CN106256813B - A kind of separation and recovery method of Fischer-Tropsch process exhaust - Google Patents
A kind of separation and recovery method of Fischer-Tropsch process exhaust Download PDFInfo
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- CN106256813B CN106256813B CN201510333938.XA CN201510333938A CN106256813B CN 106256813 B CN106256813 B CN 106256813B CN 201510333938 A CN201510333938 A CN 201510333938A CN 106256813 B CN106256813 B CN 106256813B
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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
- F25J3/0219—Refinery gas, cracking gas, coke oven gas, gaseous mixtures containing aliphatic unsaturated CnHm or gaseous mixtures of undefined nature
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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
- F25J3/0228—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
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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
- F25J3/0228—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
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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
- F25J3/0228—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
- F25J3/0252—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 hydrogen
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- 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
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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
- 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
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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
- F25J2210/00—Processes characterised by the type or other details of the feed stream
- F25J2210/12—Refinery or petrochemical off-gas
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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
- F25J2215/00—Processes characterised by the type or other details of the product stream
- F25J2215/04—Recovery of liquid products
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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
- F25J2270/00—Refrigeration techniques used
- F25J2270/04—Internal refrigeration with work-producing gas expansion loop
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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
- F25J2270/00—Refrigeration techniques used
- F25J2270/08—Internal refrigeration by flash gas recovery loop
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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
- F25J2270/00—Refrigeration techniques used
- F25J2270/12—External refrigeration with liquid vaporising loop
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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
- F25J2270/00—Refrigeration techniques used
- F25J2270/60—Closed external refrigeration cycle with single component refrigerant [SCR], e.g. C1-, C2- or C3-hydrocarbons
Abstract
The invention discloses a kind of separation and recovery methods of Fischer-Tropsch process exhaust, Fischer-Tropsch process exhaust is first carried out thick gas-liquid separation by this method, then demethanation processing is carried out after the gaseous product that thick gas-liquid separation obtains successively being cooled down in domethanizing column together with the product liquid that thick gas-liquid separation obtains, after obtained separation product carries out a series of subsequent processings, thick hydrogen production, liquefied natural gas and other hydrocarbon products have been obtained.Method flow of the invention is simple and direct, few using number of devices, and investment and land occupation are saved, and product recovery rate is high, and comprehensive energy consumption is lower.
Description
Technical field
The present invention relates to a kind of separation and recovery methods of Fischer-Tropsch process exhaust.
Background technique
The coal resources very abundant of China, coal chemical industry are the emerging strategic fields of one of China, develop at the early-stage, side
Xing Weiai.In the indirect liquefaction technique of coal oil, the synthesis tail gas of a set of 1,000,000 tons/year of Low Temperature Fischer Tropsch synthesizers generation
More than 40 ton/hours, and a set of 1,000,000 tons/year of high temperature FT synthesizer generate synthesis tail gas be even more more than 100 ton/hours,
Wherein H2、CH4、C2H4And C3H6Equal hydrocarbon components content is considerable, is effectively recycled, economic value is significant.
FT synthesis tail gas, which removes, contains a small amount of oxygen-containing organic compound and a certain amount of CO2Outside, also contain very high mole
The H of concentration2、N2, CO, Ar and CH4Etc. low boiling components, the total gas volume of C2 ' s and C2 ' s+ hydro carbons Zhan 10~13% (weight
Amount accounts for 30~50%).The processing target of FT synthesis tail gas separator seeks to remove these objectionable impurities, recycle therein
Useful constituent, makes ethylene and propylene reach polymer grade, methane reaches LNG (i.e. liquefied natural gas) standard, thick hydrogen send PSA to refine,
And other hydrocarbon products are isolated as much as possible.
Since coal chemical industry is a new industry, FT synthesis tail gas compared with various light hydrocarbon gas (such as ethylene unit is split
Vent one's spleen, MTO technology gas, dehydrogenating propane reaction gas, oil refinery dry gas, natural gas and coke-stove gas etc.), component and content
It all differs greatly, product separation requirement is also without so comprehensive, so there is presently no a kind of ready-made process for separating and recovering skills
Art can be directly used.
Summary of the invention
The object of the present invention is to provide a kind of separation and recovery method of Fischer-Tropsch process exhaust, this method process is simple and direct, uses
Number of devices is few, and investment and land occupation are saved, and product recovery rate is high, and comprehensive energy consumption is lower.
