CN203837413U - Device for extracting ethane and hydrocarbon mixture from natural gas - Google Patents
Device for extracting ethane and hydrocarbon mixture from natural gas Download PDFInfo
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- CN203837413U CN203837413U CN201420234335.5U CN201420234335U CN203837413U CN 203837413 U CN203837413 U CN 203837413U CN 201420234335 U CN201420234335 U CN 201420234335U CN 203837413 U CN203837413 U CN 203837413U
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- natural gas
- ethane
- compressor
- catch pot
- heat exchanger
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- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 title claims abstract description 87
- 239000003345 natural gas Substances 0.000 title claims abstract description 45
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 title claims abstract description 40
- 229930195733 hydrocarbon Natural products 0.000 title claims abstract description 40
- 239000004215 Carbon black (E152) Substances 0.000 title claims abstract description 39
- 150000002430 hydrocarbons Chemical class 0.000 title claims abstract description 39
- 239000000203 mixture Substances 0.000 title abstract 4
- 239000007791 liquid phase Substances 0.000 claims abstract description 23
- 239000000284 extract Substances 0.000 claims description 13
- 239000007792 gaseous phase Substances 0.000 claims description 10
- 239000003915 liquefied petroleum gas Substances 0.000 claims description 7
- 239000007789 gas Substances 0.000 abstract description 34
- 239000012071 phase Substances 0.000 abstract description 12
- 238000005057 refrigeration Methods 0.000 abstract description 10
- 239000007788 liquid Substances 0.000 abstract description 6
- 238000005516 engineering process Methods 0.000 abstract description 2
- 238000012423 maintenance Methods 0.000 abstract description 2
- 238000004519 manufacturing process Methods 0.000 abstract description 2
- 239000003507 refrigerant Substances 0.000 abstract 1
- 238000000034 method Methods 0.000 description 19
- 239000000047 product Substances 0.000 description 13
- 238000009833 condensation Methods 0.000 description 9
- 230000005494 condensation Effects 0.000 description 9
- 230000001105 regulatory effect Effects 0.000 description 7
- 238000011084 recovery Methods 0.000 description 5
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 description 4
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 description 3
- 239000005977 Ethylene Substances 0.000 description 3
- 230000005540 biological transmission Effects 0.000 description 3
- 238000001816 cooling Methods 0.000 description 3
- 238000000605 extraction Methods 0.000 description 3
- 239000003921 oil Substances 0.000 description 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 2
- 238000010521 absorption reaction Methods 0.000 description 2
- 238000005336 cracking Methods 0.000 description 2
- 239000010779 crude oil Substances 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 239000001294 propane Substances 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- 239000002904 solvent Substances 0.000 description 2
- 238000012546 transfer Methods 0.000 description 2
- 229910021529 ammonia Inorganic materials 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 239000012467 final product Substances 0.000 description 1
- 238000005194 fractionation Methods 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- -1 natural gas hydrocarbons Chemical class 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 description 1
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 description 1
- 238000010992 reflux Methods 0.000 description 1
- 230000008961 swelling Effects 0.000 description 1
Classifications
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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
- F25J2200/70—Refluxing the column with a condensed part of the feed stream, i.e. fractionator top is stripped or self-rectified
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- 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
- F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
- F25J2230/08—Cold compressor, i.e. suction of the gas at cryogenic temperature and generally without afterstage-cooler
-
- 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
Landscapes
- Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Mechanical Engineering (AREA)
- Thermal Sciences (AREA)
- General Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Separation By Low-Temperature Treatments (AREA)
Abstract
The utility model discloses a device for extracting an ethane and hydrocarbon mixture from natural gas. The device for extracting the ethane and hydrocarbon mixture from natural gas comprises a heat exchanger, a compressor, an expansion machine, a first-level low-temperature separator, a second-level low-temperature separator and a demethanizer. The heat exchanger is sequentially connected with the first-level low-temperature separator, the expansion machine, the second-level low-temperature separator and the compressor. The compressor is connected with the heat exchanger and the demethanizer. A liquid phase outlet of the first-level low-temperature separator and a liquid phase outlet of the second-level low-temperature separator are connected with the demethanizer. A gas phase outlet of the second-level low-temperature separator is further directly connected with the demethanizer. According to the device for extracting the ethane and hydrocarbon mixture from natural gas, pressure is increased through the compressor, after heat exchange is conducted on expanding gas, the expanding gas is condensed, liquid is supercooled through throttling and depressurization, and cold energy is provided for deep deethanization, wherein the compressor is effective and reliable. Compared with the technologies that deethanization is conducted through refrigeration by means of mixed refrigerants, the requirement for the compressor is low, the investment is small, the manufacturing period is short, one refrigerating system is omitted, operation and maintenance are simpler, and therefore the total project investment is greatly reduced.
