CN104792116B - A kind of natural gas reclaims the system and technique of ethane and ethane above lighter hydrocarbons - Google Patents

A kind of natural gas reclaims the system and technique of ethane and ethane above lighter hydrocarbons Download PDF

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Publication number
CN104792116B
CN104792116B CN201410690194.2A CN201410690194A CN104792116B CN 104792116 B CN104792116 B CN 104792116B CN 201410690194 A CN201410690194 A CN 201410690194A CN 104792116 B CN104792116 B CN 104792116B
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Prior art keywords
ice chest
feeding mouth
discharging opening
column
domethanizing column
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CN104792116A (en
Inventor
裴红
赵文学
闫日雄
陈令海
刘焕焕
黄建钦
陈以文
张帆
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China National Petroleum Corp
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China Huanqiu Engineering 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
    • F25J3/0238—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of CnHm with 2 carbon atoms or more
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • 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
    • F25J2200/76—Refluxing the column with condensed overhead gas being cycled in a quasi-closed loop refrigeration cycle
    • 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
    • F25J2240/00—Processes or apparatus involving steps for expanding of process streams
    • F25J2240/02—Expansion of a process fluid in a work-extracting turbine (i.e. isentropic expansion), e.g. of the feed stream
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/12—External refrigeration with liquid vaporising loop
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/60—Closed external refrigeration cycle with single component refrigerant [SCR], e.g. C1-, C2- or C3-hydrocarbons

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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)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Separation By Low-Temperature Treatments (AREA)

Abstract

The present invention relates to the system and technique that a kind of natural gas reclaims ethane and ethane above lighter hydrocarbons, unstripped gas, which is passed through after the first ice chest after a gaseous stream part for cold catch pot separation expands through coaxial expansion compressor group, enters the feeding mouth of domethanizing column first, and another part is passed through the feeding mouth of domethanizing column second after the second ice chest and the 3rd J T valves；Liquid phase discharging opening of the liquid phase stream through cold catch pot leads to the feeding mouth of domethanizing column the 3rd through the first J T valves, the second ice chest, demethanizer overhead gaseous stream goes outer defeated compress cell, another part to lead to the feeding mouth of domethanizing column the 4th after returning hydraulic compression machine, air cooler, water recirculator, the first ice chest, the second ice chest and the 2nd J T valves through methane after being compressed through the second ice chest, the first ice chest rear portion material through coaxial expansion compressor group；Middle part first discharging opening of the middle part low temperature logisticses of domethanizing column through domethanizing column simultaneously returns to domethanizing column again after the first ice chest；Demethanizer bottom reclaims ethane and ethane above lighter hydrocarbons.

Description

A kind of natural gas reclaims the system and technique of ethane and ethane above lighter hydrocarbons
Technical field
The present invention relates to gas field ground surface works field, more particularly to a kind of natural gas reclaims ethane and ethane above lighter hydrocarbons System and technique.
Background technology
To isolate the high added value component such as ethane, LPG and stable light hydrocarbon from natural gas, existing process uses physics side Method, separation cutting is carried out according to dew point of the unstripped gas under certain temperature and pressure.Generally outside gas field it is defeated under the conditions of unstripped gas In gaseous state, it is therefore desirable to which unstripped gas is freezed.The overall economy quality major embodiment of C2+ retracting devices is in investment, energy consumption With product income, this depends greatly on refrigeration process scheme and heat-exchange network, therefore solutions for refrigeration and heat-exchange network The good and bad economy to process program play vital effect, existing process is all to be researched and developed accordingly.
New through looking into, being currently primarily present three kinds of technologies has similitude, and these three techniques are all to continue to use to carry out natural gas The thinking of cryogenic separation, to reclaim light hydrocarbon component therein, exchange ther mal network has all carried out certain optimization and formd respective Some features, three kinds of technique difference are as follows：
A)：Patent No. US4687499A, process chart are as shown in Fig. 2 the patent is set based on traditional natural gas separation It is standby to have carried out process modification, on the premise of existing process equipment is not changed, complete rectifying column flow is gone into, and realize Ethane almost 100% separation, but the bottoms 50 of technique cold catch pot 46 through J-T valves 56 throttle after be directly entered it is de- Methane tower, this strand of logistics cold fails to make full use of and is provided with two sets of coaxial compressing expansion machines 52 and 64.
