CN103351896A - 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

Info

Publication number
CN103351896A
CN103351896A CN2013102247273A CN201310224727A CN103351896A CN 103351896 A CN103351896 A CN 103351896A CN 2013102247273 A CN2013102247273 A CN 2013102247273A CN 201310224727 A CN201310224727 A CN 201310224727A CN 103351896 A CN103351896 A CN 103351896A
Authority
CN
China
Prior art keywords
heavy hydrocarbon
gas
heat exchanger
tower
exchanger channels
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Granted
Application number
CN2013102247273A
Other languages
Chinese (zh)
Other versions
CN103351896B (en
Inventor
何振勇
宣永根
徐化周
李伟
刘学强
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.)
Xindi Energy Engineering Technology Co Ltd
Original Assignee
Xindi Energy Engineering Technology Co 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
Application filed by Xindi Energy Engineering Technology Co Ltd filed Critical Xindi Energy Engineering Technology Co Ltd
Priority to CN201310224727.3A priority Critical patent/CN103351896B/en
Publication of CN103351896A publication Critical patent/CN103351896A/en
Application granted granted Critical
Publication of CN103351896B publication Critical patent/CN103351896B/en
Active legal-status Critical Current
Anticipated expiration legal-status Critical

Links

Images

Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/0204—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the feed stream
    • F25J3/0209—Natural gas or substitute natural gas
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • 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
    • 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
    • F25J2200/04—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.