Description
Technical field
The utility model relates to a kind of device that reclaims the mixed hydrocarbon of ethane from natural gas, especially a kind of device that extracts the mixed hydrocarbon of ethane from natural gas.
Background technology
The C of current most of natural gas processing plant light ends unit
3 +the rate of recovery is only 15 ~ 25%, reclaims the degree of depth only for meeting the requirement of outer gas transmission hydrocarbon dew point, therefore also has most of hydrocarbon component not recycle.In view of hydrocarbon resource abundant in most natural gases, before natural gas is defeated outside, be all necessary to extract mixed hydrocarbon resource.Abundant ethane resource in while natural gas, as the optimum feed stock of cracking ethylene, the huge market demand, prospect is better, can effectively save crude oil consumption, indirectly realizes with gas for oil.
Natural gas ethane recovery technique mainly contains low temperature oil-absorption process, stepwise refrigeration/azeotrope refrigerating method etc. at present.Low temperature oil-absorption process needs a large amount of recycled solvent oils, and solvent naphtha has certain loss, and ethane recovery is lower, generally only has 60% ethane recovery.And stepwise refrigeration/azeotrope refrigerating method be by outer refrigeration process by ethane condensation, be generally applicable to the situation that raw gas pressure is lower.
Utility model content
The purpose of this utility model is: for the problem of above-mentioned existence, provide a kind of device that extracts the mixed hydrocarbon of ethane from natural gas.
A kind of device that extracts the mixed hydrocarbon of ethane from natural gas, comprise heat exchanger, compressor, decompressor, one-level cold catch pot, secondary cold catch pot, domethanizing column, described heat exchanger is connected with one-level cold catch pot, decompressor, secondary cold catch pot, compressor successively, compressor is connected with heat exchanger, domethanizing column again, the liquid-phase outlet of the liquid-phase outlet of one-level cold catch pot and secondary cold catch pot is connected with domethanizing column respectively, and a gaseous phase outlet of secondary cold catch pot is also directly connected with domethanizing column.
Preferably, at the bottom of the tower of domethanizing column, be also provided with reboiler or LPG fractionating column.
Above-mentioned domethanizing column can be preferably packed tower or plate column.
Wherein, the liquid-phase outlet of one-level cold catch pot is preferably connected with domethanizing column by choke valve.Above-mentioned heat exchanger is preferably connected with domethanizing column by choke valve.
Preferably, in order to reclaim cold and the energy of gas product, the product gas outlet of demethanizer column overhead is connected with coaxial compressing expansion machine with heat exchanger successively.
Above-mentioned heat exchanger provides the place of energy exchange for cold-producing medium and other logistics; Decompressor is main refrigeration plant, for natural gas deep cooling provides cold; Compressor is demi-inflation air compressor, and demi-inflation air compressor is by natural gas boosting, and condensation deutomerite flows through cold, as demethanizer column overhead phegma; Domethanizing column is as the mass transfer place of extracting the mixed hydrocarbon of ethane.
The utility model also provides a kind of method of extracting the mixed hydrocarbon of ethane from natural gas that adopts shallow cryogen precooling to combine with swelling agent refrigeration.
The utility model is by the following technical solutions:
A kind of method of extracting the mixed hydrocarbon of ethane from natural gas, the shallow cold cold-producing medium of natural gas via is chilled to after-37 ℃ in advance, separated through one-level cold catch pot, the gas phase of separating is through decompressor, preferably coaxial compressing expansion machine, be cooled to after-61 ℃ (3.5MPa), enter secondary cold catch pot separated, the isolated a part of gas phase of secondary cold catch pot enters heat exchanger heat exchange to-75 ℃ of condensations after compressor is pressurized to 6MPa, then by reducing pressure by regulating flow to 3.5MPa excessively cold (96 ℃), enter domethanizing column, the isolated another part gas phase of secondary cold catch pot is directly to domethanizing column, the isolated liquid phase of one-level cold catch pot and the isolated liquid phase of secondary cold catch pot enter domethanizing column, liquid phase at the bottom of demethanizer is the mixed hydrocarbon of ethane, the gas of demethanizer column overhead is the gas product that contains a small amount of ethane.