B)：Patent No. US2013074542A1, as shown in figure 3, the patent is directed to the natural gas ethane recovery rich in heavy hydrocarbon Process optimization is carried out, the technique has more preferable adaptability to the change of component of unstripped gas, but the technique cold catch pot D-1 bottoms are divided into two strand 3 and 4, and wherein logistics 3 enters throttling cooling after ice chest MSHX-2 heat exchange and entered on domethanizing column Portion, logistics 4 is directly entered after being throttled through J-T valves in the middle part of domethanizing column, and the cold of logistics 4 fails to make full use of；The technique demethanation Tower is provided with 4 sections of circulating refluxs (at first：Logistics 14 goes out, logistics 15 times；At second：Logistics 16 goes out, logistics 17 times；At 3rd： Logistics 18 goes out, logistics 19 times；Everywhere：Logistics 20 goes out, logistics 37 times), technological process is complicated, is the operation increase of domethanizing column Great difficulty；The energy consumption of the PROCESS FOR TREATMENT natural gas is 0.036KW/m3, and ethane recovery is 94%.
C) Recycle Split Vapor (RSV) techniques of U.S. ortloffs companies are as shown in figure 4, the technology key Point is that with the addition of one improves the second of the technique by the demethanizer top material inlet that outer defeated dry gas is constituted, this improvement is subcooled The alkane rate of recovery, but C1 contents 92.5% in unstripped gas handled by technique, belong to lighter natural gas；The technique goes out cryogenic separation Device D-101 bottoms are divided into two strands, and one enters at the top of domethanizing column T-101 after entering ice chest E-102 heat exchange, another stock-traders' know-how It is directly entered after crossing the throttling of J-T valves in the middle part of domethanizing column；Technological process is：The gaseous stream of domethanizing column ejection sequentially enters cold Case E-102 and ice chest E-101 heat exchange, into the supercharging of coaxial expansion compressor C-101 compression ends, further increases through outer defeated compressor It is outer defeated after pressure.One logistics is extracted out from outer defeated dry gas into throttling cooling re-injection demethanizer overhead after ice chest E-102 heat exchange, Ice chest E-101 heat exchange is not entered..
Three of the above patent the characteristics of all possessing respective in terms of ethane in realizing natural gas and ethane above lighter hydrocarbons recovery, The advanced level that current natural gas reclaims ethane and ethane above lighter hydrocarbons technique is represented, but these techniques lack there is also some Fall into, such as the adaptability to unstripped gas is still not enough, and the scope of application is smaller, fail to make full use of system cold, complex process equipment, Operability is poor etc. in production process.
The content of the invention
System cold can be recycled to greatest extent the technical problem to be solved in the present invention is to provide one kind to be used, Process energy consumption is reduced, while ensure that the natural gas of ethane and ethane above lighter hydrocarbons in high yield reclaims ethane and ethane above lighter hydrocarbons System and technique.
For up to above-mentioned purpose, the system that a kind of natural gas of the invention reclaims ethane and ethane above lighter hydrocarbons, the system bag The first ice chest, propane refrigeration unit, cold catch pot, the second ice chest, domethanizing column, methane is included to return hydraulic compression machine, air cooler, follow Ring water cooler and coaxial expansion compressor group；
The unstripped gas discharging opening of first ice chest is communicated with the feeding mouth of the cold catch pot；
First feeding mouth of the gas phase discharging opening of the cold catch pot through the coaxial expansion compressor group and described same Communicated and through described second with the feeding mouth of column plate first of the domethanizing column after first discharging opening of axle expansion compressor group With the column plate of the domethanizing column after first feeding mouth of ice chest, the first discharging opening of second ice chest and the 3rd J-T valves Two feeding mouths are communicated；
The liquid phase discharging opening of the cold catch pot is through the first J-T valves, the second feeding mouth of second ice chest and described Second discharging opening of the second ice chest is communicated with the feeding mouth of column plate the 3rd of the domethanizing column；
The of threeth feeding mouth of the demethanizer overhead gas phase discharging opening through second ice chest, second ice chest After first discharging opening of three discharging openings, the first charging aperture of first ice chest and first ice chest and respectively through described coaxial Second feeding mouth of expansion compressor group, the second discharging opening of the coaxial expansion compressor group are communicated and returned through the methane Feeding mouth, the methane of hydraulic compression machine return the discharging opening, the feeding mouth of the air cooler, the discharging of the air cooler of hydraulic compression machine Mouth, the feeding mouth of the water recirculator, the discharging opening of the water recirculator, the second pan feeding of first ice chest Mouth, the second discharging opening of first ice chest, the 4th feeding mouth of second ice chest, the 4th discharging opening of second ice chest Communicated with the feeding mouth of column plate the 4th after the 2nd J-T valves with the domethanizing column；
Threeth feeding mouth of the discharging opening of middle part first of the domethanizing column through first ice chest, first ice chest Communicated after 3rd discharging opening with the feeding mouth of middle part first of the domethanizing column；
The demethanizer bottom is provided with discharging opening；
The propane refrigeration unit is used for replenishment system cold through first ice chest.
Wherein also include the discharging opening of middle part second of the domethanizing column, the discharging opening warp of middle part second of the domethanizing column Middle part second after 4th feeding mouth of first ice chest, the 4th discharging opening of first ice chest with the domethanizing column enters Material mouth is communicated.
