CN108507277A - A kind of the cold comprehensive utilization device and method of natural gas ethane recovery - Google Patents

A kind of the cold comprehensive utilization device and method of natural gas ethane recovery Download PDF

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Publication number
CN108507277A
CN108507277A CN201810398297.XA CN201810398297A CN108507277A CN 108507277 A CN108507277 A CN 108507277A CN 201810398297 A CN201810398297 A CN 201810398297A CN 108507277 A CN108507277 A CN 108507277A
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China
Prior art keywords
ice chest
cold
domethanizing column
gas
natural gas
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Pending
Application number
CN201810398297.XA
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Chinese (zh)
Inventor
周璇
尹奎
蒲黎明
田静
王毅
张庆林
陈云强
李莹珂
汪贵
刘棋
肖乐
郑春来
刘顺剑
汤晓勇
郭建
胡益武
袁唯唯
陆永康
刘艳
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China National Petroleum Corp
China Petroleum Engineering and Construction Corp
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China Petroleum Engineering and Construction Corp
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Priority to CN201810398297.XA priority Critical patent/CN108507277A/en
Publication of CN108507277A publication Critical patent/CN108507277A/en
Pending legal-status Critical Current

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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
    • F25J3/06—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation
    • F25J3/0605—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation characterised by the feed stream
    • F25J3/061—Natural gas or substitute natural gas
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/0204—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the feed stream
    • F25J3/0209—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
    • 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
    • F25J3/06—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation
    • F25J3/063—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation characterised by the separated product stream
    • F25J3/064—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation 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
    • F25J2200/04—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
    • F25J2200/40—Features relating to the provision of boil-up in the bottom of a column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/50—Processes or apparatus using separation by rectification using multiple (re-)boiler-condensers at different heights of the column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/74—Refluxing the column with at least a part of the partially condensed overhead 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
    • 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
    • F25J2210/00—Processes characterised by the type or other details of the feed stream
    • F25J2210/06—Splitting of the feed stream, e.g. for treating or cooling in different ways
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2210/00—Processes characterised by the type or other details of the feed stream
    • F25J2210/60—Natural gas or synthetic natural gas [SNG]
    • 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
    • F25J2215/62—Ethane or ethylene
    • 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
    • F25J2270/90—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration

Abstract

The invention discloses a kind of cold comprehensive utilization device of natural gas ethane recovery and methods, cold comprehensive utilization device includes sequentially connected ice chest, cold catch pot, expanding machine, domethanizing column and dethanizer, dethanizer is connected with deethanizer overhead condenser, deethanizer overhead return tank and deethanizer overhead reflux pump successively, the outlet of deethanizer overhead reflux pump is connected with deethanizer overhead entrance, and the gas phase of the outlet of deethanizer overhead return tank is connected with ice chest；Demethanizer bottom is equipped with demethanizer bottoms reboiler, and Deethanizer bottom is equipped with deethanization bottom reboiler, and the liquid hydrocarbon of domethanizing column middle and lower part returns to domethanizing column after ice chest.Different potential temperature colds are used the present invention, reduce external high-grade cold supply amount, expander is reduced than the load with reduction external refrigeration system, and cancels the supply of domethanizing column external heating system, reduces the construction investment and energy consumption of ethane recovery factory.

Description

A kind of the cold comprehensive utilization device and method of natural gas ethane recovery
Technical field
The present invention relates to ethane recovery technical field, specially a kind of process unit recycling for recycling ethane in natural gas is cold Amount, the method for reducing energy consumption are recycled the cold of domethanizing column difference potential temperature for the ethane recovery factory of different process It utilizes, outer refrigeration compressor load and expander ratio can be reduced, achieve the purpose that save equipment investment and reduce energy consumption.