Landscapes

  • 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 shale gas takes off heavy hydrocarbon method and device
Technical field
The invention provides a kind of shale gas and take off heavy hydrocarbon method and device, from the moisture shale gas that contains heavy hydrocarbon, remove moisture and heavy hydrocarbon, but also by-product liquefied petroleum gas (LPG) (LPG) and light oil byproduct.
Background technology
Shale gas is out Sweet natural gas of exploitation from the shale bed, particularly, is to be present in Sweet natural gas in mud stone, high-carbon mud stone, shale and the aleuritic texture rock class interlayer with absorption or unbound state on the main body, can be created on the various stages of organic origin.World's shale gas stock number is 457 tcms, and is suitable with the conventional gas stock number, and wherein shale gas technology mining resources amount 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 preliminary exploitation pilot phase.By in April, 2012, China determines 33 shale gas Favorable Areas altogether, 58 mouthfuls of shale gas completions, and wherein horizontal well is 15 mouthfuls.Along with the shale gas exploration right is progressively open to the public, the shale gas exploitation of Future Ten year will be rapidly developed.Yet shale gas is as an emerging unconventional energy resource, and its treatment technology is also relatively less, along with the exploitation of new forms of energy, the development requirement of the treatment technology of shale gas is also increased day by day.Because the composition of shale gas changes greatly, i.e. moisture and the heavy hydrocarbons content of the shale gas of the exploitation of the difference in zonule point change greatly, so that utilize existing device shale gas to be carried out the operation difficult of purifying.In view of the composition difference between shale gas and the common Sweet natural gas is large, adopts the treatment process of existing common Sweet natural gas and device to process shale gas and can't obtain qualified Sweet natural gas from shale gas.
Chinese patent CN103031168A has proposed a kind of dehydration of producing natural gas liquids from the mixed gas that is rich in methane and has taken off heavy hydrocarbon technique, the composite bed of the sorbent materials such as the described process using molecular sieve of this patent, activated alumina and water-fast silica gel removes water and the heavy hydrocarbon in the methane-riched gas mixture, adopt the isobaric adsorption process of three towers, the adsorption tower resurgent gases is taken from process gas.Adopt the multiple-hearth adsorption process, heavy hydrocarbon can partly be removed, and the degree that removes depends on load and the regeneration level of sorbent material.But only adopt sorbent material can not make the content of heavy hydrocarbon to very low requirement, especially when the heavy hydrocarbon amount that need to remove is larger, may cause Cold box blocking and freezing because heavy hydrocarbon can't be removed to reasonable depth, so usually adopt absorption to take off the technology that heavy hydrocarbon cooperates low ternperature separation process.
Chinese patent CN103031169A has proposed the method and apparatus of a kind of natural gas liquefaction and heavy hydrocarbon processing, adopts self phlegma washing heavy hydrocarbon.The raw natural gas of normal temperature directly enters the heavy hydrocarbon washing tower, and through the heavy hydrocarbons such as C3, the C4 washing that low ternperature separation process goes out in Sweet natural gas, the above heavy hydrocarbon of C6 and C6 is able to deep removal in the Sweet natural gas.Because this technique relies on the heavy hydrocarbon phlegma washing heavy hydrocarbon of Sweet natural gas self, remove system and can normally move so the heavy hydrocarbons content of Sweet natural gas self directly has influence on heavy hydrocarbon.For guaranteeing that suitable heavy hydrocarbon condensing liquid quantity keeps the operate continuously of washing tower, can take on stream the precooling temperature of temperature adjustment measure control Sweet natural gas to adjust the natural gas condensates amount.In addition, when the heavy hydrocarbon condensing liquid quantity is less, also can introduce the heavy hydrocarbon in the iso-pentane washing Sweet natural gas, the purpose by the vapor liquid equilibrium that changes system reaches the heavy hydrocarbon condensation and removes still can cause a certain amount of iso-pentane consumption.Since need to be for the in good time switching flow of heavy hydrocarbons content in the 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 that is applicable to shale gas and take off heavy hydrocarbon method and device, moisture in the shale gas and heavy hydrocarbon are removed, and further heavy hydrocarbon component is separated into available liquefied petroleum gas (LPG) (LPG) and light oil byproduct, economically feasible, operational path advanced person; Shale gas dew points at normal pressure after heavy hydrocarbon is taken off in dehydration is down to≤and-76 ℃, the above heavy hydrocarbon component of C6 and C6 is removed to the soluble degree of LNG.
According to a first aspect of the invention, the method that provides a kind of shale gas to take off heavy hydrocarbon comprises dehydration procedure and takes off heavy hydrocarbon and heavy hydrocarbon treatment process two portions; Dehydration procedure comprises that the isobaric absorbing process flow process of employing removes the moisture content in the raw material shale gas, purification shale gas after heavy hydrocarbon is taken off in dehydration is as the resurgent gases in the dehydration procedure (that is, take off in heavy hydrocarbon and the heavy hydrocarbon separation circuit purification shale gas after heavy hydrocarbon is taken off in dehydration as resurgent gases); Take off heavy hydrocarbon and heavy hydrocarbon treatment process and comprise that the shale gas after the dehydration removes heavy hydrocarbon successively after the plate-fin heat exchanger cooling in heavy hydrocarbon separator and heavy hydrocarbon washing tower, the heavy hydrocarbon that is removed enters successively stripping in the deethanizing column and removes wherein light constituent, wherein enter the heavy hydrocarbon washing tower and separate again in the lighter hydrocarbons interchanger with after the isolated shale gas heat exchange that removes heavy hydrocarbon of heavy hydrocarbon washing tower cat head from the light constituent of deethanizing column, wherein divide to enter from the restructuring of deethanizing column and isolate light oil and gas phase in the rectifying tower, this gas phase is cooled into liquefied petroleum gas (LPG); With from the isolated heavy hydrocarbon shale gas that takes off of heavy hydrocarbon washing tower cat head after the heat exchange of lighter hydrocarbons interchanger, liquefaction obtains namely dewater shale gas behind the heavy hydrocarbon of natural gas liquids in the part Returning plate fin heat exchanger, goes dehydration procedure as resurgent gases after the heat exchange in the part Returning plate fin heat exchanger; Take off shale gas dew points at normal pressure behind the heavy hydrocarbon to be down to≤-76 ℃, the above heavy hydrocarbon component of C6 and C6 is removed to the soluble degree of LNG, for example≤150ppm, preferred≤100ppm, more preferably≤80ppm, more preferably≤50ppm.
Preferably, dehydration procedure adopts the isobaric absorbing process flow process of two towers, utilizes in activated alumina, 3A molecular sieve or the 4A molecular sieve one or more as sorbent material, and the water adsorption in the raw material shale gas is got off.
Preferably, send to gas distributing system after emptying or further the processing behind the resurgent gases regeneration ending of dehydration procedure.
In a preferred embodiment, dehydration procedure adopts the isobaric absorbing process flow process of two towers, utilizes in activated alumina, 3A molecular sieve or the 4A molecular sieve etc. one or more as sorbent material, and the water adsorption in the raw material shale gas is got off.
In a preferred embodiment, the flow process of the isobaric absorbing process of two towers that adopt of dehydration procedure is as follows:
Isobaric absorbing process adopts two tower paralleling models, and wherein tower T1 is in adsorption process and another tower T2 is in regenerative process.Take adsorption tower T1 as example, illustrate that the isobaric absorbing process flow process of two towers is as follows:
A, adsorption process: unstripped gas enters the adsorption tower T1 that is in adsorbed state through valve V1A from adsorption tower T1 top.Under the selection absorption of sorbent material, component to be removed wherein is that moisture is adsorbed, and the gas that is not adsorbed goes out system through valve V4A at the bottom of tower.When the mass transfer zone forward position (being called absorb leading-edge) that is adsorbed impurity arrives bed outlet reservation section, turn off unstripped gas feed valve V1A and the unstripped gas outlet valve V4A of this adsorption tower T1, stop absorption, adsorption bed begins to change over to regenerative process.