Wherein described domethanizing column is included by the 35-42 block column plates that set gradually up and down, the column plate of the domethanizing column the One feeding mouth is located at 21-24 block column plates, and the feeding mouth of column plate second of the domethanizing column is located at 3-5 block column plates, institute The feeding mouth of column plate the 3rd for stating domethanizing column is located at 4-6 block column plates, and the feeding mouth of column plate the 4th of the domethanizing column is located at At tower top, the discharging opening of middle part first of the domethanizing column is located at 25-27 block column plates, the middle part first of the domethanizing column Feeding mouth is located at 27-29 block column plates.
Wherein described domethanizing column is included by the 35-42 block column plates that set gradually up and down, the middle part of the domethanizing column the Two discharging openings are located at 31-33 block column plates, and the feeding mouth of middle part second of the domethanizing column is located at 33-35 block column plates.
Wherein described domethanizing column bottom is connected with demethanizer bottoms reboiler, and the demethanizer bottoms carry out bottom product Extract out, portioned product enters tower bottom reboiler, reboiler upper part discharge port leads to the demethanation tower side wall feeding mouth, returns to material Continue the gas-liquid mass transfer in tower.
One kind reclaims ethane using the natural gas and ethane above lighter hydrocarbons system reclaim more than ethane and ethane light The technique of hydrocarbon, comprises the following steps：
Unstripped gas is passed through in the cold catch pot after first ice chest, the gas gas-phase objects of the cold catch pot separation The gas phase discharging opening part for flowing through the cold catch pot enters described after the coaxial expansion compressor group swell refrigeration The feeding mouth of domethanizing column first, first feeding mouth of the another part through the ice chest of the second ice chest second, second ice chest The feeding mouth of column plate second of the domethanizing column is passed through after first discharging opening and the 3rd J-T valves；
Liquid phase discharging opening of the liquid phase stream through the cold catch pot of cold catch pot separation through the first J-T valves, Second discharging opening of the second feeding mouth of second ice chest and second ice chest leads to the column plate the 3rd of the domethanizing column Feeding mouth；
The demethanizer overhead gaseous stream through state the gas phase discharging opening of domethanizing column and through second ice chest Three feeding mouths, the 3rd discharging opening of second ice chest, the of the first charging aperture of first ice chest and first ice chest After one discharging opening and second feeding mouth of a part of material through the coaxial expansion compressor group, the coaxial expansion compressor group The compression of the second discharging opening after remove outer defeated compress cell, a part returns the feeding mouth of hydraulic compression machine, methane through the methane and returns liquid The discharging opening of compressor, the feeding mouth of the air cooler, the discharging opening of the air cooler, the pan feeding of the water recirculator Mouth, the discharging opening of the water recirculator, the second feeding mouth of first ice chest, the second discharging of first ice chest Lead to the piptonychia after mouth, the 4th feeding mouth of second ice chest, the 4th discharging opening of second ice chest and the 2nd J-T valves The feeding mouth of column plate the 4th of alkane tower；
Middle part first discharging opening of the middle part low temperature logisticses of the domethanizing column through the domethanizing column and through described first The domethanizing column is returned to after 3rd feeding mouth of ice chest, the 3rd discharging opening of first ice chest again；
The demethanizer bottom reclaims ethane and ethane above lighter hydrocarbons；
Wherein described propane refrigeration unit is used for replenishment system cold through first ice chest.
One kind reclaims ethane using the natural gas and ethane above lighter hydrocarbons system reclaim more than ethane and ethane light The technique of hydrocarbon, it is characterised in that comprise the following steps：
Unstripped gas is passed through in the cold catch pot after first ice chest, the gas gas-phase objects of the cold catch pot separation The gas phase discharging opening part for flowing through the cold catch pot enters described after the coaxial expansion compressor group swell refrigeration The feeding mouth of domethanizing column first, first feeding mouth of the another part through the ice chest of the second ice chest second, second ice chest The feeding mouth of column plate second of the domethanizing column is passed through after first discharging opening and the 3rd J-T valves；
Liquid phase discharging opening of the liquid phase stream through the cold catch pot of cold catch pot separation through the first J-T valves, Second discharging opening of the second feeding mouth of second ice chest and second ice chest leads to the column plate the 3rd of the domethanizing column Feeding mouth；
The demethanizer overhead gaseous stream through state the gas phase discharging opening of domethanizing column and through second ice chest Three feeding mouths, the 3rd discharging opening of second ice chest, the of the first charging aperture of first ice chest and first ice chest After one discharging opening and second feeding mouth of a part of material through the coaxial expansion compressor group, the coaxial expansion compressor group The compression of the second discharging opening after remove outer defeated compress cell, a part returns the feeding mouth of hydraulic compression machine, methane through the methane and returns liquid The discharging opening of compressor, the feeding mouth of the air cooler, the discharging opening of the air cooler, the pan feeding of the water recirculator Mouth, the discharging opening of the water recirculator, the second feeding mouth of first ice chest, the second discharging of first ice chest Lead to the piptonychia after mouth, the 4th feeding mouth of second ice chest, the 4th discharging opening of second ice chest and the 2nd J-T valves The feeding mouth of column plate the 4th of alkane tower；
Middle part first discharging opening of the middle part low temperature logisticses of the domethanizing column through the domethanizing column and through described first The domethanizing column is returned to after 3rd feeding mouth of ice chest, the 3rd discharging opening of first ice chest again；
Middle part second discharging opening of the middle part another part low temperature logisticses through the domethanizing column of the domethanizing column is simultaneously passed through The domethanizing column is returned to after 4th feeding mouth of first ice chest, the 4th discharging opening of first ice chest again；
The demethanizer bottom reclaims ethane and ethane above lighter hydrocarbons；
Wherein described propane refrigeration unit is used for replenishment system cold through first ice chest.