Background technology
2016, Chinese ethylene production capacity reached 22,690,000 tons, is only second to the U.S. and is located at second, the equilibration device utilization of capacity Reach 96%, yield has had reached 21,700,000 tons, and equivalent consumption figure has reached 39,400,000 tons, and China's ethylene is self-supporting within 2016 Rate is 55%.The year two thousand twenty is expected, Chinese ethylene production capacity is up to 30,290,000 tons/year, and yield is 27,870,000 tons, and equivalent consumption needs It is 45,540,000 tons to ask, and the degree of self-sufficiency is about 61%, and import volume is about 17,670,000 tons.It expects 2025, it is contemplated that Chinese ethylene production capacity Speedup is slowed down, and import volume is about 20,960,000 tons.Ethane to ethylene has an advantage of " one high three is low ", i.e., olefin yields it is high, Factory's counter investment is low, production cost is low, low energy consumption, and production ethane product demand is more strong.Currently, outer defeated product is natural There are a large amount of ethane in gas, individually ethane is not used, to improve the utility value of natural gas, is more effectively utilized natural Gas realizes that product diversification, upgrading synergy greatly develop ethane recovery technology and be of great significance.
In natural gas ethane recovery device, domethanizing column temperature gradient it is larger (tower top be -120~~-90 DEG C, bottom of tower 0- 30 DEG C), and demethanizer bottoms thermic load is larger, if only recycling demethanizer bottoms (potential temperature is 0-30 DEG C) reboiler cold, 0-30 DEG C of cold surplus can be caused, external heating is needed, the cold of 0-30 DEG C of potential temperature is provided, and unstripped gas is pre-chilled and subcooling process In, the cold (such as -20~-90 DEG C) of the relatively GOOD TASTE of missing then needs swell refrigeration and external refrigeration system to supplement.It is i.e. natural Gas ethane recovery device heat-exchange system high-grade cold lacks, and low taste cold is superfluous, needs extraneous supplement high-grade cold Amount, low-grade heat.Ethane recovery device refrigeration system (expanding machine and external refrigeration system) is caused to become larger, heating system is same Shi Zeng great, therefore the construction investment of ethane recovery factory increases, energy consumption increases simultaneously.
Therefore the present invention proposes a kind of method of comprehensive utilization of natural gas ethane recovery device domethanizing column cold, will be different Potential temperature cold is used, and reduces external high-grade cold supply amount, that is, reduces expander ratio and reduce external refrigeration The load of system, and cancel the supply of domethanizing column external heating system.Reduce ethane recovery factory construction investment and Energy consumption.
Invention content
The shortcomings that in order to overcome the prior art, the present invention provides a kind of comprehensive utilizations of the cold of natural gas ethane recovery to fill It sets and method has the advantages that energy consumption of reducing investment outlay and reduce suitable for all ethane recovery devices.
The technical solution adopted in the present invention is：A kind of cold comprehensive utilization device of natural gas ethane recovery, including：It is cold Case, cold catch pot, expanding machine, domethanizing column and dethanizer, the dry natural gas outlet of the ice chest and cold catch pot The gas phase of connection, the cold catch pot outlet is connected directly with ice chest and expanding machine respectively, the liquid phase of cold catch pot outlet Be connected with domethanizing column, domethanizing column outlet gas phase be connected successively with ice chest and expanding machine, domethanizing column outlet liquid phase and Dethanizer be connected, dethanizer successively with deethanizer overhead condenser, deethanizer overhead return tank and dethanizer tower It pushes up reflux pump to be connected, the outlet of deethanizer overhead reflux pump is connected with deethanizer overhead entrance, deethanizer overhead reflux The gas phase of the outlet of tank is connected with ice chest；Demethanizer bottom is equipped with demethanizer bottoms reboiler, and Deethanizer bottom is equipped with de- The liquid hydrocarbon of ethane bottom reboiler, domethanizing column middle and lower part returns to domethanizing column after ice chest.