The regeneration of adsorption tower T1 comprise successively heat, the cold blowing process.
B, heat-processed: resurgent gases is after resurgent gases well heater E1 is heated to certain temperature (for example 230～250 ℃), entering adsorption tower T1 heats, reverse purging is adsorbent bed, and the impurity that is adsorbed on the sorbent material is desorbed fully, makes the sorbent material among the T1 obtain regeneration; Go out the resurgent gases of adsorption tower T1 successively through valve V2A, resurgent gases water cooler E2, minute flow container V1, send to gas distributing system after emptying or further the processing behind cooling, the separatory, heat-processed finishes.
C, cold blowing process: after heat-processed finishes, resurgent gases well heater E1 stopped heating, resurgent gases enters the adsorption tower T1 that is in the cold blowing process, and reverse purging is adsorbent bed, makes bed be down to certain temperature (for example about 40 ℃); Go out the resurgent gases of adsorption tower T1 successively through valve V2A, resurgent gases water cooler E2, minute flow container V1, send to gas distributing system, the cold blowing end of processing after emptying or further the processing behind cooling, the separatory.
Adsorption tower T1 has just finished complete " adsorption-regeneration " circulation after this process, for next time absorption is got ready.The absorption of adsorption tower T2 and regenerative process and adsorption tower T1 are identical, realize that by the action of controlling different valves two cone pulley flow operations reach the purpose of continuous purification gas.
Shale gas after the dehydration enters and takes off heavy hydrocarbon and heavy hydrocarbon separation circuit, enters the heavy hydrocarbon separator, the C3 that separate heavy hydrocarbon separator bottom be cooled to-60～-80 ℃ (preferred-65～-75 ℃) in plate-fin heat exchanger after +Heavy hydrocarbon component returns the plate-fin heat exchanger re-heat and enters in the deethanizing column to normal temperature, reclaims C3 +The light constituent that carries in the heavy hydrocarbon component (C1, C2 hydrocarbon etc.); The isolated gas phase in heavy hydrocarbon separator top enters the heavy hydrocarbon washing tower, with the cooled logistics mass-and heat-transfer of deethanizing column top gas phase, finally obtains light constituent and the C3 such as C1, C2 respectively at the bottom of heavy hydrocarbon scrubber overhead, tower in the heavy hydrocarbon washing tower +Heavy hydrocarbon component; The C1 that heavy hydrocarbon washing tower cat head obtains,-60～-80 ℃ approximately of the light constituent temperature such as C2, enter after gas phase heat exchange that lighter hydrocarbons interchanger and deethanizing cat head tell reclaims cold, part is returned plate-fin heat exchanger liquefaction becomes natural gas liquids (LNG), part is returned the plate-fin heat exchanger re-heat to normal temperature, (wherein the above heavy hydrocarbon component of C6 and C6 is removed to the soluble degree of LNG to be the shale gas that takes off behind the heavy hydrocarbon, for example≤150ppm, preferably≤100ppm, more preferably≤80ppm, more preferably≤50ppm), tell one the tunnel and go dehydration procedure as resurgent gases, optional tell another road and go outside the battery limit (BL); Heavy hydrocarbon wash tower bottoms liquid phase is pressurized to the preferred 2.2～3.8MPaA of 2.0MPaA～4.0MPaA(through the heavy hydrocarbon pump, more preferably 2.5～3.5MPaA, further preferred 2.8～3.2MPaA), then enter deethanizing column and remove wherein light constituent (being mainly C1, C2 hydrocarbon etc.); The light constituent that the deethanizing column top is told enters lighter hydrocarbons interchanger and the heat exchange of heavy hydrocarbon scrubber overhead gas phase and is cooled to-60～-80 ℃ (preferred-62～-78 ℃, more preferably-65～-75 ℃, further preferred-68～-72 ℃), enters the heavy hydrocarbon washing tower; Liquid phase at the bottom of the deethanizing Tata (is mainly C3, C4, C5, C6 +Mixture) be decompressed to 0.5MPaA～2.0MPaA(through the first throttle device and be preferably 0.7～1.8MPaA, more preferably enter the rectifying tower middle part after 1.0～1.5MPaA), obtain the mixture of the components such as C3, C4 from cat head through rectifying, partial reflux (access road of establishing in addition by rectifying tower), the part extraction, be liquefied petroleum gas (LPG) (LPG) product, separate obtaining C5, C6 at the bottom of the tower +Etc. the mixture of component, after the light oil water cooler is cooled to normal temperature, be the light oil byproduct.
The required cold of plate-fin heat exchanger by or mainly provided by refrigerant compression systems, refrigerant compression systems removes heavy hydrocarbon for shale gas low temperature simultaneously and purifies shale gas liquefaction provides cold; 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 the refrigeration agent of one or more compositions enter the entrance of refrigerant compression systems, be compressed to the preferred 0.8～1.6MPaA of 0.6～1.8MPaA(through first paragraph, more preferably 1.0～1.4MPaA), enter first step water cooler and be cooled to 30 ℃～45 ℃ (preferred 32～42 ℃, more preferably 35～40 ℃), enter again first step gas-liquid separator and carry out gas-liquid separation, the isolated gas in first step gas-liquid separator top continues to enter the second segment entrance of compressor, be compressed to the preferred 1.5～5.0MPaA of 1.2～5.4MPaA(through two sections, more preferably 2.0～4.5MPaA, further preferred 2.5～4.0MPaA), the isolated liquid of first step gas-liquid separator bottom liquid phases end is after converging with the hot gas of second segment compression outlet conduit after the liquor pump pressurization, enter again and be cooled to 30 ℃～45 ℃ (preferred 32～42 ℃ in the second-stage cooler, more preferably 35～40 ℃), cooled refrigeration agent enters subsequently second stage gas-liquid separator and carries out gas-liquid separation, and the heat exchanger channels that the isolated liquid of the top gas of second stage gas-liquid separator and second stage gas-liquid separator bottom enters plate-fin heat exchanger participates in heat exchange.
Preferably, the liquid of drawing bottom the gas-liquid separator of the second stage at first enters the liquid phase cryogen heat exchanger channels of plate-fin heat exchanger, is chilled in advance therein-30 ℃～-80 ℃ approximately, enters the cryogen separator behind first cryogen throttling set throttling to 0.2～0.8MPaA; Be cooled to-135 ℃～-169 ℃ by the vapor phase stream thigh of the isolated refrigeration agent in gas-liquid separator top, the described second stage gas phase cryogen heat exchanger channels by plate-fin heat exchanger, behind second cryogen throttling set throttling to 0.2～0.8MPaA, oppositely enter again the other heat exchanger channels heat exchange of plate-fin heat exchanger, for plate-fin heat exchanger provides cold and then turns back to coolant compressor the first compression section.
Adopt the arbitrarily reboiler of pattern such as built-in, autoclave, heat siphon type at the bottom of the tower of deethanizing column and rectifying tower.
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 takes off heavy hydrocarbon and the heavy hydrocarbon treatment system;
Wherein
Dewatering system comprises: sorption drying device, a unstripped gas access road, a dehydration unstripped gas exit passageway, a resurgent gases access road, a resurgent gases exit passageway;
Take off heavy hydrocarbon and the heavy hydrocarbon treatment system comprises: a heavy hydrocarbon separator, a heavy hydrocarbon washing tower, a deethanizing column, rectifying tower, a platen wing interchanger, a lighter hydrocarbons interchanger, a throttling set, a light oil water cooler and a heavy hydrocarbon pump;
Described plate-fin heat exchanger comprises following heat exchanger channels at least: the first heat exchanger channels, the second heat exchanger channels, the 3rd heat exchanger channels, the 4th heat exchanger channels and be used to interchanger that the cryogen heat exchanger channels of cold is provided;
Described heavy hydrocarbon separator comprises a dehydration unstripped gas access road, a heavy hydrocarbon exit passageway and a lighter hydrocarbons exit passageway;
Described heavy hydrocarbon washing tower comprises a gas phase access road, a mixed phase access road, a gaseous phase outlet passage, a heavy hydrocarbon exit passageway;
Described deethanizing column comprises the first liquid phase access road, second liquid phase access road, a gaseous phase outlet passage, a heavy hydrocarbon exit passageway;
Described rectifying tower comprises a heavy hydrocarbon access road, a liquefied petroleum gas (LPG) exit passageway, a light oil exit passageway;