Wherein described demethanizer bottom gas-liquid component enters the demethanizer bottoms reboiler, from the demethanizer bottoms Reclaim heavy constituent, reboiler use hydrocone type reboiler, into the gas-liquid heat phase of reboiler after all return to the demethanation Tower carries out gas-liquid mass transfer.
The invention difference from existing technology is that the present invention achieves following technique effect：
1st, present invention process exchange ther mal network is improved, and cold has been carried out to the liquid phase stream for going out cold catch pot bottom Reclaim, greatly reduce the thermic load of propane refrigeration system so that propane refrigeration system energy consumption reduces 35%；
2nd, present invention process goes out after the recovered cold heating of cold catch pot bottom liquid phases, forms rate of gasification as high as possible Gas-liquid two-phase logistics enters correspondence column plate in the middle part of domethanizing column, while overhead stream is formd less than -100 DEG C after heat exchange throttling Low temperature logisticses enter tower top, the setting of this temperature at two improves the separative efficiency of whole domethanizing column, and ethane recovery surpasses Cross 98%；
3rd, improve potential temperature after the recovered cold of present invention process cold catch pot bottom liquid phases and enter domethanizing column, save The thermic load of demethanizer reboiler；
4th, one logistics has been separated before present invention process demethanation overhead stream is defeated outside supercharging to return into single methane Compressor is flowed, through the re-injection demethanation tower top that exchanges heat after supercharging, design of flow coordinates the optimization of whole heat-exchange network to realize at this From reclaiming C2+To recovery C3+Seamless transitions, and C3+Yield is more than 95%, in actual mechanical process, and domethanizing column is reserved Interface, according to the requirement in the different production periods of production unit to product, it is possible to achieve the transformation of not getting angry of different kinds of process flow.
Brief description of the drawings
Fig. 1 is present invention process schematic flow sheet；
Fig. 2 is a kind of process chart of improved natural gas separation equipment；
Fig. 3 is the process optimization flow chart of the natural gas ethane recovery rich in heavy hydrocarbon；
Fig. 4 is Recycle Split Vapor (RSV) process chart of ortloffs companies of the U.S..
Description of reference numerals：A- domethanizing columns；The ice chests of B-1- first；The ice chests of B-2- second；C- air coolers；D- recirculated water coolings But device；E- demethanizer bottoms reboilers；F- cold catch pots；The coaxial expansion compressor groups of G-；H- methane reflux compressors；I-1- First J-T valves；The J-T valves of I-2- the 2nd；The J-T valves of I-3- the 3rd.
Embodiment
With reference to embodiments, the forgoing and additional technical features and advantages are described in more detail.
As shown in figure 1, the system that a kind of natural gas of the invention reclaims ethane and ethane above lighter hydrocarbons, the system includes the One ice chest B-1, propane refrigeration unit, cold catch pot F, the second ice chest B-2, domethanizing column A, methane return hydraulic compression machine H, air cooling Device C, water recirculator D, coaxial expansion compressor group G and demethanizer bottoms reboiler；
First ice chest B-1 unstripped gas discharging opening is communicated with cold catch pot F feeding mouth；Cold catch pot F gas phase With piptonychia after first discharging opening of the first feeding mouth and coaxial expansion compressor group G of the discharging opening through coaxial expansion compressor group G The alkane tower A feeding mouth of column plate first is communicated and the first feeding mouth through the second ice chest B-2, the second ice chest B-2 the first discharging Communicated after mouth and the 3rd J-T valves I-3 with the domethanizing column A feeding mouth of column plate second；Cold catch pot F liquid phase discharging opening is through One J-T valves I-1, the second ice chest B-2 the second feeding mouth and the second ice chest B-2 the second discharging opening and domethanizing column A column plate 3rd feeding mouth is communicated；Threeth feeding mouth of the domethanizing column A top gas phases discharging opening through the second ice chest B-2, the second ice chest B-2 After first discharging opening of the 3rd discharging opening, the first ice chest B-1 first charging aperture and the first ice chest B-1 and respectively through coaxial expansion Compressor set G the second feeding mouth, coaxial expansion compressor group G the second discharging opening communicate and return hydraulic compression machine H through methane Feeding mouth, methane return hydraulic compression machine H discharging opening, air cooler C feeding mouth, air cooler C discharging opening, water recirculator D feeding mouth, water recirculator D discharging opening, the first ice chest B-1 the second feeding mouth, the first ice chest B-1 the second discharging With domethanizing column A after mouth, the second ice chest B-2 the 4th feeding mouth, the second ice chest B-2 the 4th discharging opening and the 2nd J-T valves I-2 The feeding mouth of column plate the 4th communicate；Threeth feeding mouth of the domethanizing column A discharging opening of middle part first through the first ice chest B-1, first Communicated after ice chest B-1 the 3rd discharging opening with the domethanizing column A feeding mouth of middle part first；Domethanizing column A bottoms are provided with discharging opening； Propane refrigeration unit is used for replenishment system cold through the first ice chest B-1.