To achieve the goals above, the present invention provides a kind of separation and recovery method of Fischer-Tropsch process exhaust, this method comprises:
A, will containing nitrogen, argon gas, carbon monoxide, carbon dioxide, hydrogen, methane, ethane, ethylene, propane, propylene, butane, butylene and
The Fischer-Tropsch process exhaust of gasoline component successively carries out carbon dioxide removal processing, compression processing, cooling treatment, gas-liquid separation and drying
After processing, the gas phase Fischer-Tropsch process exhaust and liquid phase Fischer-Tropsch process exhaust of 14~17 DEG C and 3.6~3.9 megapascal are obtained；It b, will step
Gas phase Fischer-Tropsch process exhaust obtained in rapid a carries out the condensation of first order propylene using two sections of propylene refrigerants, obtains -15~-19 DEG C
With the first order propylene condensed product of 3.69~3.89 megapascal；The first order propylene condensed product is used into one section of propylene refrigerant
The condensation of second level propylene is carried out, the second level propylene condensed product of -30~-34 DEG C and 3.68~3.88 megapascal is obtained；It c, will step
Second level propylene condensed product obtained in rapid b carries out the first ethylene Quench using two sections of ethylene cryogens, obtain through gas-liquid separation-
The the first ethylene shock gas and the first ethylene Quench liquid of 50~-60 DEG C and 3.66~3.86 megapascal；By first ethylene
Shock gas carries out the second ethylene Quench using one section of ethylene cryogen, obtains -96~-98 DEG C and 3.6~3.8 million through gas-liquid separation
Second ethylene shock gas of pa and the second ethylene Quench liquid；The second ethylene shock gas is provided by off-gas expander
Cooling capacity is further condensed, through gas-liquid separation obtain the first time methane of -160 DEG C~-165 DEG C and 3.58~3.78 megapascal/
Hydrogen separates gas and first time methane/hydrogen separates liquid；By the first time methane/hydrogen separation liquid be warming up to -101 DEG C~-
102 DEG C and 3.09~3.29 megapascal are fed as first burst of demethanation；D, by liquid phase Fischer-Tropsch process exhaust obtained in step a
After cooling decompression to -53~-57 DEG C and 3.2~3.4 megapascal, liquid phase Fischer-Tropsch process exhaust before demethanation is handled is obtained；It e, will step
Gained is de- in first burst of demethanation charging of gained, the second ethylene Quench liquid and the first ethylene Quench liquid and step d in rapid c
Liquid phase Fischer-Tropsch process exhaust carries out demethanation processing under -100~-105 DEG C and 3.00~3.20 megapascal before methane processing, obtains
Demethanation gas to -102~-105 DEG C and 3.00~3.20 megapascal and ethylene contents less than 0.2mol% and 50~55 DEG C
With the demethanation liquid of 3.07~3.27 megapascal；F, by first time obtained in demethanation gas obtained in step e and step c
Methane/hydrogen separates gas mixing, after entering off-gas expander swell refrigeration together, carries out second of methane/hydrogen separation, obtain-
175~-180 DEG C separate hydrogen and expansion separation of methane with the expansion of 0.25~0.33 megapascal；G, by gained expansion point in step f
From hydrogen successively in step c gained the second ethylene shock gas and the first ethylene shock gas, step b in obtained by the second level third
Alkene condensed product and gas phase Fischer-Tropsch process exhaust described in first order propylene condensed product, step a and 38~40 DEG C of propylene are cold
Agent liquid obtains the thick hydrogen production of room temperature after being exchanged heat.
Preferably, wherein the processing of carbon dioxide removal described in step a successively includes washing or amine is washed and alkali cleaning.
Preferably, this method further include: α, by step f gained more than half expansion separation of methane and second second
Alkene shock gas exchanges heat, and obtains first strand of heat exchange expansion separation of methane gas；Gained demi-inflation in step f is separated into first
Overhead condensation heat exchange of the alkane for demethanation processing in step e obtains second strand of heat exchange expansion separation of methane gas；By step f
After the expansion separation of methane of middle gained remainder is vaporized heating treatment, third stock heat exchange expansion separating methane gas is obtained
Body；β, first burst of heat exchange expansion separation of methane gas, second burst of heat exchange described in step α are expanded into separation of methane gas and third
Stock heat exchange expansion separation of methane gas merges into total heat exchange expansion separating methane gas of -100~-104 DEG C and 0.26-0.28 megapascal
After body, after further heating up processing to room temperature, then alternately most compression processings three times and cooling treatment, 38- is obtained
The expansion separation of methane gas of the compression cooling treatment of 40 DEG C and 5.0-6.5 megapascal；γ, it will be compressed at cooling described in step β
After the expansion separation of methane gas of reason carries out desuperheating, liquefies again and cross cold treatment, expenditure and pressure obtains -162~-163 DEG C
With 15~20 kPas of liquefied natural gas product；δ, the flashed vapour of liquefied natural gas product described in step γ is subjected to two-stage liter
After temperature processing, after alternately 2~3 times boostings and cooling, it is used as fuel gas.
Preferably, this method further include: one section of ethylene cryogen and two sections of ethylene cryogens used in the step c, with step
The ethylene cryogen used that liquefies again for expanding separation of methane gas in γ after compression cooling treatment, comes from same ethylene refrigeration
Machine.
Preferably, this method further include: by the vaporization heating treatment of the expansion separation of methane of remainder described in step α
Cooling capacity caused by first order heating treatment with the flashed vapour of liquefied natural gas product described in step δ is for institute in step γ
That states the expansion separation of methane gas of compression cooling treatment crosses cold treatment.
Preferably, this method further include: always heat exchange expansion separation of methane gas described in step β is further heated up into place
Cooling capacity caused by the second level heating treatment of reason and the flashed vapour of liquefied natural gas product described in step δ is in step γ
The desuperheating processing of the expansion separation of methane gas of the compression cooling treatment.
Preferably, this method further include: function needed for the compression processing of always heat exchange expansion separation of methane gas described in step β
Rate is all provided by the off-gas expander in step f.
Preferably, this method further include: by gained demethanation liquid in step e in -12~-16 DEG C and 2.1~2.3 megapascal
Lower progress deethanization processing obtains the deethanization gas containing ethylene and ethane and contains propane, propylene, butane, butylene and vapour
The deethanization liquid of oil ingredient；The deethanization gas is subjected to ethylene distillation, obtains ethylene and ethane；By the deethanization liquid
Body carries out depropanization processing in 13~17 DEG C and 0.65~0.85 megapascal, obtains the depropanization gas containing propane and propylene and contains
There is the depropanization liquid of butane, butylene and gasoline component；The depropanization gas is subjected to propylene rectifying, obtains propylene and third
Alkane；The depropanization liquid is subjected to debutanization processing in 46~50 DEG C and 0.35~0.45 megapascal, obtains the mixing carbon of liquid
The gasoline component of four products and liquid.