Described lighter hydrocarbons interchanger comprises the first and second two heat exchanger channels at least; The inlet end of the first heat exchanger channels of lighter hydrocarbons interchanger is connected with the gaseous phase outlet passage of heavy hydrocarbon washing tower, the exit end of the first heat exchanger channels of lighter hydrocarbons interchanger is divided into two-way, respectively with the inlet end of the first heat exchanger channels of described plate-fin heat exchanger be connected the inlet end of heat exchanger channels and be connected, the inlet end of the second heat exchanger channels of lighter hydrocarbons interchanger is connected with the gaseous phase outlet passage of described deethanizing column, and the exit end of the second heat exchanger channels of lighter hydrocarbons interchanger is connected with the mixed phase access road of described heavy hydrocarbon washing tower;
The exit end of the first heat exchanger channels of described plate-fin heat exchanger is divided into two-way, and one the tunnel connects the resurgent gases access road of dewatering system, and another road is gone outside the battery limit (BL);
The exit end of the second heat exchanger channels of described plate-fin heat exchanger is connected to downstream pipe network (for example natural gas liquefaction system);
The inlet end of the 3rd heat exchanger channels of described plate-fin heat exchanger connects the dehydration unstripped gas exit passageway of dewatering system, and exit end connects the dehydration unstripped gas access road of heavy hydrocarbon separator;
The 4th heat exchanger channels inlet end of plate-fin heat exchanger is connected with the heavy hydrocarbon exit passageway of heavy hydrocarbon separator; Exit end connects the second liquid phase access road of deethanizing column,
The lighter hydrocarbons exit passageway of described heavy hydrocarbon separator is connected with the gas phase access road of heavy hydrocarbon washing tower;
The heavy hydrocarbon exit passageway of described heavy hydrocarbon washing tower is connected to the input terminus of heavy hydrocarbon pump, and the heavy hydrocarbon delivery side of pump connects the first liquid phase access road of deethanizing column;
The heavy hydrocarbon exit passageway of described deethanizing column is connected with the liquid phase access road of described rectifying tower via a described throttling set;
The liquefied petroleum gas (LPG) exit passageway of described rectifying tower is connected to the liquefied petroleum gas product storage tank via an aftercooler; The light oil exit passageway of rectifying tower is connected to the light oil products storage tank after connecting the light oil water cooler.
Dewatering system can adopt this area sorption drying device commonly used, and preferred isobaric sorption drying device more preferably adopts the isobaric sorption drying device of two towers, and further preferred sorption drying device is filled the sorbent material that is selected from 3A or 4A molecular sieve, the activated alumina.The raw material shale gas can be with moisture removal to dew points at normal pressure≤-76 ℃ after the dehydration of described dewatering system.
As preferred embodiment, wherein sorption drying device comprises:
The first drying tower (T1) and the second drying tower (T2), the two alternately is in drying process and regenerative process the first drying tower and the second drying tower,
Resurgent gases well heater (E1),
Gas-liquid separator (V1), and
Resurgent gases water cooler (E2),
Each drying tower have one or two or a plurality of adsorbent bed,
The transfer lime of raw material shale gas is divided into two branch roads i.e. the first branch road and the second branch road, the first branch road is via ingress pipe, the first drying tower (T1) and the 4th valve (V4A) of first valve (V1A), the first drying tower (T1), and then the dehydration unstripped gas exit passageway by dewatering system leads to and takes off heavy hydrocarbon and heavy hydrocarbon treatment system; The second branch road is via ingress pipe, the second drying tower (T2) and the 8th valve (V4B) of the 5th valve (V1B), the second drying tower (T2), and then the dehydration unstripped gas exit passageway by dewatering system leads to and takes off heavy hydrocarbon and heavy hydrocarbon treatment system; Draw arm between first drying tower (T1) and the 4th valve (V4A) and between second drying tower (T2) and the 8th valve (V4B), drawing arm, these two arms converge an end that is connected to resurgent gases well heater (E1) afterwards via the 3rd valve (V3A) and the 7th valve (V3B) respectively, and the resurgent gases access road of the other end of resurgent gases well heater (E1) by dewatering system is connected to and takes off heavy hydrocarbon and heavy hydrocarbon treatment system; Draw arm between first drying tower (T1) and first valve (V1A) and between second drying tower (T2) and the 5th valve (V1B), drawing arm, these two arms converge afterwards via second valve (V2A) and the 6th valve (V2B) respectively, importing end via resurgent gases water cooler (E2), resurgent gases water cooler (E2), the derivation end of resurgent gases water cooler (E2) is connected to the ingress pipe of gas-liquid separator (V1), and the top delivery line of gas-liquid separator (V1) is connected to dewatering system resurgent gases exit passageway.
Generally, control the carrying out of each process by means of each program-controlled valve.
Preferably, the adsorbent bed independently filling of each of each drying tower is selected from one or more sorbent materials in 3A or 4A molecular sieve, the activated alumina.
As an embodiment, the gaseous phase outlet passage of described rectifying tower is at first via described aftercooler with randomly via a rectifying tower return tank, then tell two arms, an arm is connected with the liquefied petroleum gas product storage tank, and another arm, optional via a pump, be connected in the liquid phase access road that rectifying tower is established in addition.
Here, the liquid phase access road that rectifying tower is established in addition refer to except with liquid phase access road that a described throttling set is connected, the rectifying tower backflow liquid phase access road of setting.
At the bottom of the tower of described deethanizing column and/or described rectifying tower, can adopt the reboiler of any pattern, for example built-in, autoclave, thermosyphon reboiler.
Be used to plate-fin heat exchanger to provide the cryogen heat exchanger channels of cold to design connection according to the actual process demand.As an optimal way, be used to plate-fin heat exchanger to provide the cryogen heat exchanger channels of cold to have 2, i.e. the 5th, the 6th heat exchanger channels, the cryogen exit passageway that the 5th heat exchanger channels one end of plate-fin heat exchanger connects refrigeration compression system connects, the other end is connected with an end of the 6th heat exchanger channels via the first cryogen throttling set, and the other end of the 6th heat exchanger channels is connected to the cryogen access road of refrigeration compression system;
As another optimal way, be used to plate-fin heat exchanger to provide the cryogen heat exchanger channels of cold to have 3, i.e. the 5th, the 6th, the 7th heat exchanger channels, the inlet end of the inlet end of described the 5th heat exchanger channels and the 7th heat exchanger channels via two pipelines respectively with described refrigerant compression systems in the gas phase end of second stage gas-liquid separator be connected with the liquid phase end, and the exit end of the 6th heat exchanger channels is connected to the cryogen access road of the first compression section via pipeline; The exit end of the 7th heat exchanger channels of described plate-fin heat exchanger returns the 6th heat exchanger channels after via the first cryogen throttling set throttling; The exit end of the 5th heat exchanger channels of described plate-fin heat exchanger is connected with the inlet end of the 6th heat exchanger channels via the second cryogen throttling set.For example, as cold C1～C5 and N 2When the azeotrope that forms provided, the liquid phase cryogen entered the 7th heat exchanger channels of plate-fin heat exchanger, was chilled in advance therein-30 ℃～-80 ℃ approximately, returned the 6th heat exchanger channels of plate-fin heat exchanger behind first cryogen throttling set throttling to 0.2～0.8MPaA; The 5th heat exchanger channels that the gas phase cryogen enters plate-fin heat exchanger is cooled to-135 ℃～-169 ℃, oppositely enter the 6th heat exchanger channels heat exchange of plate-fin heat exchanger behind second cryogen throttling set throttling to 0.2～0.8MPaA, re-heat is returned cryogen to the certain temperature system is provided again.
Preferably, the required cold of plate-fin heat exchanger by or mainly provided by the mix refrigerant circulation, azeotrope is for example by C1～C5 and N 2Form, usually be selected from C1, C2, C3, C4 and C5 paraffinic hydrocarbons and N 2In four kinds, five kinds or six kinds, they mix according to the arbitrary volume ratio or according to the volume ratio that approximately is equal to, hybrid refrigeration cycle removes heavy hydrocarbon for shale gas low temperature simultaneously and purifies shale gas liquefaction provides cold.