In a preferred embodiment, the isolated liquid phase of one-level cold catch pot enters domethanizing column after reducing pressure by regulating flow together with the isolated liquid phase of secondary cold catch pot.
The gas pressure of above-mentioned demethanizer column overhead is preferably higher, as 3.0～3.7MPa, can effectively dwindle tower diameter and the volume of demethanation, is conducive to save gross investment.
In said method, according to downstream product needs, reboiler or LPG fractionating column etc. can be set at the bottom of demethanizer, to collect flexibly liquefied petroleum gas (LPG) and light oil etc.
In order to reclaim cold and the energy of gas product, the gas product of demethanation tower top can also be discharged and collected again successively after heat exchanger and coaxial compressing expansion machine.
Shallow cold cold-producing medium of the present invention refers to a class cold-producing medium that gas at normal temperature is cooled to-35 ℃ of left and right, such as propane, propylene, ammonia and R134a, commonly uses cold-producing medium etc.
Adopt said method, the mixed hydrocarbon yield of ethane in natural gas is up to 75% left and right, and the mixed hydrocarbon yield of propane is especially up to more than 98%.
The utility model is by the compressor boost condensation after gas heat exchange that makes to expand, then by reducing pressure by regulating flow, make this logistics excessively cold, for degree of depth deethanization provides cold, compressor mature and reliable wherein, adopt azeotrope refrigeration deethanization technique to compare with other, that compressor requires is lower, it is less to invest, manufacturing schedule is short, few a set of refrigeration system, and Operation and Maintenance is more succinct simultaneously, and total investment of engineering of the present utility model is declined to a great extent; The mixed hydrocarbon extraction effect of ethane is good, outside guaranteeing under the prerequisite of defeated gas product calorific value, the mixed hydrocarbon of ethane in natural gas is removed as much as possible, for cracking ethylene provides quality raw materials, be conducive to reduce crude oil consumption, ensure that the raw material of ethylene industry provides, effectively avoid outer gas transmission liquid hydrocarbon to separate out simultaneously, can optimize national energy structure, and effectively utilize product; In natural gas, extract the mixed hydrocarbon technological process of ethane simple, reduced investment, in more traditional extraction natural gas, the mixed hydrocarbon technological process of ethane is simplified greatly, the relevant devices such as special refrigeration system have been reduced, by natural gas condensation throttling, cross cold reflux and in domethanizing column, can reach the mixed hydrocarbon of deep natural gas extraction ethane, reclaim the hydrocarbon resource in natural gas, meet the needs of natural gas hydrocarbons dew point.
Accompanying drawing explanation
Fig. 1 is the structure connection diagram of the device of embodiment 3.
The specific embodiment
Below in conjunction with accompanying drawing, the utility model is described in detail.
In order to make the purpose of this utility model, technical scheme and advantage clearer, below in conjunction with drawings and Examples, the utility model is further elaborated.Should be appreciated that specific embodiment described herein is only in order to explain the utility model, and be not used in restriction the utility model.
Embodiment 1
A kind of method of extracting the mixed hydrocarbon of ethane from natural gas, the shallow cold cold-producing medium of natural gas via is chilled to after-37 ℃ in advance, separated through one-level cold catch pot, the gas phase of separating is through decompressor, preferably coaxial compressing expansion machine, be cooled to after-61 ℃ (3.5MPa), enter secondary cold catch pot separated, the isolated gas phase of secondary cold catch pot is divided into two parts, wherein fraction gas phase (for example 30%) enters heat exchanger heat exchange to-75 ℃ of condensations after compressor is pressurized to 6MPa, then by reducing pressure by regulating flow to 3.5MPa excessively cold (96 ℃), enter demethanizer column overhead as liquid backflow liquid, the isolated another part gas phase of secondary cold catch pot directly to domethanizing column as charging, the isolated liquid phase of one-level cold catch pot enters domethanizing column as charging with the isolated liquid phase of secondary cold catch pot after reducing pressure by regulating flow, natural gas is shunted at domethanizing column inner transmission matter, liquid at the bottom of demethanizer is the mixed hydrocarbon of ethane, the gas of demethanizer column overhead is the gas product that contains a small amount of ethane.
The method of the present embodiment is utilized shallow cold cold-producing medium precooling natural gas, cold or deep cooling during the high-pressure natural gas swell refrigeration of process precooling reaches, again that cooling natural gas boosting, condensation and throttling is excessively cold, as demethanizer column overhead phegma, thereby remove the mixed hydrocarbon of most ethane in natural gas, effectively reduce plant energy consumption.