Method of the invention can be to H2、N2, CO, Ar and CH4The equal very high FT synthesis tail gas of amount of components having low boiling points carries out
It is successfully separated, removes objectionable impurities, recycled hydrocarbon component to the maximum extent, ethylene and propylene can be made to reach polymer grade, methane
Reach liquefied natural gas (i.e. LNG) standard.H in thick hydrogen2Yield >=99.9%；Yield of ethene >=99.1%；Other heavy hydrocarbons
Yield is almost 100%.Machine, energy saving are recompressed using off-gas expander driving methane.
Other features and advantages of the present invention will the following detailed description will be given in the detailed implementation section.
Detailed description of the invention
The drawings are intended to provide a further understanding of the invention, and constitutes part of specification, with following tool
Body embodiment is used to explain the present invention together, but is not construed as limiting the invention.In the accompanying drawings:
Fig. 1 is the schematic diagram that the present invention includes the used device of specific embodiment that demethanation is handled；
Fig. 2 is that the specific embodiment that the present invention is separated including Fischer-Tropsch process exhaust pretreatment with demethanation liquid is used
The schematic diagram of device.
Description of symbols
1 6# hydrogen recuperator, 2 5# hydrogen recuperator, 3 4# hydrogen recuperator
4 3# hydrogen recuperator, 5 2# hydrogen recuperator, 6 1# hydrogen recuperator
7 Fischer-Tropsch tail gas 1# condenser, 8 Fischer-Tropsch tail gas 2# condenser, 9 Fischer-Tropsch tail gas 1# ethylene condenser
10 Fischer-Tropsch tail gas 2# ethylene condenser, 11 Fischer-Tropsch tail gas undercooling device
12 domethanizing columns first feed 13 domethanizing column second of knockout drum and feed knockout drum
14 domethanizing column thirds feed 15 demethanizer reboiler of knockout drum, 16 domethanizing column
17 domethanizing column condenser, 18 demethanizer reflux tank, 19 expanding machine head tank
20 off-gas expander, 21 22 hydrogen of liquid phase throttle valve/23 gas phase Fischer-Tropsch process exhaust of methane separation tank
Thick 26 propylene refrigerant of hydrogen production, the 27 demethanation liquid of 24 liquid phase Fischer-Tropsch process exhaust 25
28 natural 29 methane of gas condenser recompression, one section of 30 methane of machine recompress two sections of machine
31 methane recompress three section of 32 methane of machine and recompress the first aftercooler of machine
33 methane recompress 34 methane of the second aftercooler of machine and recompress machine third aftercooler
35 37 gas product of low temperature methane JT 36 natural gas storage tank of valve, 38 natural gas 1# heat exchanger
39 natural gas 2# heat exchanger, one section 41 of 40 BOG compressor, two sections of BOG compressor
42 the first aftercooler of BOG compressor, 43 the second aftercooler of BOG compressor, 44 fuel gas
45 Fischer-Tropsch process exhaust, 46 water scrubber, 47 Fischer-Tropsch tail gas heater, 48 caustic wash tower
49 alkali cleaning tower top cooler, 50 Fischer-Tropsch tail gas increases by 51 Fischer-Tropsch tail gas of machine suction tank and increases machine
52 Fischer-Tropsch tail gas dryer feed deep freezer, 53 dryer feed knockout drum
54 Fischer-Tropsch tail gas gas phase drier, 55 Fischer-Tropsch tail gas liquid phase drier, 56 dethanizer
57 ethylene rectifying column, 58 59 depropanizing tower of deethanization tower reactor cooler, 60 propylene rectification tower
61 debutanizing tower, 62 ethylene, 63 ethane, 64 propylene, 65 propane
66 mixing four product of carbon, 67 gasoline components
Specific embodiment
Below in conjunction with attached drawing, detailed description of the preferred embodiments.It should be understood that this place is retouched
The specific embodiment stated is merely to illustrate and explain the present invention, and is not intended to restrict the invention.
