reboiler at the bottom of the tower of described dethanizer and/or described rectifying column.
14. devices according to Claim 8 described in-10 any one, it is characterized in that: the cold in described plate-fin heat exchanger is provided by refrigerant compression systems, the liquor pump that described refrigerant compression systems comprises two-period form mixed working fluid compressor, the first order cooler be connected with first paragraph and the second segment of described two-period form mixed working fluid compressor respectively and second-stage cooler, the first order gas-liquid separator be connected with described first order cooler and second-stage cooler respectively and second level gas-liquid separator and is connected with first order gas-liquid separator
Described plate-fin heat exchanger for providing the cryogen heat exchanger channels of cold to comprise the 5th heat exchanger channels, the 6th heat exchanger channels and the 7th heat exchanger channels for heat exchanger, the arrival end of described 5th heat exchanger channels and the arrival end of the 7th heat exchanger channels are connected with the gas phase end of the second level gas-liquid separator in described refrigerant compression systems and liquid phase end respectively via two pipelines, and the port of export of the 6th heat exchanger channels is connected to the cryogen access road of the first compression section via pipeline;
The port of export of the 5th heat exchanger channels of described plate-fin heat exchanger is connected via the arrival end of the second cryogen throttling arrangement with the 6th heat exchanger channels, and the port of export of the 7th heat exchanger channels of described plate-fin heat exchanger returns the 6th heat exchanger channels via after the first cryogen throttling arrangement throttling;
The gas phase end of the first order gas-liquid separator wherein in two gas-liquid separators is connected with the second compression section of two-period form mixed working fluid compressor, and the liquid phase end of first order gas-liquid separator is connected to the second-stage cooler in described two coolers after converging via the outlet conduit of liquor pump and the second compression section.
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