Fourth feeding mouth of the domethanizing column A discharging opening of middle part second through the first ice chest B-1, the 4th of the first ice chest B-1 the Communicated after discharging opening with the domethanizing column A feeding mouth of middle part second.
Wherein domethanizing column A includes the 35-42 block column plates by setting gradually up and down, the domethanizing column A pan feeding of column plate first Mouth is located at 21-24 block column plates, and the domethanizing column A feeding mouth of column plate second is located at 3-5 block column plates, domethanizing column A's The feeding mouth of column plate the 3rd is located at 4-6 block column plates, and the domethanizing column A feeding mouth of column plate the 4th is located at tower top, domethanizing column A The discharging opening of middle part first be located at 25-27 block column plates, the domethanizing column A feeding mouth of middle part first is located at 27-29 block towers At plate；The domethanizing column A discharging opening of middle part second is located at 31-33 block column plates, the domethanizing column A feeding mouth position of middle part second At 33-35 block column plates.
Domethanizing column A is carried out bottom product extraction, portioned product by the demethanizer bottoms reboiler E of domethanizing column A bottoms Into tower bottom reboiler E, reboiler E upper part discharge ports lead to domethanizing column A sides wall feeding mouth, return to material and continue the gas-liquid in tower Mass transfer.
1) example 1
A) unstripped gas composition and flow
Unstripped gas constitutes (mol%, i and n are the symbol logos of isomer) such as following table：
CO2 N2 C1 C2 C3 iC4 nC4 iC5 nC5 C6 +
0.0077 0.0304 0.8676 0.0658 0.0169 0.0036 0.0048 0.0013 0.001 0.0008
Unstripped gas treating capacity：126×108m3/a(annum)
B) stream components and property
Unstripped gas (1,30 DEG C of logistics, 6.10MPa) enters the first ice chest B-1 heat exchange, cooling drop after being dehydrated demercuration processing Temperature to -42 DEG C, 6.04MPa logistics 2 enters cold catch pot F.Go out cold catch pot F gas phases (C1Content 88.18%) it is divided into two Stock logistics 3 (20%-30%) and material 5 (70%-80%), logistics 3 enter coaxial expansion compressor G expanding end swell refrigerations Enter the 23rd block of column plate of domethanizing column A after to -79.4 DEG C, 2.40MPa logistics 4, logistics 5 enters the second ice chest B-2 heat exchange drops Enter demethanation by the 3rd J-T valve I-3 throttling expansions to the logistics 6 of -97.9 DEG C, 2.40MPa after extremely -70 DEG C of temperature, 6.03MPa Tower A the 4th block of column plate；Cold catch pot F exports liquid phase stream 7, (C1Content 52.63%) it is swollen into the first J-T valves I-1 throttlings Swollen to -63.7 DEG C, 2.40MPa logistics 8, gas-liquid two-phase logistics 8 exchanges heat to -40 DEG C into the second ice chest B-2,2.39MPa's Logistics 9, rate of gasification 50%, the gaseous stream 10 that logistics 9 is ejected into domethanizing column the 5th block of column plate of A, domethanizing column A, (- 102.6 DEG C, 2.35MPa, C1Content 95.92%) exchanged heat into the second ice chest B-2 to -47.8 DEG C, 2.34MPa logistics 11 Continue to exchange heat to 27 DEG C, 2.33MPa into the first ice chest B-1, be divided into (the 70%- of logistics 12 by certain distribution ratio after cooling box 80%) with two strands of logistics 13 (20%-30%), logistics 13 is pressurized to 91.6 DEG C, 4.5MPa thing into methane reflux compressor H Device D temperature is dropped to 35 DEG C through air cooler C and recirculated water cooling after stream 14, is exchanged heat into the first ice chest B-1 to the thing of -20 DEG C, 4.49MPa Stream 15, logistics 15 exchanges heat to -91.5 DEG C, 4.48MPa through the 2nd J-T valve I-2 throttling expansions to -104.3 into the second ice chest B-2 DEG C, 2.45MPa be back to domethanizing column A top；Logistics 12 into coaxial expanding machine compressor G compression ends be compressed to 45.8 DEG C, Outer defeated compress cell is removed in 2.84MPa logistics 25.