As optimal way, described refrigerant compression systems comprises two-section type mixing medium compressor, is connected respectively the first step gas-liquid separator and second stage gas-liquid separator and a liquor pump that is connected with first step gas-liquid separator that is connected with second-stage cooler with described first step water cooler with second-stage cooler with the first step water cooler that the first paragraph of described two-section type mixing medium compressor is connected with second segment respectively
The interchanger that is used to of described plate-fin heat exchanger provides 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, the inlet end of the inlet end of described the 5th heat exchanger channels and the 7th heat exchanger channels via two pipelines respectively with described refrigerant compression systems in the gas phase end of second stage gas-liquid separator be connected with the liquid phase end, and the exit end of the 6th heat exchanger channels is connected to the cryogen access road of the first compression section via pipeline;
The exit end of the 5th heat exchanger channels of described plate-fin heat exchanger is connected with the inlet end of the 6th heat exchanger channels via the second cryogen throttling set, and the exit end of the 7th heat exchanger channels of described plate-fin heat exchanger returns the 6th heat exchanger channels after via the first cryogen throttling set throttling;
Wherein the gas phase end of the first step gas-liquid separator in two gas-liquid separators is connected with the second compression section of two-section type mixing medium compressor, and the liquid phase end of first step 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.
In this application " adsorption dry " be used interchangeably with " dry absorption ".Term " is chosen " expression wantonly and is with or without.
Employed unstripped gas refers to the raw material shale gas.In this application, C1, C2, C3, C4, C5, C6 philosophy represent the hydro carbons (or paraffinic) of corresponding carbonatoms.C3 among the application +Refer to contain three and three hydro carbons (or paraffinic) that carbonatoms is above." be mainly " in this application and refer to more than the 50wt% that more than the preferred 70wt%, or more than the preferred 80wt%, more preferably more than the 90wt%, for example 95wt% is above is made of this component.Refer to more than the 50wt% that such as " being mainly C1, C2 hydrocarbon etc. " more than the preferred 70wt%, or more than the preferred 80wt%, more preferably more than the 90wt%, for example 95wt% is above is made of C1, C2 hydrocarbon; Liquid phase is mainly C3, C4, C5, C6 at the bottom of the deethanizing Tata +Mixture refer to more than the 50wt% of liquid phase at the bottom of the deethanizing Tata that more than the preferred 70wt%, or more than the preferred 80wt%, more preferably more than the 90wt%, for example 95wt% is above by C3, C4, C5, C6 +Mixture consist of.
Advantage of the present invention:
1, the method for the present invention's employing removes the moisture in the shale gas and heavy hydrocarbon component, and heavy hydrocarbon component is processed recovery, obtains LPG and light oil byproduct, and is viable economically;
2, adopt two tower flow process adsorption dewaterings, flow process is simple than three towers, and saves facility investment;
3, by adopting the isobaric absorbing process flow process of two towers, can be with the moisture removal in the shale gas to dew points at normal pressure≤-76 ℃, preferred≤-78 ℃, more preferably≤-80 ℃;
4, the heavy hydrocarbon washing tower washing flow that usually adopts in compared to existing technology, flow process of the present invention is stronger to the adaptability of heavy hydrocarbon component fluctuation in the unstripped gas;
5, heavy hydrocarbon component removes thoroughly, and after processing, heavy hydrocarbon component is C6 for example +Deng heavy hydrocarbon component, basically be removed,, for example≤and 150ppm, preferred≤100ppm, more preferably≤80ppm, more preferably≤50ppm.
6, cold and hot fluid heat exchange highway route design is reasonable, realizes the rational Match of fluid cold, heat, makes the plant energy consumption reduce.
Description of drawings
Fig. 1 is the process flow sheet that shale gas of the present invention takes off heavy hydrocarbon;
Fig. 2 is a kind of process flow sheet of refrigerant compression systems.
1, dewatering system 2, take off shale gas 5 after heavy hydrocarbon and heavy hydrocarbon treatment system 3, raw material shale gas 4, the dehydration, finish the resurgent gases 6 of regeneration, shale gas 7, resurgent gases 8, LNG9, LPG10, light oil after purifying
V1A/B, V2A/B, V3A/B, V4A/B, program-controlled valve V-1, the first cryogen throttling set V-2, the second cryogen throttling set V-3, throttling set V1, gas-liquid separator V2, heavy hydrocarbon separator V3, rectifying tower return tank V4, first step gas-liquid separator V5, second stage gas-liquid separator E1, resurgent gases well heater E2, resurgent gases water cooler E3, plate-fin heat exchanger E4, lighter hydrocarbons interchanger E5, light oil water cooler E6, deethanizing column reboiler E7, rectifying tower reboiler E8, rectifying tower top condenser E10, first step water cooler E11, second-stage cooler T1, the first drying tower T2, the second drying tower T3, heavy hydrocarbon washing tower T4, deethanizing column T5, rectifying tower P1, heavy hydrocarbon pump P2, rectifying tower reflux pump P3, liquor pump C1, coolant compressor
Embodiment
Method of the present invention comprises dehydration procedure and takes off heavy hydrocarbon and heavy hydrocarbon treatment process two portions; Dehydration procedure comprises that the isobaric absorbing process flow process of employing removes the moisture content in the shale gas, and the purification shale gas after heavy hydrocarbon is taken off in dehydration is as resurgent gases; Take off heavy hydrocarbon and heavy hydrocarbon treatment process and comprise that the shale gas after the dehydration removes heavy hydrocarbon successively in heavy hydrocarbon separator and heavy hydrocarbon washing tower, and the heavy hydrocarbon that is removed enters successively stripping in the deethanizing column and removes wherein light constituent (being mainly C1, C2 hydrocarbon etc.), enters and be separated into LPG and light oil byproduct in the rectifying tower.Shale gas dew points at normal pressure after heavy hydrocarbon is taken off in dehydration is down to≤-76 ℃, the above heavy hydrocarbon component of C6 and C6 be removed to the soluble degree of LNG (for example≤150ppm, preferred≤100ppm, more preferably≤80ppm); And obtain simultaneously liquefied petroleum gas (LPG) (LPG) and light oil byproduct, economically feasible, operational path advanced person.
Referring to accompanying drawing 1, accompanying drawing 2, the method that shale gas provided by the invention takes off heavy hydrocarbon is as follows:
Dewatering system 1 adopts the isobaric absorbing process flow process of two towers, and the water adsorption in the 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 two tower paralleling models, and wherein tower T1 is in adsorption process and another tower T2 is in regenerative process.Take drying tower T1 as example, illustrate that the isobaric absorbing process flow process of two towers is as follows:
A, adsorption process: raw material shale gas 3 enters the drying tower T1 that is in adsorbed state through valve V1A self-desiccation tower T1 top.Under the selection absorption of sorbent material, component to be removed wherein is that moisture is adsorbed, and the gas that is not adsorbed goes heavy hydrocarbon and heavy hydrocarbon treatment system through valve V4A at the bottom of tower.When the mass transfer zone forward position (being called absorb leading-edge) that is adsorbed impurity arrives bed outlet reservation section, turn off unstripped gas feed valve V1A and the unstripped gas outlet valve V4A of this drying tower T1, stop absorption, adsorption bed begins to change over to regenerative process.
The regeneration of drying tower T1 comprise successively heat, the cold blowing process.
B, heat-processed: resurgent gases 4 is after resurgent gases well heater E1 is heated to certain temperature (for example 230～250 ℃), entering drying tower T1 through valve V3A heats, reverse purging is adsorbent bed, and the impurity that is adsorbed on the sorbent material is desorbed fully, makes the sorbent material among the T1 obtain regeneration; Go out the resurgent gases of drying tower T1 successively through valve V2A, resurgent gases water cooler E2, gas-liquid separator V1 cooling, separatory, finish resurgent gases 5 emptying of regeneration or further send to the downstream pipe network after the processing, heat-processed finishes.