The present invention also provides a kind of cold method of comprehensive utilization of natural gas ethane recovery, include the following steps：20~ ~50 DEG C of dry natural gas enters ice chest precooling, and cold catch pot is entered after partial condensation, and the gas phase part isolated is logical Expanding machine is crossed, is directly entered domethanizing column after expansion, remainder gas phase goes successively to after ice chest further condenses and be subcooled, lead to Enter domethanizing column top after crossing the throttling of J-T valves；The liquid phase that cold catch pot is isolated is directly entered de- after being throttled by J-T valves Methane tower, demethanizer overhead outlet gas phase enter ice chest, and cold is recycled by ice chest, and expanding machine pressurized end is entered after re-heat and is increased To outer defeated compress cell after pressure；The C that domethanizing column bottom of tower comes out2+ it is directly entered dethanizer, after dethanizer is fractionated, The gas phase that tower top comes out passes through deethanizer overhead return tank gas-liquid point after deethanizer overhead condenser partial condensation From the liquid phase isolated returns to dethanizer after being pressurized by deethanizer overhead reflux pump and is used as overhead reflux liquid；According to reality The demand of border heat exchange, the liquid hydrocarbon of domethanizing column section is extracted out, and into ice chest, cold, portion are provided for unstripped gas precooling and condensation After dividing vaporization, domethanizing column is returned.
Compared with prior art, the positive effect of the present invention is：For all natural gas ethane recovery devices, by demethanation Tower difference potential temperature cold is recycled, and is had the advantages that reduce factory's one-time investment and is reduced plant energy consumption.
Description of the drawings
Examples of the present invention will be described by way of reference to the accompanying drawings, wherein：
Fig. 1 is the technological principle flow chart of the cold comprehensive utilization device of embodiment 1；
Fig. 2 is the technological principle flow chart of the cold comprehensive utilization device of embodiment 2；
Fig. 3 is the technological principle flow chart of the cold comprehensive utilization device of embodiment 3.
Specific implementation mode
Example 1
A kind of cold comprehensive utilization device of natural gas ethane recovery, as shown in Figure 1, including：Ice chest 1, cold catch pot 2, expanding machine 3,1#J-T valves 4,2#J-T valves 5,3#J-T valves 6, domethanizing column 7, domethanizing column bottom of tower reboiler 8, dethanizer 9, Deethanizer overhead condenser 10, deethanizer overhead return tank 11, deethanizer overhead reflux pump 12, dethanizer bottom of tower weight Boil device 13.
Ice chest 1 be ethane recovery device unstripped gas precooling and low temperature gas supercooling main heat exchange place, ice chest 1 successively with it is low Warm separator 2, expanding machine 3, domethanizing column 7 and domethanizing column bottom of tower reboiler 8 connect.
The gas phase that cold catch pot 2 exports is connected directly with ice chest 1 and expanding machine 3 respectively.
The liquid phase that cold catch pot 2 exports is connected directly with domethanizing column 7.
The gas phase that domethanizing column 7 exports is connected with ice chest 1 and expanding machine 3 successively.
The liquid phase that domethanizing column 7 exports is connected directly with dethanizer 9.
Dethanizer 9 flows back with deethanizer overhead condenser 10, deethanizer overhead return tank 11, deethanizer overhead The outlet of pump 12 is connected with 9 tower top entrance of dethanizer.
The portion is recycled for providing heat for 7 bottom of domethanizing column in 7 bottom of domethanizing column equipped with demethanizer bottoms reboiler 8 Divide cold that partial raw gas is pre-chilled, ensures the content of ethane in domethanizing column base oil；9 bottom of dethanizer is equipped with dethanizer Bottom reboiler 13 ensures the quality of product for providing heat for 9 bottom of dethanizer.
The present invention also provides a kind of cold method of comprehensive utilization of natural gas ethane recovery, include the following steps：
20~~50 DEG C of dry natural gas is connected with ice chest 1, and a part is pre-chilled by ice chest 1, and remaining drying contains second Alkane natural gas enters demethanizer bottoms reboiler 8, provides heat for 7 bottom of domethanizing column, dry natural gas returns cold after being pre-chilled In case 1, continue to be pre-chilled after mixing with the dry natural gas being pre-chilled by ice chest 1, cold catch pot 2 is entered after partial condensation, point The gas phase part separated out is directly entered domethanizing column 7 by expanding machine 3 after expansion, remainder gas phase goes successively to ice chest 1 After condensing and being subcooled, enter 7 top of domethanizing column after throttling by 2#J-T valves 5.