Embodiment 2
A kind of device that extracts the mixed hydrocarbon of ethane from natural gas, comprise heat exchanger, compressor, decompressor, one-level cold catch pot, secondary cold catch pot, domethanizing column, heat exchanger is connected with one-level cold catch pot, the gaseous phase outlet of one-level cold catch pot is connected with decompressor, decompressor is connected with secondary cold catch pot, secondary cold catch pot has two gaseous phase outlets, one of them gaseous phase outlet is connected with compressor, compressor more successively with heat exchanger, domethanizing column is connected, another gaseous phase outlet of secondary cold catch pot, and the liquid-phase outlet of one-level cold catch pot, the liquid-phase outlet of secondary cold catch pot is connected with domethanizing column respectively, according to actual needs, at the bottom of the tower of domethanizing column, be also provided with reboiler or LPG fractionating column.
In other embodiment, the liquid-phase outlet of one-level cold catch pot can also be connected with domethanizing column by choke valve, and heat exchanger can also be connected with domethanizing column by choke valve.
Embodiment 3
A kind of natural gas extracts the process unit of the mixed hydrocarbon of ethane, as shown in Figure 1, comprising: heat exchanger-1, compressor-2, coaxial compressing expansion machine-3, one-level cold catch pot-4, secondary cold catch pot-5, choke valve (a)-6, choke valve (b)-7, domethanizing column-8, demethanizer bottoms reboiler-9.Wherein:
Heat exchanger 1 is connected with one-level cold catch pot 4, the gaseous phase outlet of one-level cold catch pot 4 is connected with coaxial compressing expansion machine 3, coaxial compressing expansion machine 3 is connected with secondary cold catch pot 5, secondary cold catch pot 5 has two gaseous phase outlets, one of them gaseous phase outlet is connected with compressor 2, compressor 2 is connected with heat exchanger 1, heat exchanger 1 is connected with the charging aperture 8 of domethanizing column by choke valve (b) 7 again, another gaseous phase outlet of secondary cold catch pot 5 and the liquid-phase outlet of secondary cold catch pot 5 are connected with the charging aperture of domethanizing column 8 respectively, the liquid-phase outlet of one-level cold catch pot 4 is connected with the charging aperture of domethanizing column 8 by choke valve (a) 6, at the bottom of the tower of domethanizing column, be also provided with demethanizer bottoms reboiler 9, the overhead product gas outlet of domethanizing column 8 is connected with coaxial compressing expansion machine 3 with heat exchanger 1 successively.
Above-mentioned domethanizing column can be both that packed tower can be also plate column.
Embodiment 4
Natural gas extracts a method for the mixed hydrocarbon of ethane, and step is as follows:
Unstripped gas and shallow cold cold-producing medium are chilled in advance after-37 ℃ in heat exchanger, separated through one-level cold catch pot gas-liquid two-phase, gas phase to decompressor is expanded to 3.5MPa(-61 ℃), enter secondary cold catch pot separated, second-stage separator gas phase is out divided into two parts, part gas phase (70%) is directly to domethanizing column, a residue part (30%) enters heat exchanger heat exchange to-75 ℃ of condensations by compressor boost to 6MPa, then reducing pressure by regulating flow is to 3.5MPa excessively cold (96 ℃), then enter domethanizing column, after the liquid phase reducing pressure by regulating flow of one-level cold catch pot, enter domethanizing column, the liquid phase of secondary cold catch pot directly enters domethanizing column, natural gas carries out mass transfer fractionation in domethanizing column, demethanizer top gas is the gas product that contains a small amount of ethane, domethanizing column bottom liquid phase is the mixed hydrocarbon product of ethane, demethanizer top gas reclaims cold and the coaxial compressing expansion machine pressure recovery energy of process through heat exchanger respectively.According to the needs of product, by improving domethanizing column bottom reboiler temperature (being increased to 108 ℃ by 57 ℃), get final product depropanization or in downstream, increase LPG fractionating column etc.30% the low-flash natural gas because only have an appointment, after compressor compresses, condensation is crossed cold for domethanizing column provides cold, greatly reduces the energy consumption of whole device.
The foregoing is only preferred embodiment of the present utility model; not in order to limit the utility model; all any modifications of doing within spirit of the present utility model and principle, be equal to and replace and improvement etc., within all should being included in protection domain of the present utility model.
