CN109111336A - A kind of expense drags synthesis tail gas deep cooling recyclable device and technique - Google Patents
A kind of expense drags synthesis tail gas deep cooling recyclable device and technique Download PDFInfo
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- CN109111336A CN109111336A CN201811140277.9A CN201811140277A CN109111336A CN 109111336 A CN109111336 A CN 109111336A CN 201811140277 A CN201811140277 A CN 201811140277A CN 109111336 A CN109111336 A CN 109111336A
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- 230000015572 biosynthetic process Effects 0.000 title claims abstract description 72
- 238000003786 synthesis reaction Methods 0.000 title claims abstract description 72
- 238000001816 cooling Methods 0.000 title claims abstract description 54
- 238000000034 method Methods 0.000 title claims abstract description 15
- 239000007789 gas Substances 0.000 claims abstract description 181
- 239000000463 material Substances 0.000 claims abstract description 115
- 229910052799 carbon Inorganic materials 0.000 claims abstract description 69
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims abstract description 69
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims abstract description 67
- 229910002091 carbon monoxide Inorganic materials 0.000 claims abstract description 29
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 28
- 239000001257 hydrogen Substances 0.000 claims abstract description 27
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 27
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 25
- 238000000746 purification Methods 0.000 claims abstract description 20
- 238000011084 recovery Methods 0.000 claims abstract description 16
- 238000005057 refrigeration Methods 0.000 claims abstract description 15
- 238000009833 condensation Methods 0.000 claims abstract description 11
- 230000005494 condensation Effects 0.000 claims abstract description 11
- 229930195733 hydrocarbon Natural products 0.000 claims abstract description 8
- 150000002430 hydrocarbons Chemical class 0.000 claims abstract description 8
- 229920000642 polymer Polymers 0.000 claims abstract description 8
- -1 ethylene, propylene Chemical group 0.000 claims abstract description 7
- 238000004064 recycling Methods 0.000 claims abstract description 7
- 238000011144 upstream manufacturing Methods 0.000 claims abstract description 4
- 239000007792 gaseous phase Substances 0.000 claims description 58
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 claims description 55
- 239000005977 Ethylene Substances 0.000 claims description 55
- 239000007788 liquid Substances 0.000 claims description 52
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 claims description 32
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 claims description 32
- 239000007791 liquid phase Substances 0.000 claims description 30
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 24
- 238000002156 mixing Methods 0.000 claims description 24
- 238000000926 separation method Methods 0.000 claims description 22
- 150000001336 alkenes Chemical class 0.000 claims description 21
- 239000003949 liquefied natural gas Substances 0.000 claims description 14
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 14
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 claims description 13
- 229910052757 nitrogen Inorganic materials 0.000 claims description 12
- 239000012071 phase Substances 0.000 claims description 11
- 206010019133 Hangover Diseases 0.000 claims description 10
- 239000002737 fuel gas Substances 0.000 claims description 10
- 239000002253 acid Substances 0.000 claims description 9
- 238000010992 reflux Methods 0.000 claims description 9
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims description 7
- 238000001035 drying Methods 0.000 claims description 7
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 claims description 6
- 238000010276 construction Methods 0.000 claims description 6
- 239000011344 liquid material Substances 0.000 claims description 6
- 150000002431 hydrogen Chemical class 0.000 claims description 5
- 230000006835 compression Effects 0.000 claims description 4
- 238000007906 compression Methods 0.000 claims description 4
- 235000019628 coolness Nutrition 0.000 claims description 4
- 150000001993 dienes Chemical class 0.000 claims description 4
- PVXVWWANJIWJOO-UHFFFAOYSA-N 1-(1,3-benzodioxol-5-yl)-N-ethylpropan-2-amine Chemical compound CCNC(C)CC1=CC=C2OCOC2=C1 PVXVWWANJIWJOO-UHFFFAOYSA-N 0.000 claims description 3
- CYNYIHKIEHGYOZ-UHFFFAOYSA-N 1-bromopropane Chemical compound CCCBr CYNYIHKIEHGYOZ-UHFFFAOYSA-N 0.000 claims description 3
- QMMZSJPSPRTHGB-UHFFFAOYSA-N MDEA Natural products CC(C)CCCCC=CCC=CC(O)=O QMMZSJPSPRTHGB-UHFFFAOYSA-N 0.000 claims description 3
- 238000010521 absorption reaction Methods 0.000 claims description 3
- 239000003463 adsorbent Substances 0.000 claims description 3
- 150000001335 aliphatic alkanes Chemical class 0.000 claims description 3
- 229910002092 carbon dioxide Inorganic materials 0.000 claims description 3
- 239000001569 carbon dioxide Substances 0.000 claims description 3
- 238000004939 coking Methods 0.000 claims description 3
- 238000004821 distillation Methods 0.000 claims description 3
- 230000013011 mating Effects 0.000 claims description 3
- 239000002808 molecular sieve Substances 0.000 claims description 3
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 claims description 3
- 238000006116 polymerization reaction Methods 0.000 claims description 3
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 claims description 3
- 238000001179 sorption measurement Methods 0.000 claims description 3
- 229960004424 carbon dioxide Drugs 0.000 claims 2
- 239000004215 Carbon black (E152) Substances 0.000 claims 1
- DGAQECJNVWCQMB-PUAWFVPOSA-M Ilexoside XXIX Chemical compound C[C@@H]1CC[C@@]2(CC[C@@]3(C(=CC[C@H]4[C@]3(CC[C@@H]5[C@@]4(CC[C@@H](C5(C)C)OS(=O)(=O)[O-])C)C)[C@@H]2[C@]1(C)O)C)C(=O)O[C@H]6[C@@H]([C@H]([C@@H]([C@H](O6)CO)O)O)O.[Na+] DGAQECJNVWCQMB-PUAWFVPOSA-M 0.000 claims 1