The liquid phase that cold catch pot 2 is isolated is directly entered domethanizing column 7 after throttling by 3#J-T valves 6.
The partial high pressure dry gas come from outer defeated compress cell is connected with ice chest 1, after condensing and being subcooled, is saved by 1#J-T valves 4 Enter 7 top of domethanizing column after stream.
7 top exit gas phase of domethanizing column enters ice chest 1, and cold is recycled by ice chest 1, and expanding machine 3 is entered after re-heat and is increased It to outer defeated compress cell after pressure side supercharging, takes outside a part of return mechanism, remainder is directly outer defeated.
The C that 7 bottom of tower of domethanizing column comes out2+ it is directly entered dethanizer 9, after the fractionation of dethanizer 9, tower top comes out Gas phase after 10 partial condensation of deethanizer overhead condenser, by 11 gas-liquid separation of deethanizer overhead return tank, point The liquid phase separated out after deethanizer overhead reflux pump 12, supercharging by returning to 9 overhead reflux liquid of dethanizer.Dethanizer top gas The cold needed in condensation process extracts liquid phase out from 7 middle part of domethanizing column, is 9 tower overhead gas of dethanizer according to the potential temperature of condensation Cold is mutually provided, while by its partial condensation, reduces the heat exchange load of demethanizer bottoms reboiler 8.
During unstripped gas is pre-chilled and condenses, the cold of a certain potential temperature section usually can be also lacked, according to what is actually exchanged heat Demand extracts certain section of the liquid hydrocarbon of domethanizing column 7 out, into ice chest 1, provides cold for unstripped gas precooling and condensation, part vaporizes Afterwards, domethanizing column 7 is returned.
In this example, the cold that is expanded by unstripped gas and extracts two strands of low temperature hydrocarbon liquid out from domethanizing column and be respectively Unstripped gas is pre-chilled and is condensed in ice chest 1 and 9 tower overhead gas condensing reflux of dethanizer provides cold.
In the present invention, from domethanizing column extract out two strands of low temperature hydrocarbon liquid relative position by ice chest lack cold potential temperature and The potential temperature of deethanizer reflux tank determines.
Domethanizing column and dethanizer are respectively equipped with reboiler in the present invention.
It can also be filler and the board-like form being combined that domethanizing column, which is plate column, in the present invention, and dethanizer can be Plate column can also be packed tower.
In the present invention, the gas phase that deethanization return tank of top of the tower is isolated is ethane product, can be transported outward according to factory's ethane The difference of mode determines defeated outside gas phase after whether ethane product continues to be condensed into liquid phase or re-heat recycling cold.
The liquid phase that dethanizer bottom comes out in the present invention is C3+, can be decided whether according to user demand by taking off the third butane Tower is fractionated to obtain and be sold outside propane, butane, LPG products and stable light hydrocarbon product, directly outer can also sell.Realize product diversification.
Example 2
Ethane recovery device is insufficient only with expander cold, and when needing external complement cold, refrigeration system can be with The precooling for being unstripped gas in ice chest and the partial condensation of condensation and dethanizer top gas provide cold.
Due to there is the presence of external refrigeration system, unlike example 1, increase domethanizing column survey line heat exchanger 14.20 The dry natural gas of~~50 DEG C is connected with ice chest 1, and a part is pre-chilled by ice chest 1, and remaining drying natural gas containing ethane is first Into demethanizer bottoms reboiler 8, provides heat for 7 bottom of domethanizing column and go successively to demethanation after dry natural gas is pre-chilled Tower survey line heat exchanger 14 exchanges heat with the low temperature hydrocarbon liquid extracted out in domethanizing column, is returned in ice chest 1 after partial condensation, then with pass through Continue to be pre-chilled after the dry natural gas mixing that ice chest 1 is pre-chilled, cold catch pot 2 is entered after partial condensation.