Extract two streams in the middle part of domethanizing column A out and carry out cold recovery：The circulation of first stage casing extracted out from the 26th layer of column plate- 77.4 DEG C, 2.38MPa logistics 17, exchanging heat to reclaim into the first ice chest B-1 is warming up to -45 DEG C, 2.37MPa logistics after cold 18, it is injected back into from the 28th layer of column plate；Second stage casing circulation is entered from the 32nd layer of -55.9 DEG C of column plate extraction, 2.39MPa logistics 19 Enter after cold is reclaimed in the first ice chest B-1 heat exchange and be warming up to -40.0 DEG C, 2.38MPa logistics 20, be injected back into from the 34th layer of column plate.
Domethanizing column A bottoms go out C2 +Product, wherein C1Content 1%, C2Content 66.59%.
C in this example2Yield 97.75%, C2 +Yield 98.42%, C3 +Yield 100%.
Stream components refer to following table.
2) example 2
A) unstripped gas is constituted
Unstripped gas composition such as following table：
CO2 N2 C1 C2 C3 iC4 nC4 iC5 nC5 C6 +
0.0081 0.0320 0.8491 0.0808 0.0178 0.0038 0.0050 0.0014 0.0011 0.0008
Unstripped gas treating capacity：126×108m3/a
B) technique content
Unstripped gas (5 DEG C of logistics Isosorbide-5-Nitrae, 7.0MPa) through be dehydrated demercuration processing after enter ice chest B-1 heat exchange, cool to- 42 DEG C, 6.94MPa (logistics 2) entrance cold catch pots F.Go out cold catch pot gas phase (C1Content 86.45%) it is divided into two strands of things Flow (3 and 5), logistics 3 enters extremely -84.1 DEG C of coaxial expansion compressor G expanding ends swell refrigeration, 2.40MPa (logistics 4) and enters de- The 23rd block of column plate of methane tower A, logistics 5 is cooled to after -70 DEG C, 6.93MPa swollen by J-T valves I-3 throttlings into ice chest B-2 heat exchange Swollen to -98.4 DEG C, 2.40MPa (logistics 6) the 4th block of column plate of entrance, cold catch pot outlet liquid phase (logistics 7, C1Content 60.49%) J-T valve I-1 throttling expansions are entered to -68.9 DEG C, 2.40MPa (logistics 8, gas-liquid two-phase) enters ice chest B-2 heat exchange To -40 DEG C, 2.39MPa (logistics 9, rate of gasification 64.41%) enters the 5th block of column plate of domethanizing column.The gas phase of domethanizing column ejection (logistics 10, -103.9 DEG C, 2.35MPa, C1Content 95.73%) exchanged heat into ice chest B-2 to -50.8 DEG C, 2.34MPa (logistics 11) enter ice chest B-1 afterwards to continue to exchange heat to 27 DEG C, 2.33MPa, be divided into logistics 12 and 13 liang by certain distribution ratio after cooling box Stock, logistics 13 is into methane reflux compressor is pressurized to 91.6 DEG C, 4.5MPa (logistics 14) drops by air cooler and recirculated water cooling Temperature exchanges heat to -20 DEG C, 4.49MPa (logistics 15), logistics 15 exchanges heat to -91.5 into ice chest B-2 to 35 DEG C into ice chest B-1 DEG C, 4.48MPa through J-T valve I-2 throttling expansions to -104.4 DEG C, 2.45MPa be back to demethanation tower top.Logistics 12 enters coaxial Expanding machine compressor G compression ends be compressed to 45.9 DEG C, 2.84MPa (logistics 25) remove outer defeated compress cell.Taken out in the middle part of domethanizing column Go out two streams and carry out cold recovery：Circulate from the 26th layer of -83.81 DEG C of column plate extraction, 2.38MPa logistics in first stage casing 17, -45 DEG C, 2.37MPa (logistics 18) are warming up to after reclaiming cold into ice chest B-1 heat exchange, is injected back into from the 28th layer of column plate；Second Individual stage casing circulation is reclaimed into ice chest B-1 heat exchange and risen after cold from the 32nd layer of -64.2 DEG C of column plate extraction, 2.39MPa logistics 19 Temperature is injected back into -40.0 DEG C, 2.38MPa (logistics 20) from the 34th layer of column plate.Demethanizer bottoms go out C2 +Product, wherein C1Content 1%, C2Content 69.39%.
C in this example2Yield 98.01%, C2 +Yield 98.54%, C3 +Yield 100%.