C, cold blowing process: after heat-processed finishes, resurgent gases well heater E1 stopped heating, resurgent gases 4 enters the drying tower T1 that is in the cold blowing process, and reverse purging is adsorbent bed, makes bed be down to certain temperature (for example about 40 ℃); Go out the resurgent gases of drying tower T1 successively through valve V2A, resurgent gases water cooler E2, gas-liquid separator V1 cooling, separatory, finish resurgent gases 5 emptying of regeneration or further send to the downstream pipe network, the cold blowing end of processing after the processing.
Drying tower T1 has just finished complete " adsorption-regeneration " circulation after this process, for next time absorption is got ready.
The absorption of drying tower T2 and regenerative process and drying tower T1 are identical, realize that by the action of controlling different valves two cone pulley flow operations reach the purpose of continuous purification gas.Its process is as follows:
A, adsorption process: raw material shale gas 3 enters the drying tower T2 that is in adsorbed state through valve V1B self-desiccation tower T2 top.Under the selection absorption of sorbent material, component to be removed wherein is that moisture is adsorbed, and the gas that is not adsorbed goes heavy hydrocarbon and heavy hydrocarbon treatment system through valve V4B at the bottom of tower.When the mass transfer zone forward position (being called absorb leading-edge) that is adsorbed impurity arrives bed outlet reservation section, turn off unstripped gas feed valve V1B and the unstripped gas outlet valve V4B of this drying tower T2, stop absorption, adsorption bed begins to change over to regenerative process.
The regeneration of drying tower T2 comprise successively heat, the cold blowing process.
B, heat-processed: resurgent gases 4 is after resurgent gases well heater E1 is heated to certain temperature (for example 230～250 ℃), entering drying tower T2 through valve V3B heats, reverse purging is adsorbent bed, and the impurity that is adsorbed on the sorbent material is desorbed fully, makes the sorbent material among the T2 obtain regeneration; Go out the resurgent gases of drying tower T2 successively through valve V2B, resurgent gases water cooler E2, gas-liquid separator V1 cooling, separatory, finish resurgent gases 5 emptying of regeneration or further send to the downstream pipe network after the processing, heat-processed finishes.
C, cold blowing process: after heat-processed finishes, resurgent gases well heater E1 stopped heating, resurgent gases 4 enters the drying tower T2 that is in the cold blowing process, and reverse purging is adsorbent bed, makes bed be down to certain temperature (for example about 40 ℃); Go out the resurgent gases of drying tower T2 successively through valve V2B, resurgent gases water cooler E2, gas-liquid separator V1 cooling, separatory, finish resurgent gases 5 emptying of regeneration or further send to the downstream pipe network, the cold blowing end of processing after the processing.
Drying tower T2 has just finished complete " adsorption-regeneration " circulation after this process, for next time absorption is got ready.
The technical process of taking off heavy hydrocarbon and heavy hydrocarbon treatment system 2 is as follows:
Shale gas 4 after the dehydration enters and takes off heavy hydrocarbon and heavy hydrocarbon treatment system 2, at plate-fin heat exchanger E3(the 3rd heat exchanger channels) in enter heavy hydrocarbon separator V2 after being cooled to-60～-80 ℃, the C3 that heavy hydrocarbon separator V2 separates the bottom +Heavy hydrocarbon component returns plate-fin heat exchanger E3(the 4th heat exchanger channels) re-heat to normal temperature, enter among the deethanizing column T4, reclaim C3 +The C1 that carries in the heavy hydrocarbon component, C2 hydrocarbon etc.; The isolated gas phase in heavy hydrocarbon separator V2 top enters heavy hydrocarbon washing tower T3, with the cooled logistics mass-and heat-transfer of deethanizing column T4 top gas phase, finally obtains light constituent and the C3 such as C1, C2 respectively at the bottom of heavy hydrocarbon washing tower T3 cat head, tower in heavy hydrocarbon washing tower T3 +Heavy hydrocarbon component; The C1 that heavy hydrocarbon washing tower T3 cat head obtains,-60～-80 ℃ approximately of the light constituent temperature such as C2, enter and be divided into two-way after cold is reclaimed in gas phase heat exchange that lighter hydrocarbons interchanger E4 and deethanizing column T4 cat head tell, one the tunnel returns plate-fin heat exchanger E3(the second heat exchanger channels) liquefying becomes natural gas liquids (LNG) 8, plate-fin heat exchanger E3(the first heat exchanger channels is returned on another road) re-heat is to normal temperature, (the above heavy hydrocarbon component of C6 and C6 for example is removed to≤150ppm to be the purified gas that takes off behind the heavy hydrocarbon, preferably≤100ppm, more preferably≤80ppm), go dewatering system as resurgent gases 4 from wherein telling one the tunnel, all the other purified gass 6 go outside the battery limit (BL); Heavy hydrocarbon washing tower T3 bottom liquid phases is pressurized to 2.0MPaA～4.0MPaA through heavy hydrocarbon pump P1, then enters deethanizing column T4 and removes wherein light constituent (being mainly C1, C2 hydrocarbon etc.); The light constituent that deethanizing column T4 tells at the top enters lighter hydrocarbons interchanger E4, is cooled to-60～-80 ℃ with the heat exchange of heavy hydrocarbon washing tower T3 top gaseous phase, enters heavy hydrocarbon washing tower T3; Liquid phase (is mainly C3, C4, C5, C6 at the bottom of the deethanizing column T4 tower +Mixture) after the 3rd throttling set V-3 is decompressed to 0.5MPaA～2.0MPaA, enter rectifying tower T5 middle part, obtain the mixture of the components such as C3, C4 from cat head through rectifying, partial reflux, the part extraction is the LPG product, separates obtaining C5, C6 at the bottom of the tower +Etc. the mixture of component, after light oil water cooler E5 is cooled to normal temperature, be the light oil byproduct.
Preferably, the required cold of plate-fin heat exchanger E3 by or mainly provided by refrigerant compression systems, refrigerant compression systems removes heavy hydrocarbon for shale gas low temperature simultaneously and purifies shale gas liquefaction provides cold; 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 water cooler E10, E11, two gas-liquid separator V4, V5 and a 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 the refrigeration agent of one or more compositions enter the entrance of refrigerant compression systems, be compressed to 0.6～1.8MPaA through first paragraph, enter first step water cooler E10 and be cooled to 30 ℃～45 ℃, enter again first step gas-liquid separator V4 and carry out gas-liquid separation, the isolated gas in first step gas-liquid separator V4 top continues to enter the second segment entrance of compressor, be compressed to 1.2～5.4MPaA through two sections, the isolated liquid of first step gas-liquid separator V4 bottom liquid phases end is after converging with the hot gas of second segment compression outlet conduit after the liquor pump P3 pressurization, enter again and be cooled to 30 ℃～45 ℃ among the second-stage cooler E11, cooled refrigeration agent enters subsequently second stage gas-liquid separator V5 and carries out gas-liquid separation, the 5th heat exchanger channels that the top gas of second stage gas-liquid separator V5 enters plate-fin heat exchanger E3 subsequently participates in heat exchange, and the 7th heat exchanger channels that the isolated liquid in second stage gas-liquid separator V5 bottom enters plate-fin heat exchanger E3 participates in heat exchange;
As shown in Figures 1 and 2, the liquid refrigerant that goes out refrigerant compression systems enters the 7th heat exchanger channels of plate-fin heat exchanger E3 in the accompanying drawing 1 through liquid phase cryogen exit passageway, be chilled in advance therein-30 ℃～-80 ℃ approximately, behind first cryogen throttling set V-1 throttling to 0.2～0.8MPaA, returned the 6th heat exchanger channels of plate-fin heat exchanger E3; The gas refrigerant that goes out refrigerant compression systems enters through gas phase cryogen exit passageway that the 5th heat exchanger channels of plate-fin heat exchanger E3 is cooled to-135 ℃～-169 ℃ in the accompanying drawing 1, the 6th heat exchanger channels heat exchange that oppositely enters plate-fin heat exchanger E3 again behind second cryogen throttling set V-2 throttling to 0.2～0.8MPaA, re-heat to normal temperature returns refrigerant compression systems by the access road of refrigerant compression systems.
Can adopt the arbitrarily reboiler of pattern such as built-in, autoclave, heat siphon type at the bottom of the tower of deethanizing column T4 and rectifying tower T5.
Here, pressure unit MPaA is MPa, absolute pressure.
Adopt except the technical process of the described mix refrigerant compression system of this patent, for plate-fin heat exchanger E3 provides the device of the technical process of cold, also belong to the protection domain of this patent.