The present invention provides a kind of separation and recovery method of Fischer-Tropsch process exhaust, this method comprises: a, will contain nitrogen, argon
Gas, carbon monoxide, carbon dioxide, hydrogen, methane, ethane, ethylene, propane, propylene, butane, butylene and gasoline component Fischer-Tropsch
After synthesis tail gas successively carries out carbon dioxide removal processing, compression processing, cooling treatment, gas-liquid separation and drying process, 14 are obtained
The gas phase Fischer-Tropsch process exhaust and liquid phase Fischer-Tropsch process exhaust of~17 DEG C and 3.6~3.9 megapascal；B, by gas obtained in step a
Phase Fischer-Tropsch process exhaust carries out the condensation of first order propylene using two sections of propylene refrigerants, obtains -15~-19 DEG C and 3.69~3.89 million
The first order propylene condensed product of pa；The first order propylene condensed product is subjected to second level propylene using one section of propylene refrigerant
Condensation, obtains the second level propylene condensed product of -30~-34 DEG C and 3.68~3.88 megapascal；It c, will be second obtained in step b
Grade propylene condensed product carries out the first ethylene Quench using two sections of ethylene cryogens, obtains -50~-60 DEG C and 3.66 through gas-liquid separation
First ethylene shock gas of~3.86 megapascal and the first ethylene Quench liquid；The first ethylene shock gas is used one section
Ethylene cryogen carries out the second ethylene Quench, obtains the second ethylene Quench of -96~-98 DEG C and 3.6~3.8 megapascal through gas-liquid separation
Gas and the second ethylene Quench liquid；By the second ethylene shock gas by off-gas expander provide cooling capacity carry out further it is cold
It is solidifying, -160 DEG C~-165 DEG C, which are obtained, through gas-liquid separation separates gas and first with the first time of 3.58~3.78 megapascal methane/hydrogen
Secondary methane/hydrogen separates liquid；The first time methane/hydrogen separation liquid is warming up to -101 DEG C~-102 DEG C and 3.09~3.29
Megapascal is fed as first burst of demethanation；D, by liquid phase Fischer-Tropsch process exhaust cooling decompression obtained in step a to -53~-57
DEG C and 3.2~3.4 megapascal after, obtain liquid phase Fischer-Tropsch process exhaust before demethanation is handled；E, by first strand of piptonychia of gained in step c
Liquid phase Fischer-Tropsch before gained demethanation is handled in alkane charging, the second ethylene Quench liquid and the first ethylene Quench liquid and step d
Synthesis tail gas carries out demethanation processing under -100~-105 DEG C and 3.00~3.20 megapascal, obtains -102~-105 DEG C and 3.00
The demethanation gas of~3.20 megapascal and ethylene contents less than 0.2mol% and 50~55 DEG C and 3.07~3.27 megapascal take off
Methane liquid；F, demethanation gas obtained in step e is separated into gas mixing with the methane of first time obtained in step c/hydrogen,
After entering off-gas expander swell refrigeration together, carry out the separation of second of methane/hydrogen, obtain -175~-180 DEG C and 0.25~
The expansion separation hydrogen and expansion separation of methane of 0.33 megapascal；G, by gained expansion separation hydrogen in step f successively and in step c
Gained second level propylene condensed product and the first order in gained the second ethylene shock gas and the first ethylene shock gas, step b
Gas phase Fischer-Tropsch process exhaust described in propylene condensed product, step a and 38~40 DEG C of propylene refrigerant liquid obtain after being exchanged heat
To the thick hydrogen production of room temperature.
According to the present invention, gas-liquid separation processing is first time simple separation in step a, therefore the gas phase F- T synthesis tail
Gas is similar with the substance classes contained by liquid phase Fischer-Tropsch process exhaust, but the content of substance is different, gas phase Fischer-Tropsch process exhaust
Containing more light component, liquid phase Fischer-Tropsch process exhaust contains more heavy constituent.The master of first ethylene shock gas described in step c
Wanting ingredient is nitrogen, argon gas, carbon monoxide, hydrogen, methane, ethylene, ethane and propylene etc., and the first ethylene Quench liquid contains
The heavy constituent of three or more carbon is more；The main component of the second ethylene shock gas is nitrogen, argon gas, carbon monoxide, hydrogen
Gas, methane, ethylene and ethane etc., heavy constituent of the second ethylene Quench liquid then containing two or more carbon are more；Described
Methane/hydrogen separation gas main component is hydrogen, nitrogen, carbon monoxide, argon gas and methane etc., first time methane/hydrogen
The main component for separating liquid is methane, ethylene and ethane etc..Ethylene contents are less than in demethanation gas described in step e
0.2mol% and it is rich in methane, the main component of the demethanation liquid is the component of two or more carbon.It is expanded described in step f
The main component for separating hydrogen is hydrogen, nitrogen, carbon monoxide, argon gas and a small amount of methane, the master of the expansion separation of methane
Wanting ingredient is methane.
According to the present invention, the processing of carbon dioxide removal described in step a and drying process are that those skilled in the art institute is ripe
Know, the carbon dioxide removal processing can successively include washing or amine is washed and alkali cleaning, and the drying process can use 3A
The desiccant such as molecular sieve are dried.
A kind of specific embodiment according to the present invention, the separation and recovery method can also include: α, by step f gained
The expansion separation of methane of more than half exchanges heat with the second ethylene shock gas, obtains first burst of heat exchange expansion separation first
Alkane gas；Gained demi-inflation separation of methane in step f is used for the overhead condensation heat exchange that demethanation is handled in step e, is obtained
Second burst of heat exchange expands separation of methane gas；The expansion separation of methane of gained remainder in step f is vaporized at heating
After reason, third stock heat exchange expansion separation of methane gas is obtained；β, first burst of heat exchange described in step α is expanded into separating methane gas
Body, second burst of heat exchange expansion separation of methane gas and third stock heat exchange expansion separation of methane gas merge into -100~-104 DEG C and
After total heat exchange expansion separation of methane gas of 0.26-0.28 megapascal, further heats up and handle to room temperature, then alternately most
After more compression processings three times and cooling treatment, obtains 38-40 DEG C and separate first with the expansion of the compression cooling treatment of 5.0-6.5 megapascal
Alkane gas；γ, the expansion separation of methane gas that cooling treatment is compressed described in step β is subjected to desuperheating, again liquefaction and mistake
After cold treatment, expenditure and pressure obtains the liquefied natural gas product of -162~-163 DEG C and 15~20 kPas；δ, by institute in step γ
After the flashed vapour progress two-stage heating treatment for stating liquefied natural gas product, after alternately 2~3 times boostings and cooling, it is used as combustion
Expect gas.Wherein, the processing of desuperheating described in step γ can take heat exchange mode, and liquefaction can be using ethylene refrigeration etc. again
Condensing mode, crossing cold treatment can also be by the way of heat exchange；Flashed vapour described in step δ is well known to those skilled in the art
, refer to that the boiling point of the liquid can reduce, even lower than the liquid when the decline of the pressure of high-pressure liquid substance
Temperature, so that the gas that instantaneous portion vaporization occurs and generates, becomes flashed vapour.