Stream components refer to following table.
Embodiment described above is only that the preferred embodiment of the present invention is described, not to the model of the present invention Enclose and be defined, on the premise of design spirit of the present invention is not departed from, technical side of the those of ordinary skill in the art to the present invention In various modifications and improvement that case is made, the protection domain that claims of the present invention determination all should be fallen into.

Claims (8)

1. the system that a kind of natural gas reclaims ethane above lighter hydrocarbons, it is characterised in that：The system includes the first ice chest, propane system Cold unit, cold catch pot, the second ice chest, domethanizing column, methane return hydraulic compression machine, air cooler, water recirculator and coaxial Expansion compressor group；
The unstripped gas discharging opening of first ice chest is communicated with the feeding mouth of the cold catch pot；
First feeding mouth of expanding end of the gas phase discharging opening of the cold catch pot through the coaxial expansion compressor group and institute The feeding mouth of column plate first after first discharging opening of the expanding end for stating coaxial expansion compressor group with the domethanizing column is mutually passed to And after the first feeding mouth, the first discharging opening of second ice chest and the 3rd J-T valves through second ice chest with the piptonychia The feeding mouth of column plate second of alkane tower is communicated；
The liquid phase discharging opening of the cold catch pot is through the first J-T valves, the second feeding mouth of second ice chest and described second Second discharging opening of ice chest is communicated with the feeding mouth of column plate the 3rd of the domethanizing column；
Threeth feeding mouth of the demethanizer overhead gas phase discharging opening through second ice chest, the 3rd of second ice chest the go out After first discharging opening of material mouth, the first feeding mouth of first ice chest and first ice chest and respectively through the coaxial expansion Second feeding mouth of the compression end of compressor set, the second discharging opening of the compression end of the coaxial expansion compressor group communicate and Discharging opening, the feeding mouth of the air cooler, the sky that the feeding mouth of hydraulic compression machine, methane return hydraulic compression machine are returned through the methane The discharging opening of cooler, the feeding mouth of the water recirculator, the discharging opening of the water recirculator, first ice chest Second feeding mouth, the second discharging opening of first ice chest, the 4th feeding mouth of second ice chest, the of second ice chest Communicated after four discharging openings and the 2nd J-T valves with the feeding mouth of column plate the 4th of the domethanizing column；
Threeth feeding mouth of the discharging opening of middle part first of the domethanizing column through first ice chest, the 3rd of first ice chest the Communicated after discharging opening with the feeding mouth of middle part first of the domethanizing column；
The demethanizer bottom is provided with discharging opening；
The propane refrigeration unit is used for replenishment system cold through first ice chest.
2. the system that natural gas according to claim 1 reclaims ethane above lighter hydrocarbons, it is characterised in that：Also include described de- The discharging opening of middle part second of methane tower, fourth pan feeding of the discharging opening of middle part second through first ice chest of the domethanizing column Communicated after mouth, the 4th discharging opening of first ice chest with the feeding mouth of middle part second of the domethanizing column.
3. the system that natural gas according to claim 1 reclaims ethane above lighter hydrocarbons, it is characterised in that：The domethanizing column Including the 35-42 block column plates by setting gradually up and down, the feeding mouth of column plate first of the domethanizing column is located at 21-24 block column plates Place, the feeding mouth of column plate second of the domethanizing column is located at 3-5 block column plates, the feeding mouth of column plate the 3rd of the domethanizing column At 4-6 block column plates, the feeding mouth of column plate the 4th of the domethanizing column is located at tower top, the middle part of the domethanizing column the One discharging opening is located at 25-27 block column plates, and the feeding mouth of middle part first of the domethanizing column is located at 27-29 block column plates.
4. the system that natural gas according to claim 2 reclaims ethane above lighter hydrocarbons, it is characterised in that：The domethanizing column Including the 35-42 block column plates by setting gradually up and down, the discharging opening of middle part second of the domethanizing column is located at 31-33 block column plates Place, the feeding mouth of middle part second of the domethanizing column is located at 33-35 block column plates.
5. the system that the natural gas according to any one of claim 1-4 reclaims ethane above lighter hydrocarbons, it is characterised in that：Institute State domethanizing column bottom and be connected with demethanizer bottoms reboiler, the demethanizer bottoms carry out bottom product extraction, portioned product Into tower bottom reboiler, reboiler upper part discharge port leads to the demethanation tower side wall feeding mouth, returns to material and continues the gas in tower Liquid mass transfer.