Claims (6)
1. one kind is extracted from natural gas the device that ethane mixes hydrocarbon, it is characterized in that, comprise heat exchanger, compressor, decompressor, one-level cold catch pot, secondary cold catch pot, domethanizing column, described heat exchanger is connected with one-level cold catch pot, decompressor, secondary cold catch pot, compressor successively, compressor is connected with heat exchanger, domethanizing column again, the liquid-phase outlet of the liquid-phase outlet of one-level cold catch pot and secondary cold catch pot is connected with domethanizing column respectively, and a gaseous phase outlet of secondary cold catch pot is also directly connected with domethanizing column.
2. a kind of device that extracts the mixed hydrocarbon of ethane from natural gas as claimed in claim 1, is characterized in that, is also provided with reboiler at the bottom of the tower of described domethanizing column.
3. a kind of device that extracts the mixed hydrocarbon of ethane from natural gas as claimed in claim 1, is characterized in that, is also provided with LPG fractionating column at the bottom of the tower of described domethanizing column.
4. a kind of device that extracts the mixed hydrocarbon of ethane from natural gas as described in arbitrary claim in claim 1-3, is characterized in that, described domethanizing column is packed tower or plate column.
5. a kind of device that extracts the mixed hydrocarbon of ethane from natural gas as described in arbitrary claim in claim 1-3, is characterized in that, the liquid-phase outlet of one-level cold catch pot is connected with domethanizing column by choke valve.
6. a kind of device that extracts the mixed hydrocarbon of ethane from natural gas as described in arbitrary claim in claim 1-3, is characterized in that, described heat exchanger is connected with domethanizing column by choke valve.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201420234335.5U CN203837413U (en) | 2014-05-09 | 2014-05-09 | Device for extracting ethane and hydrocarbon mixture from natural gas |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201420234335.5U CN203837413U (en) | 2014-05-09 | 2014-05-09 | Device for extracting ethane and hydrocarbon mixture from natural gas |
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| Publication Number | Publication Date |
|---|---|
| CN203837413U true CN203837413U (en) | 2014-09-17 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201420234335.5U Expired - Lifetime CN203837413U (en) | 2014-05-09 | 2014-05-09 | Device for extracting ethane and hydrocarbon mixture from natural gas |
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103940199A (en) * | 2014-05-09 | 2014-07-23 | 中国石油集团工程设计有限责任公司 | Method and device for extracting ethane-mixed hydrocarbon from natural gas |
| CN107548446A (en) * | 2015-05-04 | 2018-01-05 | 通用电气石油和天然气公司 | Prepare the hydrocarbon stream for storage |
| CN108759305A (en) * | 2018-06-11 | 2018-11-06 | 西南石油大学 | A kind of natural gas ethane recovery methods to flow back more |
| CN108759306A (en) * | 2018-06-13 | 2018-11-06 | 中国石油工程建设有限公司 | A kind of LNG recycling ethane mixes the process unit and method of hydrocarbon |
| RU2794122C1 (en) * | 2023-02-03 | 2023-04-11 | Общество с ограниченной ответственностью научно-исследовательский и проектный институт "ПЕГАЗ" | Hydrocarbon gas preparation system for supply to the demethanizer (options) |
-
2014
- 2014-05-09 CN CN201420234335.5U patent/CN203837413U/en not_active Expired - Lifetime
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103940199A (en) * | 2014-05-09 | 2014-07-23 | 中国石油集团工程设计有限责任公司 | Method and device for extracting ethane-mixed hydrocarbon from natural gas |
| CN107548446A (en) * | 2015-05-04 | 2018-01-05 | 通用电气石油和天然气公司 | Prepare the hydrocarbon stream for storage |
| US10928128B2 (en) | 2015-05-04 | 2021-02-23 | GE Oil & Gas, Inc. | Preparing hydrocarbon streams for storage |
| CN108759305A (en) * | 2018-06-11 | 2018-11-06 | 西南石油大学 | A kind of natural gas ethane recovery methods to flow back more |
| CN108759305B (en) * | 2018-06-11 | 2019-08-23 | 西南石油大学 | A kind of natural gas ethane recovery methods to flow back more |
| CN108759306A (en) * | 2018-06-13 | 2018-11-06 | 中国石油工程建设有限公司 | A kind of LNG recycling ethane mixes the process unit and method of hydrocarbon |
| RU2794122C1 (en) * | 2023-02-03 | 2023-04-11 | Общество с ограниченной ответственностью научно-исследовательский и проектный институт "ПЕГАЗ" | Hydrocarbon gas preparation system for supply to the demethanizer (options) |
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