Claims (13)

1. the method that shale gas takes off heavy hydrocarbon is characterized in that, the method comprises dehydration procedure and takes off heavy hydrocarbon and heavy hydrocarbon treatment process two portions;
Dehydration procedure comprises that the isobaric absorbing process flow process of employing removes the moisture content in the raw material shale gas, and the purification shale gas after heavy hydrocarbon is taken off in dehydration is as the resurgent gases in the dehydration procedure; Take off heavy hydrocarbon and heavy hydrocarbon treatment process and comprise that the shale gas after the dehydration removes heavy hydrocarbon successively after the plate-fin heat exchanger cooling in heavy hydrocarbon separator and heavy hydrocarbon washing tower, the heavy hydrocarbon that is removed enters successively stripping in the deethanizing column and removes wherein light constituent, wherein enter the heavy hydrocarbon washing tower and separate again in the lighter hydrocarbons interchanger with after the isolated shale gas heat exchange that removes heavy hydrocarbon of heavy hydrocarbon washing tower cat head from the light constituent of deethanizing column, wherein divide to enter from the restructuring of deethanizing column and isolate light oil and gas phase in the rectifying tower, this gas phase is cooled into liquefied petroleum gas (LPG); With from the isolated heavy hydrocarbon shale gas that takes off of heavy hydrocarbon washing tower cat head after the heat exchange of lighter hydrocarbons interchanger, liquefaction obtains namely dewater shale gas behind the heavy hydrocarbon of natural gas liquids in the part Returning plate fin heat exchanger, goes dehydration procedure as resurgent gases after the heat exchange in the part Returning plate fin heat exchanger; Take off shale gas dew points at normal pressure behind the heavy hydrocarbon to be down to≤-76 ℃, the above heavy hydrocarbon component of C6 and C6 is removed to the soluble degree of LNG.
2. shale gas according to claim 1 takes off the method for heavy hydrocarbon, it is characterized in that, dehydration procedure adopts the isobaric absorbing process flow process of two towers, utilizes in activated alumina, 3A molecular sieve or the 4A molecular sieve one or more as sorbent material, and the water adsorption in the raw material shale gas is got off.
3. described shale gas takes off the method for heavy hydrocarbon according to claim 1-2, it is characterized in that, sends to gas distributing system after emptying or further the processing behind the resurgent gases regeneration ending of dehydration procedure.
4. described shale gas takes off the method for heavy hydrocarbon according to claim 1-3, it is characterized in that, in taking off heavy hydrocarbon and heavy hydrocarbon separation circuit, the shale gas after the dehydration enters the heavy hydrocarbon separator after entering in the plate-fin heat exchanger and be cooled to-60～-80 ℃, the C3 that separate heavy hydrocarbon separator bottom +Heavy hydrocarbon component returns the plate-fin heat exchanger re-heat and enters in the deethanizing column to normal temperature, reclaims C3 +The light constituent that comprises C1, C2 hydrocarbon that carries in the heavy hydrocarbon component; The isolated gas phase in heavy hydrocarbon separator top enters the heavy hydrocarbon washing tower, in the heavy hydrocarbon washing tower with the cooled logistics mass-and heat-transfer of deethanizing column top gas phase, final light constituent and the C3 that obtains comprising respectively C1, C2 at the bottom of heavy hydrocarbon washing tower cat head, the tower +Heavy hydrocarbon component; Temperature that the heavy hydrocarbon scrubber overhead obtains is after-60～-80 ℃ the light constituent that comprises C1, C2 enters the gas phase heat exchange recovery cold that lighter hydrocarbons interchanger and deethanizing cat head tell approximately, part is returned plate-fin heat exchanger liquefaction becomes natural gas liquids, part is returned the plate-fin heat exchanger re-heat to normal temperature, be the shale gas that takes off behind the heavy hydrocarbon, tell one the tunnel and go dehydration procedure as resurgent gases, optional tell another road and go outside the battery limit (BL); Heavy hydrocarbon wash tower bottoms liquid phase is pressurized to 2.0MPaA～4.0MPaA through the heavy hydrocarbon pump, then enters deethanizing column and removes wherein the light constituent that is mainly C1, C2 hydrocarbon; The light constituent that the deethanizing column top is told enters the lighter hydrocarbons interchanger and the heat exchange of heavy hydrocarbon washing tower top gaseous phase is cooled to-60～-80 ℃, enters the heavy hydrocarbon washing tower; Be mainly C3, C4, C5, C6 +The deethanizing Tata of mixture at the bottom of liquid phase after throttling set is decompressed to 0.5MPaA～2.0MPaA, enter the rectifying tower middle part, separate obtaining light oil products and obtaining gas phase from cat head at the bottom of the tower through rectifying, then this gas phase is cooled into liquefied petroleum gas (LPG).
5. the method that any one described shale gas takes off heavy hydrocarbon according to claim 1-4, it is characterized in that, the required cold of plate-fin heat exchanger by or mainly provided by refrigerant compression systems, refrigerant compression systems removes heavy hydrocarbon for shale gas low temperature simultaneously and purifies shale gas liquefaction provides cold;
By C1～C5 and N 2In the refrigeration agent of one or more compositions enter the entrance of refrigerant compression systems, be compressed to 0.6～1.8MPaA through first paragraph, enter first step water cooler and be cooled to 30 ℃～45 ℃, enter again first step gas-liquid separator and carry out gas-liquid separation, the isolated gas in first step gas-liquid separator top continues to enter the second segment entrance of compressor, be compressed to 1.2～5.4MPaA through two sections, the isolated liquid of first step gas-liquid separator bottom liquid phases end is after converging with the hot gas of second segment compression outlet conduit after the liquor pump pressurization, enter again and be cooled to 30 ℃～45 ℃ in the second-stage cooler, cooled refrigeration agent enters subsequently second stage gas-liquid separator and carries out gas-liquid separation, and the cryogen heat exchanger channels that the isolated liquid in the top gas of second stage gas-liquid separator and bottom enters plate-fin heat exchanger participates in heat exchange;
Preferably, the liquid of drawing bottom the gas-liquid separator of the second stage at first enters the liquid phase cryogen heat exchanger channels of plate-fin heat exchanger, is chilled in advance therein-30 ℃～-80 ℃ approximately, enters the cryogen separator behind first throttle device throttling to 0.2～0.8MPaA; Be cooled to-135 ℃～-169 ℃ by the vapor phase stream thigh of the isolated refrigeration agent in gas-liquid separator top, the described second stage gas phase cryogen heat exchanger channels by plate-fin heat exchanger, behind second throttling set throttling to 0.2～0.8MPaA, oppositely enter again the other heat exchanger channels heat exchange of plate-fin heat exchanger, for plate-fin heat exchanger provides cold and then turns back to coolant compressor the first compression section.
6. technique according to claim 1-5 is characterized in that, adopts the reboiler of built-in, autoclave, any pattern of heat siphon type at the bottom of the tower of deethanizing column and rectifying tower.
7. a shale gas takes off the device of heavy hydrocarbon, and it is characterized in that: described device comprises dewatering system and takes off heavy hydrocarbon and the heavy hydrocarbon treatment system;
Wherein
Dewatering system comprises: sorption drying device, a unstripped gas access road, a dehydration unstripped gas exit passageway, a resurgent gases access road, a resurgent gases exit passageway;
Take off heavy hydrocarbon and the heavy hydrocarbon treatment system comprises: a heavy hydrocarbon separator, a heavy hydrocarbon washing tower, a deethanizing column, rectifying tower, a platen wing interchanger, a lighter hydrocarbons interchanger, a throttling set, a light oil water cooler and a heavy hydrocarbon pump;
Described plate-fin heat exchanger comprises following heat exchanger channels at least: the first heat exchanger channels, the second heat exchanger channels, the 3rd heat exchanger channels, the 4th heat exchanger channels and be used to interchanger that the cryogen heat exchanger channels of cold is provided;
Described heavy hydrocarbon separator comprises a dehydration unstripped gas access road, a heavy hydrocarbon exit passageway and a lighter hydrocarbons exit passageway;
Described heavy hydrocarbon washing tower comprises a gas phase access road, a mixed phase access road, a gaseous phase outlet passage, a heavy hydrocarbon exit passageway;
Described deethanizing column comprises the first liquid phase access road, second liquid phase access road, a gaseous phase outlet passage, a heavy hydrocarbon exit passageway;
Described rectifying tower comprises a heavy hydrocarbon access road, a liquefied petroleum gas (LPG) exit passageway, a light oil exit passageway;
Described lighter hydrocarbons interchanger comprises the first and second two heat exchanger channels at least; The inlet end of the first heat exchanger channels of lighter hydrocarbons interchanger is connected with the gaseous phase outlet passage of heavy hydrocarbon washing tower, the exit end of the first heat exchanger channels of lighter hydrocarbons interchanger is divided into two-way, respectively with the inlet end of the first heat exchanger channels of described plate-fin heat exchanger be connected the inlet end of heat exchanger channels and be connected, the inlet end of the second heat exchanger channels of lighter hydrocarbons interchanger is connected with the gaseous phase outlet passage of described deethanizing column, and the exit end of the second heat exchanger channels of lighter hydrocarbons interchanger is connected with the mixed phase access road of described heavy hydrocarbon washing tower;
The exit end of the first heat exchanger channels of described plate-fin heat exchanger is divided into two-way, and one the tunnel connects the resurgent gases access road of dewatering system, and another road is gone outside the battery limit (BL);
The exit end of the second heat exchanger channels of described plate-fin heat exchanger is connected to downstream pipe network (for example natural gas liquefaction system);
The inlet end of the 3rd heat exchanger channels of described plate-fin heat exchanger connects the dehydration unstripped gas exit passageway of dewatering system, and exit end connects the dehydration unstripped gas access road of heavy hydrocarbon separator;
The 4th heat exchanger channels inlet end of plate-fin heat exchanger is connected with the heavy hydrocarbon exit passageway of heavy hydrocarbon separator; Exit end connects the second liquid phase access road of deethanizing column,
The lighter hydrocarbons exit passageway of described heavy hydrocarbon separator is connected with the gas phase access road of heavy hydrocarbon washing tower;
The heavy hydrocarbon exit passageway of described heavy hydrocarbon washing tower is connected to the input terminus of heavy hydrocarbon pump, and the heavy hydrocarbon delivery side of pump connects the first liquid phase access road of deethanizing column;
The heavy hydrocarbon exit passageway of described deethanizing column is connected with the liquid phase access road of described rectifying tower via the First throttling set;
The liquefied petroleum gas (LPG) exit passageway of described rectifying tower is connected to the liquefied petroleum gas product storage tank via an aftercooler; The light oil exit passageway of rectifying tower is connected to the light oil products storage tank after connecting the light oil water cooler.
8. shale gas dehydration de-heavy hydrocarbon apparatus according to claim 7 is characterized in that, described dewatering system adopts the isobaric absorption drying system of two towers.
9. shale gas according to claim 8 dehydration de-heavy hydrocarbon apparatus is characterized in that the sorption drying device of described dewatering system comprises:
The first drying tower (T1) and the second drying tower (T2), the two alternately is in drying process and regenerative process the first drying tower and the second drying tower,
Resurgent gases well heater (E1),
Gas-liquid separator (V1), and
Resurgent gases water cooler (E2),
Each drying tower have one or two or a plurality of adsorbent bed,
The transfer lime of raw material shale gas is divided into two branch roads i.e. the first branch road and the second branch road, the first branch road is via first valve (V1A), the ingress pipe of the first drying tower (T1), the first drying tower (T1) and the 4th valve (V4A), then the dehydration unstripped gas exit passageway by dewatering system leads to and takes off heavy hydrocarbon and heavy hydrocarbon treatment system, the second branch road is via the 5th valve (V1B), the ingress pipe of the second drying tower (T2), the second drying tower (T2) and the 8th valve (V4B), then the dehydration unstripped gas exit passageway by dewatering system leads to and takes off heavy hydrocarbon and heavy hydrocarbon treatment system; Draw arm between first drying tower (T1) and the 4th valve (V4A) and between second drying tower (T2) and the 8th valve (V4B), drawing arm, these two arms converge an end that is connected to resurgent gases well heater (E1) afterwards via the 3rd valve (V3A) and the 7th valve (V3B) respectively, and the resurgent gases access road of the other end of resurgent gases well heater (E1) by dewatering system is connected to and takes off heavy hydrocarbon and heavy hydrocarbon treatment system; Draw arm between first drying tower (T1) and first valve (V1A) and between second drying tower (T2) and the 5th valve (V1B), drawing arm, these two arms converge afterwards via second valve (V2A) and the 6th valve (V2B) respectively, importing end via resurgent gases water cooler (E2), resurgent gases water cooler (E2), the derivation end of resurgent gases water cooler (E2) is connected to the ingress pipe of gas-liquid separator (V1), and the top delivery line of gas-liquid separator (V1) is connected to dewatering system resurgent gases exit passageway.
10. the described device of any one according to claim 7-9 is characterized in that: the sorbent material in the described sorption drying device is the sorbent material that is selected from 3A or 4A molecular sieve, the activated alumina.
11. the described device of any one according to claim 7-9, it is characterized in that: the gaseous phase outlet passage of described rectifying tower is at first via aftercooler with randomly via a rectifying tower return tank, then tell two arms, an arm is connected with the liquefied petroleum gas product storage tank, and another arm, optional via a pump, what be connected in rectifying tower establishes the liquid phase access road in addition.
12. the described device of any one according to claim 7-9 is characterized in that: adopt built-in, autoclave or thermosyphon reboiler at the bottom of the tower of described deethanizing column and/or described rectifying tower.
13. the described device of any one according to claim 7-9, it is characterized in that: the cold in the described plate-fin heat exchanger is provided by refrigerant compression systems, described refrigerant compression systems comprises two-section type mixing medium compressor, the first step water cooler and the second-stage cooler that are connected with second segment with the first paragraph of described two-section type mixing medium compressor respectively, the first step gas-liquid separator and second stage gas-liquid separator and a liquor pump that is connected with first step gas-liquid separator that are connected with second-stage cooler with described first step water cooler respectively
The interchanger that is used to of described plate-fin heat exchanger provides 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, the inlet end of the inlet end of described the 5th heat exchanger channels and the 7th heat exchanger channels via two pipelines respectively with described refrigerant compression systems in the gas phase end of second stage gas-liquid separator be connected with the liquid phase end, and the exit end of the 6th heat exchanger channels is connected to the cryogen access road of the first compression section via pipeline;
The exit end of the 5th heat exchanger channels of described plate-fin heat exchanger is connected with the inlet end of the 6th heat exchanger channels via the second cryogen throttling set, and the exit end of the 7th heat exchanger channels of described plate-fin heat exchanger returns the 6th heat exchanger channels after via the first cryogen throttling set throttling;
Wherein the gas phase end of the first step gas-liquid separator in two gas-liquid separators is connected with the second compression section of two-section type mixing medium compressor, is connected to the second-stage cooler in described two water coolers after the liquid phase end of first step gas-liquid separator converges via the outlet conduit of liquor pump and the second compression section.
CN201310224727.3A 2013-06-07 2013-06-07 Method and device for removing water and heavy hydrocarbons from shale gas Active CN103351896B (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
CN201310224727.3A CN103351896B (en) 2013-06-07 2013-06-07 Method and device for removing water and heavy hydrocarbons from shale gas