6. one kind reclaims ethane above lighter hydrocarbons system using the natural gas as described in claim 1 or 3 and carried out more than recovery ethane The technique of lighter hydrocarbons, it is characterised in that comprise the following steps：
Unstripped gas is passed through in the cold catch pot after first ice chest, the gaseous stream warp of the cold catch pot separation A gas phase discharging opening part for the cold catch pot enters the piptonychia after the coaxial expansion compressor group swell refrigeration The feeding mouth of alkane tower first, first feeding mouth of the another part through the ice chest of the second ice chest second, the first of second ice chest The feeding mouth of column plate second of the domethanizing column is passed through after discharging opening and the 3rd J-T valves；
Liquid phase discharging opening of the liquid phase stream through the cold catch pot of cold catch pot separation is through the first J-T valves, described Second discharging opening of the second feeding mouth of the second ice chest and second ice chest leads to the pan feeding of column plate the 3rd of the domethanizing column Mouthful；
The demethanizer overhead gaseous stream is through stating the gas phase discharging opening of domethanizing column and the 3rd through second ice chest enters Material mouth, the 3rd discharging opening of second ice chest, the first of the first feeding mouth of first ice chest and first ice chest go out After material mouth and second feeding mouth of a part of material through the coaxial expansion compressor group, the of the coaxial expansion compressor group Outer defeated compress cell is removed after the compression of two discharging openings, a part returns the feeding mouth of hydraulic compression machine, methane through the methane and returns hydraulic compression The discharging opening of machine, the feeding mouth of the air cooler, the discharging opening of the air cooler, the feeding mouth of the water recirculator, institute State the discharging opening of water recirculator, it is the second feeding mouth of first ice chest, the second discharging opening of first ice chest, described Lead to the domethanizing column after the 4th feeding mouth, the 4th discharging opening of second ice chest and the 2nd J-T valves of second ice chest The feeding mouth of column plate the 4th；
Middle part first discharging opening of the middle part low temperature logisticses of the domethanizing column through the domethanizing column and through first ice chest The 3rd feeding mouth, return to the domethanizing column again after the 3rd discharging opening of first ice chest；
The demethanizer bottom reclaims ethane above lighter hydrocarbons；
Wherein described propane refrigeration unit is used for replenishment system cold through first ice chest.
7. one kind reclaims ethane above lighter hydrocarbons system using the natural gas as described in claim 2 or 4 and carried out more than recovery ethane The technique of lighter hydrocarbons, it is characterised in that comprise the following steps：
Unstripped gas is passed through in the cold catch pot after first ice chest, the gaseous stream warp of the cold catch pot separation A gas phase discharging opening part for the cold catch pot enters the piptonychia after the coaxial expansion compressor group swell refrigeration The feeding mouth of alkane tower first, first feeding mouth of the another part through the ice chest of the second ice chest second, the first of second ice chest The feeding mouth of column plate second of the domethanizing column is passed through after discharging opening and the 3rd J-T valves；
Liquid phase discharging opening of the liquid phase stream through the cold catch pot of cold catch pot separation is through the first J-T valves, described Second discharging opening of the second feeding mouth of the second ice chest and second ice chest leads to the pan feeding of column plate the 3rd of the domethanizing column Mouthful；
The demethanizer overhead gaseous stream is through stating the gas phase discharging opening of domethanizing column and the 3rd through second ice chest enters Material mouth, the 3rd discharging opening of second ice chest, the first of the first feeding mouth of first ice chest and first ice chest go out After material mouth and second feeding mouth of a part of material through the coaxial expansion compressor group, the of the coaxial expansion compressor group Outer defeated compress cell is removed after the compression of two discharging openings, a part returns the feeding mouth of hydraulic compression machine, methane through the methane and returns hydraulic compression The discharging opening of machine, the feeding mouth of the air cooler, the discharging opening of the air cooler, the feeding mouth of the water recirculator, institute State the discharging opening of water recirculator, it is the second feeding mouth of first ice chest, the second discharging opening of first ice chest, described Lead to the domethanizing column after the 4th feeding mouth, the 4th discharging opening of second ice chest and the 2nd J-T valves of second ice chest The feeding mouth of column plate the 4th；
Middle part first discharging opening of the middle part low temperature logisticses of the domethanizing column through the domethanizing column and through first ice chest The 3rd feeding mouth, return to the domethanizing column again after the 3rd discharging opening of first ice chest；
Described in the discharging opening of middle part second of the middle part another part low temperature logisticses through the domethanizing column and warp of the domethanizing column The domethanizing column is returned to after 4th feeding mouth of the first ice chest, the 4th discharging opening of first ice chest again；
The demethanizer bottom reclaims ethane above lighter hydrocarbons；
Wherein described propane refrigeration unit is used for replenishment system cold through first ice chest.
8. the technique that natural gas according to claim 6 or 7 reclaims ethane above lighter hydrocarbons, it is characterised in that also including with Lower step：The demethanizer bottom gas-liquid component enters demethanizer bottoms reboiler, reclaims and recombinates from the demethanizer bottoms Point, reboiler uses hydrocone type reboiler, into the gas-liquid heat phase of reboiler after all return to the domethanizing column and enter promoting the circulation of qi Liquid mass transfer.
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