An ethylene refrigeration machine system can be set using two sections in a kind of specific embodiment according to the present invention, the present invention
Ethylene cryogen carries out two-stage ethylene Quench, and the temperature of first order ethylene Quench can be -50~-62 DEG C, second level ethylene Quench
Temperature can be -95~-98 DEG C, therefore, this method can also include: one section of ethylene cryogen and two used in the step c
The ethylene cryogen used that liquefies again of separation of methane gas is expanded in section ethylene cryogen, with step γ after compression cooling treatment,
From same ethylene refrigeration machine.In addition, the present invention can carry out three-level propylene refrigeration, the first order third using three sections of propylene refrigerants
The temperature of alkene condensation can be lower than -30 DEG C, and the temperature of second level propylene condensation can be between -20~-15 DEG C, third level propylene
Refrigeration, can be at 10 DEG C or more.The propylene refrigeration or ethylene refrigeration, which refer to, is pressed using propylene or ethylene as refrigerant
The refrigerating method that contracting, liquefaction re-vaporization are freezed.
A kind of specific embodiment according to the present invention, this method can also include: by remainder described in step α
Expand the first order heating treatment of the flashed vapour for vaporizing liquefied natural gas product described in heating treatment and step δ of separation of methane
Expansion separation of methane gas of the generated cooling capacity for compressing cooling treatment described in step γ crosses cold treatment.The cooling capacity
Refer to the concept opposite with heat, moves away heat and generate.
A kind of specific embodiment according to the present invention, this method can also include: by always heat exchange expansion described in step β
At the second level heating of the flashed vapour for further heating up liquefied natural gas product described in processing and step δ of separation of methane gas
Desuperheating processing of the cooling capacity caused by managing for the expansion separation of methane gas of compression cooling treatment described in step γ.
A kind of specific embodiment according to the present invention, this method can also include: always heat exchange expansion point described in step β
Power needed for compression processing from methane gas is all provided by the off-gas expander in step f.The off-gas expander refers to
Exporting mechanical work when expanding and be depressured using the industrial tail gas of high pressure outward makes the principle of gas temperature reduction to obtain more energy
Machinery, temperature more lower than direct expenditure and pressure can be obtained.
A kind of specific embodiment according to the present invention, this method can also include: by gained demethanation liquid in step e
Deethanization processing is carried out under -12~-16 DEG C and 2.1~2.3 megapascal, is obtained the deethanization gas containing ethylene and ethane and is contained
There is the deethanization liquid of propane, propylene, butane, butylene and gasoline component；The deethanization gas is subjected to ethylene distillation, is obtained
Ethylene and ethane；The deethanization liquid is subjected to depropanization processing in 13~17 DEG C and 0.65~0.85 megapascal, is contained
The depropanization gas of propane and propylene and depropanization liquid containing butane, butylene and gasoline component；By the depropanization gas
Propylene rectifying is carried out, propylene and propane are obtained；The depropanization liquid is taken off in 46~50 DEG C and 0.35~0.45 megapascal
Butane treatment obtains the gasoline component of mixing carbon four products and liquid of liquid.
It is provided below the boiling point of Common materials contained by Fischer-Tropsch process exhaust under normal pressure: nitrogen, -195.8 DEG C；Argon gas ,-
185.7℃；Carbon monoxide, -191.4 DEG C；Methane, -164.5 DEG C；Hydrogen, -252.8 DEG C；Ethane, -88.6 DEG C；Ethylene ,-
109.4℃；Propane, -42.1 DEG C；Normal butane, -0.5 DEG C；Butylene, -6.9 DEG C；Iso-butane, -12 DEG C.But due to present invention side
Pressure used by method is higher than normal pressure, so, at a higher temperature, relatively heavy substance contained by Fischer-Tropsch process exhaust can liquid
Change, thus can reach the purpose of separation.
The present invention will be illustrated by embodiment below, but method of the invention is not therefore and by any limit
System.
As shown in Fig. 2, will containing nitrogen, argon gas, carbon monoxide, carbon dioxide, hydrogen, methane, ethane, ethylene, propane,
Propylene, butane, butylene and gasoline component Fischer-Tropsch process exhaust successively pass through the water scrubber of Fischer-Tropsch process exhaust pretreatment unit
46, Fischer-Tropsch tail gas heater 47, caustic wash tower 48, alkali cleaning top cooler 49, Fischer-Tropsch tail gas increase machine 51, demethanizer reboiler 15
With successively carry out carbon dioxide removal processing, compression processing, cooling treatment in Fischer-Tropsch tail gas dryer feed deep freezer 52 after enter
Gas-liquid separation processing is carried out in dryer feed knockout drum 53, being separated into the tail gas of gas phase and liquid phase, to enter Fischer-Tropsch tail gas gas phase dry
After dry device 54 and Fischer-Tropsch tail gas liquid phase drier 55 are dried, the gas phase F- T synthesis of 15 DEG C and 3.81 megapascal is obtained
Tail gas and liquid phase Fischer-Tropsch process exhaust.