The three strands of low temperature hydrocarbon liquid extracted out in domethanizing column are respectively ice chest 1, domethanizing column survey line heat exchanger 14 and piptonychia Alkane bottom reboiler 8 provides cold.The expansion ratio of expanding machine and the cooling load of refrigeration system can be reduced.
Example 3
Unlike example 2：When the temperature of unstripped gas is with seasonal variations, winter unstripped gas cannot carry for demethanizer bottoms When heat for needing potential temperature, example 3 may be used.
20~~50 DEG C of dry natural gas is connected with ice chest 1, and a part is pre-chilled by ice chest 1, and remaining drying contains second Alkane natural gas is introduced into domethanizing column survey line heat exchanger 14, exchanges heat with the low temperature hydrocarbon liquid extracted out in domethanizing column, after partial condensation It returns in ice chest, continues to be pre-chilled after mixing with the dry natural gas being pre-chilled by ice chest 1, cold catch pot is entered after partial condensation 2。
The partial high pressure dry gas come from outer defeated compress cell is introduced into demethanizer bottoms reboiler 8, is carried for 7 bottom of domethanizing column Heating load enters back into ice chest 1 after high pressure dry gas is pre-chilled, and after condensing and being subcooled, enters demethanation after throttling by 1#J-T valves 4 7 top of tower.
Three of the above example proposes three kinds of different cryogenic energy utilization schemes, cannot include all according to the condition of unstripped gas Cold Comprehensive Utilization Scheme, but the thinking similar with Utilization plan proposed by the present invention belongs to the scope of this patent.

Claims (8)

1. a kind of cold comprehensive utilization device of natural gas ethane recovery, it is characterised in that：Including：It is ice chest, cold catch pot, swollen The dry natural gas outlet of swollen machine, domethanizing column and dethanizer, the ice chest is connect with cold catch pot, the cryogenic separation The gas phase of device outlet is connected directly with ice chest and expanding machine respectively, and the liquid phase of cold catch pot outlet is connected with domethanizing column, takes off The gas phase of methane tower outlet is connected with ice chest and expanding machine successively, and the liquid phase of domethanizing column outlet is connected with dethanizer, takes off second Alkane tower is connected with deethanizer overhead condenser, deethanizer overhead return tank and deethanizer overhead reflux pump successively, takes off second The outlet of alkane column overhead reflux pump is connected with deethanizer overhead entrance, the gas phase of the outlet of deethanizer overhead return tank with it is cold Case is connected；Demethanizer bottom is equipped with demethanizer bottoms reboiler, and Deethanizer bottom is equipped with deethanization bottom reboiler, piptonychia The liquid hydrocarbon of alkane tower middle and lower part returns to domethanizing column after ice chest.
2. a kind of cold comprehensive utilization device of natural gas ethane recovery according to claim 1, it is characterised in that：It is dry Natural gas enters by demethanizer bottoms reboiler in ice chest；The high pressure dry gas that outer defeated compress cell comes passes through after ice chest J-T valves enter demethanizer overhead；Liquid phase in the middle part of domethanizing column returns after deethanizer overhead condenser recycles cold Domethanizing column.
3. a kind of cold comprehensive utilization device of natural gas ethane recovery according to claim 1, it is characterised in that：It is described Ice chest is connect with refrigeration system；Dry natural gas passes through demethanizer bottoms reboiler successively and domethanizing column survey line heat exchanger is laggard Enter in ice chest；The high pressure dry gas that outer defeated compress cell comes enters demethanizer overhead after ice chest by J-T valves.
4. a kind of cold comprehensive utilization device of natural gas ethane recovery according to claim 1, it is characterised in that：It is described Ice chest is connect with refrigeration system；Dry natural gas enters by domethanizing column survey line heat exchanger in ice chest；Outer defeated compress cell comes High pressure dry gas successively enter demethanizer bottoms reboiler and ice chest, enter demethanizer overhead after then throttling by J-T valves.