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
CN201310224727.3A CN103351896B (en) 2013-06-07 2013-06-07 Method and device for removing water and heavy hydrocarbons from shale gas

Publications (2)

Publication Number Publication Date
CN103351896A true CN103351896A (en) 2013-10-16
CN103351896B CN103351896B (en) 2015-05-06

Family

ID=49308311

Family Applications (1)

Application Number Title Priority Date Filing Date
CN201310224727.3A Active CN103351896B (en) 2013-06-07 2013-06-07 Method and device for removing water and heavy hydrocarbons from shale gas

Country Status (1)

Country Link
CN (1) CN103351896B (en)

Cited By (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN104726127A (en) * 2015-03-31 2015-06-24 西安长庆科技工程有限责任公司 Refined heavy-hydrocarbon removal system for recovering LNG/LPG/NGL from petroleum associated gas
CN104748463A (en) * 2013-12-25 2015-07-01 新地能源工程技术有限公司 Mixed refrigerant recovering and supplementing method and device
CN106237783A (en) * 2016-08-31 2016-12-21 成都赛普瑞兴科技有限公司 A kind of de-heavy hydrocarbon system of absorption method dehydration
CN107042051A (en) * 2017-01-10 2017-08-15 杨皓 Preliminary clearning prevents frozen block technique before a kind of methanation LNG liquefaction
CN107726731A (en) * 2017-10-26 2018-02-23 枣庄学院 The liquefied natural gas (LNG) production device and its production technology of a kind of anti-frozen block
CN110180322A (en) * 2019-06-05 2019-08-30 杨皓 A kind of technique obtaining highly concentrated unsaturated component mixed gas from off-gas
CN111456702A (en) * 2019-01-18 2020-07-28 中国石油天然气股份有限公司 Oil-gas separation system and method
CN112812869A (en) * 2020-12-22 2021-05-18 中国石油天然气集团有限公司 Natural gas dehydration and dealkylation integrated device and method
CN117106499A (en) * 2023-10-23 2023-11-24 陕西航天德林科技集团有限公司 Oilfield associated gas comprehensive utilization system and process

Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN101508923A (en) * 2009-03-12 2009-08-19 西安长庆科技工程有限责任公司 De-heavy hydrocarbon apparatus and process for gas dehydration
US20110192190A1 (en) * 2008-09-23 2011-08-11 Diki Andrian Process for removing gaseous contaminants from a feed gas stream comprising methane and gaseous contaminants
CN102643694A (en) * 2012-04-27 2012-08-22 新地能源工程技术有限公司 Technique and device for drying and liquefaction of natural gas
CN103031169A (en) * 2012-12-13 2013-04-10 新地能源工程技术有限公司 Method and device for carrying out liquefaction and heavy hydrocarbon treatment on natural gas
CN203319964U (en) * 2013-06-07 2013-12-04 新地能源工程技术有限公司 Device for removing water and heavy hydrocarbon out of shale gas

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20110192190A1 (en) * 2008-09-23 2011-08-11 Diki Andrian Process for removing gaseous contaminants from a feed gas stream comprising methane and gaseous contaminants
CN101508923A (en) * 2009-03-12 2009-08-19 西安长庆科技工程有限责任公司 De-heavy hydrocarbon apparatus and process for gas dehydration
CN102643694A (en) * 2012-04-27 2012-08-22 新地能源工程技术有限公司 Technique and device for drying and liquefaction of natural gas
CN103031169A (en) * 2012-12-13 2013-04-10 新地能源工程技术有限公司 Method and device for carrying out liquefaction and heavy hydrocarbon treatment on natural gas
CN203319964U (en) * 2013-06-07 2013-12-04 新地能源工程技术有限公司 Device for removing water and heavy hydrocarbon out of shale gas

Cited By (13)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN104748463A (en) * 2013-12-25 2015-07-01 新地能源工程技术有限公司 Mixed refrigerant recovering and supplementing method and device
CN104748463B (en) * 2013-12-25 2017-04-05 新地能源工程技术有限公司 A kind of mix refrigerant is reclaimed and compensation process and device
CN104726127A (en) * 2015-03-31 2015-06-24 西安长庆科技工程有限责任公司 Refined heavy-hydrocarbon removal system for recovering LNG/LPG/NGL from petroleum associated gas
CN104726127B (en) * 2015-03-31 2016-08-24 西安长庆科技工程有限责任公司 A kind of loss of essence heavy hydrocarbon system reclaiming LNG/LPG/NGL for oil field gas
CN106237783A (en) * 2016-08-31 2016-12-21 成都赛普瑞兴科技有限公司 A kind of de-heavy hydrocarbon system of absorption method dehydration
CN107042051A (en) * 2017-01-10 2017-08-15 杨皓 Preliminary clearning prevents frozen block technique before a kind of methanation LNG liquefaction
CN107726731A (en) * 2017-10-26 2018-02-23 枣庄学院 The liquefied natural gas (LNG) production device and its production technology of a kind of anti-frozen block
CN111456702A (en) * 2019-01-18 2020-07-28 中国石油天然气股份有限公司 Oil-gas separation system and method
CN110180322A (en) * 2019-06-05 2019-08-30 杨皓 A kind of technique obtaining highly concentrated unsaturated component mixed gas from off-gas
CN110180322B (en) * 2019-06-05 2022-02-22 杨皓 Process for obtaining high-concentration unsaturated component mixed gas from purge gas
CN112812869A (en) * 2020-12-22 2021-05-18 中国石油天然气集团有限公司 Natural gas dehydration and dealkylation integrated device and method
CN117106499A (en) * 2023-10-23 2023-11-24 陕西航天德林科技集团有限公司 Oilfield associated gas comprehensive utilization system and process
CN117106499B (en) * 2023-10-23 2024-02-23 陕西航天德林科技集团有限公司 Oilfield associated gas comprehensive utilization system and process

Also Published As

Publication number Publication date
CN103351896B (en) 2015-05-06

Similar Documents

Publication Publication Date Title
CN103351896A (en) Method and device for removing water and heavy hydrocarbons from shale gas
CN203319964U (en) Device for removing water and heavy hydrocarbon out of shale gas
CN102643694B (en) Technique and device for drying and liquefaction of natural gas
CN103031169B (en) Method and device for carrying out liquefaction and heavy hydrocarbon treatment on natural gas
CN105716371B (en) A kind of method and device of azeotrope refrigeration natural gas lighter hydrocarbons recovery
USRE39826E1 (en) Comprehensive natural gas processing
US9255731B2 (en) Sour NGL stream recovery
US20080016909A1 (en) Flexible hydrocarbon gas separation process and apparatus
CN103031168A (en) Dehydration and de-heavy hydrocarbon technology for production of liquefied natural gas from methane-rich mixed gas
CN104557387A (en) Refinery mixed dry gas recovery system and recovery method
CN110538476A (en) Low-temperature flash light hydrocarbon recovery system and method for oilfield associated gas
CN103453730A (en) Natural gas liquefying method and device with light hydrocarbon recovery function
CN101633595B (en) Method for reclaiming ethylene in catalytic dry gas
CN204981793U (en) Processing apparatus of associated gas is applied to to LNG cold energy
CN105276924B (en) A kind of lighter hydrocarbons cryogenic separation retracting device and method
CN106085528A (en) High-adaptability heavy hydrocarbon removal process
CN104419466B (en) A kind of oil refinery dry gas recovery system and dry-gas recovery method
CN202626134U (en) Process device for preparing liquefied natural gas (LNG) and hydrogen simultaneously through coke oven gas
CN202595073U (en) Natural gas drying and liquefying device
US9200833B2 (en) Heavy hydrocarbon processing in NGL recovery system
CN103626619A (en) Light hydrocarbon separation method used in methanol to olefin device
CN202924980U (en) Natural gas liquefaction and heavy hydrocarbon treatment device
CN211946916U (en) Oil field associated gas light hydrocarbon recovery system
CN203454604U (en) Natural gas liquefaction device with light hydrocarbon recovery function
CN208356427U (en) Fischer-Tropsch process exhaust purification device

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