As shown in Figure 1, gas phase Fischer-Tropsch process exhaust is successively passed through 5# hydrogen recuperator 2 and Fischer-Tropsch tail gas 1# condenser 7
The condensation of first order propylene is carried out, the first order propylene condensed product of -17 DEG C and 3.79 megapascal is obtained；First order propylene is condensed and is produced
Object successively passes through 4# hydrogen recuperator 3 and Fischer-Tropsch tail gas 2# condenser 8 carries out the condensation of second level propylene, obtains -32 DEG C and 3.78
The second level propylene condensed product of megapascal；By second level propylene condensed product according to pass through 3# hydrogen recuperator 4 and Fischer-Tropsch tail gas 1#
Ethylene condenser 9 is sent into the charging progress gas-liquid separation of knockout drum 12 of domethanizing column first after carrying out the first ethylene Quench, obtains -55
DEG C and 3.74 megapascal the first ethylene shock gas and the first ethylene Quench liquid；The first ethylene shock gas is successively passed through
It crosses 2# hydrogen recuperator 5 and Fischer-Tropsch tail gas 2# ethylene condenser 10 carries out the feeding charging of domethanizing column second after the second ethylene Quench
Knockout drum 13 carries out gas-liquid separation, obtains the second ethylene shock gas and the second ethylene Quench liquid of -98 DEG C and 3.7 megapascal；
Above-mentioned second ethylene shock gas is sent into domethanizing column third charging knockout drum 14 after 1# hydrogen recuperator 6 and carries out gas-liquid
Separation obtains -160 DEG C and separates gas and the first methane/hydrogen separation liquid with the first methane of 3.68 megapascal/hydrogen；By the first first
Alkane/hydrogen separation liquid is warming up to -101.5 DEG C and 3.19 megapascal by 1# hydrogen recuperator 6, feeds as first burst of demethanation.
Wherein the hydrogen recuperator is plate-fin.
By liquid phase Fischer-Tropsch process exhaust by Fischer-Tropsch tail gas undercooling device 11 carry out cooling decompression after, obtain -54 DEG C and
Liquid phase Fischer-Tropsch process exhaust before the demethanation of 3.3 megapascal is handled.By above-mentioned first burst of demethanation charging, the second ethylene Quench liquid
Liquid phase Fischer-Tropsch process exhaust is sequentially sent to the first charging of domethanizing column 16 before body, the first ethylene Quench liquid and demethanation are handled
Distribution grid, the second feed distributing plate, third feed distributing plate and the 4th feed distributing plate are in -101 DEG C and 3.10 megapascal (tower top)
Lower progress demethanation processing obtains the demethanation liquid of demethanation top gaseous phase and 52 DEG C and 3.13 megapascal, by demethanation tower top
Gas phase is sent into demethanizer reflux tank 18 after domethanizing column condenser 17 is condensed and carries out gas-liquid separation, obtains -103 DEG C
With 3.1 megapascal and ethylene contents are the demethanation gas of 0.10mol%.Wherein, domethanizing column is single column high pressure demethanizer, tower
It is pressed between 3.00~3.16MPaG, tower reactor mainly increases machine outlet gas phase by FT tail gas and provides boiling hot amount again；Overhead reflux
It than very little, but needs to provide -106 DEG C of cooling capacity below by off-gas expander system, effectively to control ethylene loss.
After demethanation gas is separated gas mixing with the first methane/hydrogen from domethanizing column third charging knockout drum 14
It is sent into expanding machine head tank 19 together, obtained product liquid passes through after liquid phase throttle valve 21 throttles and be sent into off-gas expander 20
Gaseous product after refrigeration is sent into hydrogen/methane separation tank 22 together and carries out gas-liquid separation, obtains the swollen of -177 DEG C and 0.29 megapascal
Swollen separation hydrogen and expansion separation of methane；The liquid reflux that demethanizer reflux tank 18 is obtained is returned in domethanizing column 16.Wherein,
The methane concentration for expanding separation of methane is 93.3mol% (generally should be greater than 92mol%).Expansion separation hydrogen is successively passed through
1# hydrogen recuperator 6,2# hydrogen recuperator 5,3# hydrogen recuperator 4,4# hydrogen recuperator 3,5# hydrogen recuperator 2 and 6# hydrogen
Recuperator 1 successively with the second ethylene shock gas, the first ethylene shock gas, second level propylene condensed product, first order propylene
Condensed product, gas phase Fischer-Tropsch process exhaust and 39 DEG C of propylene refrigerant liquid (for absorbing cooling capacity) exchange heat, and obtain often
The thick hydrogen production of temperature.
52% expansion separation of methane is sent into 1# hydrogen recuperator 6 to exchange heat with the second ethylene shock gas, is obtained
First burst of heat exchange expands separation of methane gas；22% expansion separation of methane is sent into domethanizing column condenser 17 and domethanizing column
Overhead condensation heat exchange, obtain second burst of heat exchange and expand separation of methane gas；The expansion separation of methane of residue 26% is sent into day
Right gas 1# heat exchanger 38 exchanges heat, and obtains third stock heat exchange expansion separation of methane gas.By three strands of expansion separation of methane gases
It is sent into natural gas 2# heat exchanger 39 after converging to be further heated up to room temperature, then is sequentially sent to methane and recompresses one section of machine
29, methane recompression the first aftercooler of machine 32, two section 30 of machine of methane recompression, methane recompress the second aftercooler of machine 33, methane
Three section 31 of recompression machine and methane recompression machine third aftercooler 34 carry out alternate compression and cooling treatment, obtain 39 DEG C and
The expansion separation of methane gas of the compression cooling treatment of 5.7 megapascal；The expansion separation of methane gas of cooling treatment will be compressed successively
By natural gas 2# heat exchanger 39, natural gas condenser 28 and natural gas 1# heat exchanger 38 carry out desuperheating, again liquefaction and it is cold
But it after handling, is re-fed into low temperature methane JT valve 35 and carries out expenditure and pressure, obtain -163 DEG C and 20 kPas of liquefied natural gas (i.e.