5. a kind of cold method of comprehensive utilization of natural gas ethane recovery, it is characterised in that：Include the following steps：20~~50 DEG C Dry natural gas enter ice chest precooling, cold catch pot is entered after partial condensation, the gas phase part isolated passes through expansion Machine, is directly entered domethanizing column after expansion, remainder gas phase goes successively to after ice chest condenses and be subcooled, throttle by J-T valves Enter domethanizing column top afterwards；The liquid phase that cold catch pot is isolated is directly entered domethanizing column, piptonychia after throttling by J-T valves Alkane top of tower outlet gas phase enters ice chest, and cold is recycled by ice chest, enters after re-heat after expanding machine pressurized end is pressurized to outer defeated Compress cell；The C that domethanizing column bottom of tower comes out2+ it is directly entered dethanizer, after dethanizer is fractionated, what tower top came out Gas phase, by deethanizer overhead return tank gas-liquid separation, is isolated after deethanizer overhead condenser partial condensation Liquid phase returns to dethanizer after being pressurized by deethanizer overhead reflux pump and is used as overhead reflux liquid；According to the need actually to exchange heat It asks, the liquid hydrocarbon of domethanizing column section is extracted out, into ice chest, cold is provided and is returned after part vaporizes for unstripped gas precooling and condensation Return domethanizing column.
6. a kind of cold method of comprehensive utilization of natural gas ethane recovery according to claim 5, it is characterised in that：20~ ~50 DEG C of dry natural gas parts enter ice chest precooling, and another part enters demethanizer bottoms reboiler, for demethanation Bottom of tower provides heat and returns after being pre-chilled in ice chest, continues to be pre-chilled after mixing with the dry natural gas being pre-chilled by ice chest, portion Enter cold catch pot after dividing condensation；The partial high pressure dry gas come from outer defeated compress cell is connected with ice chest, after condensing and being subcooled, Enter demethanizer overhead after throttling by J-T valves；The cold needed in dethanizer top gas condensation process, according to the temperature of condensation Position extracts liquid phase out from domethanizing column middle part, cold is provided for deethanizer overhead gas phase.
7. a kind of cold method of comprehensive utilization of natural gas ethane recovery according to claim 5, it is characterised in that：Work as second Alkane retracting device is insufficient only with expander cold, and when needing external complement cold, it is that unstripped gas exists to increase refrigeration system The partial condensation of precooling and condensation and domethanizing column top gas in ice chest provides cold；20~~50 DEG C of dry natural gas one Part is pre-chilled into ice chest, and another part enters demethanizer bottoms reboiler, for demethanizer bottoms provide heat and by After precooling, domethanizing column survey line heat exchanger is gone successively to, exchanges heat with the low temperature hydrocarbon liquid extracted out in domethanizing column, is returned after partial condensation It returns in ice chest, then continues to be pre-chilled after mixing with the dry natural gas being pre-chilled by ice chest, cold catch pot is entered after partial condensation； The partial high pressure dry gas come from outer defeated compress cell is connected with ice chest, after condensing and being subcooled, enters piptonychia after throttling by J-T valves Alkane top of tower.
8. a kind of cold method of comprehensive utilization of natural gas ethane recovery according to claim 5, it is characterised in that：Work as original When the temperature of material gas cannot provide the heat for needing potential temperature for demethanizer bottoms, increase refrigeration system is unstripped gas in ice chest Precooling and the partial condensation of condensation and domethanizing column top gas provide cold；20~~50 DEG C of dry natural gas parts enter Ice chest is pre-chilled, and another part enters domethanizing column survey line heat exchanger, is exchanged heat with the low temperature hydrocarbon liquid extracted out in domethanizing column, portion It is returned in ice chest after dividing condensation, continues to be pre-chilled after mixing with the dry natural gas being pre-chilled by ice chest, entered after partial condensation low Warm separator；The partial high pressure dry gas come from outer defeated compress cell is introduced into demethanizer bottoms reboiler, is carried for demethanizer bottoms Heating load enters back into ice chest after high pressure dry gas is pre-chilled, and after condensing and being subcooled, enters domethanizing column top after throttling by J-T valves Portion.
CN201810398297.XA 2018-04-28 2018-04-28 A kind of the cold comprehensive utilization device and method of natural gas ethane recovery Pending CN108507277A (en)

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