LNG) product is deposited in atmospheric low-temperature list and is contained in the natural gas storage tank 36 of pattern；By flash distillation caused by natural gas storage tank 36
After gas (i.e. bubble point gas BOG) is sequentially sent to natural gas 1# heat exchanger 38 and the heating of natural gas 2# heat exchanger 39, then it is sequentially sent to BOG
One section 40 of compressor, the first aftercooler of BOG compressor 42, two section 41 of BOG compressor and the second aftercooler of BOG compressor 43 carry out
After alternately boosting and being cooling, it is used as fuel gas.Wherein, the driver of methane recompression machine is off-gas expander, BOG compressor
Driver is motor；Cooling capacity required for the condensation of gas phase Fischer-Tropsch tail gas most cold grade, domethanizing column condensation and LNG are subcooled, all by
Off-gas expander provides.
As shown in Fig. 2, demethanation liquid feeding dethanizer 56 is carried out at deethanization under -14 DEG C and 2.23 megapascal
Reason, obtains the deethanization gas containing ethylene and ethane and the deethanization containing propane, propylene, butane, butylene and gasoline component
Liquid；Deethanization gas is sent into ethylene rectifying column 57 and carries out ethylene distillation, obtains ethylene and ethane；By the deethanization liquid
It is sent into depropanizing tower 59 after the cooling of deethanization tower reactor cooler 58 and carries out depropanization processing in 15 DEG C and 0.76 megapascal, obtains
Depropanization gas containing propane and propylene and the depropanization liquid containing butane, butylene and gasoline component；By depropanization gas
It is sent into propylene rectification tower 60 and carries out propylene rectifying, obtain propylene and propane；Depropanization liquid is sent into debutanizing tower 61 at 48 DEG C
Debutanization processing is carried out with 0.42 megapascal, obtains the gasoline component of mixing carbon four products and liquid of liquid.
H in the embodiment in thick hydrogen2Yield >=99.9%；Yield of ethene >=99.1%；Other above heavy hydrocarbons of ethylene
Yield is almost 100%；Ethylene with propylene reaches polymer grade, methane reaches liquefied natural gas (i.e. LNG) standard.It is expanded with tail gas
Machine drives methane to recompress machine, energy saving.The tail gas for such as handling a set of 1,000,000 tons/year of high temperature FT synthesis, can economize on electricity about daily
57000 degree.
Claims (8)
1. a kind of separation and recovery method of Fischer-Tropsch process exhaust, this method comprises:
A, will containing nitrogen, argon gas, carbon monoxide, carbon dioxide, hydrogen, methane, ethane, ethylene, propane, propylene, butylene and
The Fischer-Tropsch process exhaust of gasoline component successively carries out carbon dioxide removal processing, compression processing, cooling treatment, gas-liquid separation and drying
After processing, the gas phase Fischer-Tropsch process exhaust and liquid phase Fischer-Tropsch process exhaust of 14~17 DEG C and 3.6~3.9 megapascal are obtained；
B, gas phase Fischer-Tropsch process exhaust obtained in step a is subjected to the condensation of first order propylene using two sections of propylene refrigerants, obtain-
The first order propylene condensed product of 15~-19 DEG C and 3.69~3.89 megapascal；The first order propylene condensed product is used one
Section propylene refrigerant carries out the condensation of second level propylene, and the second level propylene condensation for obtaining -30~-34 DEG C and 3.68~3.88 megapascal produces
Object；
C, propylene condensed product in the second level obtained in step b is subjected to the first ethylene Quench using two sections of ethylene cryogens, through gas
The the first ethylene shock gas and the first ethylene Quench liquid of liquid isolated -50~-60 DEG C and 3.66~3.86 megapascal；By institute
State the first ethylene shock gas and the second ethylene Quench carried out using one section of ethylene cryogen, through gas-liquid separation obtain -96~-98 DEG C and
Second ethylene shock gas of 3.6~3.8 megapascal and the second ethylene Quench liquid；By the second ethylene shock gas by tail gas
Expanding machine provides cooling capacity and is further condensed, and obtains the of -160 DEG C~-165 DEG C and 3.58~3.78 megapascal through gas-liquid separation
Methane/hydrogen separation gas and first time methane/hydrogen separate liquid；The first time methane/hydrogen separation liquid is warming up to-
101 DEG C~-102 DEG C and 3.09~3.29 megapascal are fed as first burst of demethanation；
D, it by after liquid phase Fischer-Tropsch process exhaust cooling decompression obtained in step a to -53~-57 DEG C and 3.2~3.4 megapascal, obtains
Liquid phase Fischer-Tropsch process exhaust before being handled to demethanation；
E, by first burst of demethanation charging of gained, the second ethylene Quench liquid and the first ethylene Quench liquid and step in step c
Liquid phase Fischer-Tropsch process exhaust carries out piptonychia under -100~-105 DEG C and 3.00~3.20 megapascal before gained demethanation is handled in rapid d
Alkane processing, obtain the demethanation gas of -102~-105 DEG C and 3.00~3.20 megapascal and ethylene contents less than 0.2mol% with
The demethanation liquid of 50~55 DEG C and 3.07~3.27 megapascal；
F, demethanation gas obtained in step e is separated into gas mixing with the methane of first time obtained in step c/hydrogen, together
Into after off-gas expander swell refrigeration, second of methane/hydrogen separation is carried out, -175~-180 DEG C and 0.25~0.33 million are obtained
The expansion separation hydrogen and expansion separation of methane of pa；
G, gained expansion separation hydrogen in step f is successively swashed with the second ethylene shock gas of gained in step c with the first ethylene
Gas phase Fischer-Tropsch described in second level propylene condensed product obtained by cold air, step b and first order propylene condensed product, step a
Synthesis tail gas and 38~40 DEG C of propylene refrigerant liquid obtain the thick hydrogen production of room temperature after being exchanged heat.
2. the method according to claim 1, wherein carbon dioxide removal described in step a processing successively include washing or amine wash, with
And alkali cleaning.
3. the method according to claim 1, this method further include:
α, more than half expansion separation of methane of gained in step f is exchanged heat with the second ethylene shock gas, is obtained
First burst of heat exchange expands separation of methane gas；Gained demi-inflation separation of methane in step f is used to demethanation in step e to handle
Overhead condensation heat exchange, obtain second burst of heat exchange and expand separation of methane gas；By the expansion separation of gained remainder in step f
After methane is vaporized heating treatment, third stock heat exchange expansion separation of methane gas is obtained；
β, the expansion of first burst of heat exchange described in step α separation of methane gas, second burst of heat exchange are expanded to separation of methane gas and the
Three strands of heat exchange expansion separation of methane gases merge into total heat exchange expansion separation of methane of -100~-104 DEG C and 0.26-0.28 megapascal
After gas, after further heating up processing to room temperature, then alternately most compression processings three times and cooling treatment, obtain
The expansion separation of methane gas of the compression cooling treatment of 38-40 DEG C and 5.0-6.5 megapascal；
γ, the expansion separation of methane gas that cooling treatment is compressed described in step β is carried out at desuperheating, again liquefaction and supercooling
After reason, expenditure and pressure obtains the liquefied natural gas product of -162~-163 DEG C and 15~20 kPas；
δ, it after the flashed vapour of liquefied natural gas product described in step γ is carried out two-stage heating treatment, rises for alternately 2~3 times
After pressure and cooling, it is used as fuel gas.
4. according to the method in claim 3, this method further include: one section of ethylene cryogen and two sections of ethylene used in the step c
The ethylene cryogen used that liquefies again for expanding separation of methane gas in cryogen, with step γ after compression cooling treatment, from same
One ethylene refrigeration machine.
5. according to the method in claim 3, this method further include: by the expansion separation of methane of remainder described in step α
Cooling capacity caused by the first order heating treatment of the flashed vapour of liquefied natural gas product described in heating treatment and step δ is vaporized to use
The expansion separation of methane gas of the compression cooling treatment described in step γ crosses cold treatment.
6. according to the method in claim 3, this method further include: by always heat exchange expansion separation of methane gas described in step β
Further heat up cooling capacity caused by the second level heating treatment of the flashed vapour of liquefied natural gas product described in processing and step δ
The desuperheating processing of expansion separation of methane gas for compression cooling treatment described in step γ.
7. according to the method in claim 3, this method further include: the pressure of always heat exchange expansion separation of methane gas described in step β
Power needed for contracting is handled all is provided by the off-gas expander in step f.
8. the method according to claim 1, this method further include:
Gained demethanation liquid in step e is subjected to deethanization processing under -12~-16 DEG C and 2.1~2.3 megapascal, is contained
There are the deethanization gas of ethylene and ethane and the deethanization liquid containing propane, propylene, butylene and gasoline component；
The deethanization gas is subjected to ethylene distillation, obtains ethylene and ethane；By the deethanization liquid at 13~17 DEG C and
0.65~0.85 megapascal carries out depropanization processing, obtains the depropanization gas containing propane and propylene and contains butylene and gasoline group
The depropanization liquid divided；
The depropanization gas is subjected to propylene rectifying, obtains propylene and propane；By the depropanization liquid at 46~50 DEG C and
0.35~0.45 megapascal carries out debutanization processing, obtains the gasoline component of mixing carbon four products and liquid of liquid.
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| BR112019009939A2 (en) * | 2016-11-17 | 2019-08-20 | Sasol South Africa Ltd | process for hydrocarbon recovery from a gas stream |
| CN108276236B (en) * | 2017-01-06 | 2020-08-04 | 中国石化工程建设有限公司 | Cryogenic separation and recovery method for Fischer-Tropsch synthesis tail gas for increasing olefin yield |
| CN106938170B (en) * | 2017-03-31 | 2023-02-28 | 武汉金中石化工程有限公司 | Treatment device and treatment method for Fischer-Tropsch synthesis purge gas of cobalt-based fixed bed |
| CN109704899B (en) * | 2017-10-26 | 2022-07-08 | 中国石油化工股份有限公司 | Method for preparing olefin from synthesis gas |
| CN108676579B (en) * | 2018-05-09 | 2023-04-25 | 天津市天地创智科技发展有限公司 | Dry gas sequential separation system and separation method based on argon circulation refrigeration |
| CN109111336B (en) * | 2018-09-28 | 2024-04-05 | 北京恒泰洁能科技有限公司 | Deep cooling recovery device and process for waste towed synthetic tail gas |
| CN111116299A (en) * | 2018-10-30 | 2020-05-08 | 中国石油化工股份有限公司 | Method and device for product separation and byproduct utilization of olefin prepared from synthesis gas |
| CN109321268B (en) * | 2018-11-15 | 2019-12-06 | 中国科学院山西煤炭化学研究所 | Method and device for preparing gasoline and aromatic hydrocarbon from Fischer-Tropsch synthesis tail gas |
| CN111394120B (en) * | 2019-09-18 | 2022-02-22 | 中国石化工程建设有限公司 | Light hydrocarbon recovery method and device |
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