- 229910002090 carbon oxide Inorganic materials 0.000 claims 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-M hydroxide Chemical compound [OH-] XLYOFNOQVPJJNP-UHFFFAOYSA-M 0.000 claims 1
- 229910052708 sodium Inorganic materials 0.000 claims 1
- 239000011734 sodium Substances 0.000 claims 1
- 238000005406 washing Methods 0.000 claims 1
- 238000006243 chemical reaction Methods 0.000 abstract description 3
- WWYNJERNGUHSAO-XUDSTZEESA-N (+)-Norgestrel Chemical group O=C1CC[C@@H]2[C@H]3CC[C@](CC)([C@](CC4)(O)C#C)[C@@H]4[C@@H]3CCC2=C1 WWYNJERNGUHSAO-XUDSTZEESA-N 0.000 description 11
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 6
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 description 4
- 238000005516 engineering process Methods 0.000 description 4
- HSFWRNGVRCDJHI-UHFFFAOYSA-N alpha-acetylene Natural products C#C HSFWRNGVRCDJHI-UHFFFAOYSA-N 0.000 description 3
- 125000002534 ethynyl group Chemical group [H]C#C* 0.000 description 3
- 239000003054 catalyst Substances 0.000 description 2
- 239000003245 coal Substances 0.000 description 2
- 238000004581 coalescence Methods 0.000 description 2
- 238000005336 cracking Methods 0.000 description 2
- 239000000446 fuel Substances 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 239000001294 propane Substances 0.000 description 2
- 150000001345 alkine derivatives Chemical class 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000005984 hydrogenation reaction Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
Classifications
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C7/00—Purification; Separation; Use of additives
- C07C7/005—Processes comprising at least two steps in series
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C7/00—Purification; Separation; Use of additives
- C07C7/04—Purification; Separation; Use of additives by distillation
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
- C10L3/12—Liquefied petroleum gas
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- Analytical Chemistry (AREA)
- Water Supply & Treatment (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Separation By Low-Temperature Treatments (AREA)
Abstract
A kind of expense drags synthesis tail gas deep cooling recyclable device and technique.The invention discloses a kind of expenses to drag synthetic oil tail gas cryogenic recovery process, it is that expense drags synthetic oil at normal temperature cannot the higher hydro carbons of value such as the carbon two of liquefied light component material and its entrainment, carbon three, carbon four that expense, which drags synthesis tail gas, this technique is exactly to utilize azeotrope refrigeration system, expense after purification is dragged into synthesis tail gas cooling liquefaction, carbon two, carbon three and heavier component are recycled, then carbon two, three rectifying of carbon are obtained polymer grade ethylene, propylene respectively；LNG product is made in methane condensation liquefaction in tail gas；Hydrogen and carbon monoxide are sent to expense according to the composition and ratio of synthesis gas and drag synthesis reactor upstream by purifying hydrogen of hydrogen and carbon monoxide.This Fischer-Tropsch synthesis oil tail gas cryogenic recovery process not only recycles the economic values higher composition such as ethylene, propylene, and also recycling expense drags the unstripped gas hydrogen and carbon monoxide of synthetic reaction, and LNG or CNG is made in methane therein.Additionally provide it is a kind of expense drag synthetic oil tail gas cryogenic recyclable device.
Description
Technical field
The invention belongs to the expenses of coal chemical industry to drag synthesis field, and specifically a kind of expense drags synthesis tail gas deep cooling recyclable device
And technique.
Background technique
F- T synthesis is one of technology of ICL for Indirect Coal Liquefaction, be synthesis gas under certain temperature and pressure, using appropriate
Catalyst so that carbon monoxide is reacted the technical process for generating liquid fuel based on direct-connected hydro carbons with hydrogen；Synthesis is dragged in expense
In the production process of oil, the low-carbons hydro carbons such as methane, ethylene, ethane, propylene, propane and carbon four can be also generated, some does not have
There are the hydrogen and carbon monoxide component for participating in reacting.
Synthetic oil tail gas be exactly under the temperature and pressure of normal operating can not liquefied " fixed gas " and its entrainment compared with
Heavy hydrocarbons, the economic values higher composition such as ethylene, propylene for dragging synthesis and production process to generate compared with early expense is seldom, this strand of tail gas is just made
It is sent into fuel gas system for fuel, the unstripped gas of reaction is dragged including largely taking --- carbon monoxide and hydrogen.
With the raising of catalyst technology and the improvement of process conditions, the low-carbon alkene content in Fischer-Tropsch synthesis oil tail gas is not
It is disconnected to increase, it is imperative to recycle economic value higher composition in Fischer-Tropsch synthesis oil tail gas.In addition, utilizing the work of synthesis gas alkene
Make progress also in full preparation, and constantly have good news outflow, this Fischer-Tropsch synthesis oil tail gas cryogenic recovery process is equally suitable
Close the product gas deep cooling recycling of synthesis gas alkene.
Summary of the invention
Technical problem to be solved by the invention is to provide a kind of expenses to drag synthesis tail gas deep cooling recyclable device and technique, with solution
Defect certainly existing in the prior art.
The technical scheme to solve the above technical problems is that
A kind of expense drags synthesis tail gas deep cooling recyclable device, including gas inlet and the oxygen being sequentially communicated with the gas inlet
Compound and acid gas removal system, drying system and high pressure depropanizer, the high pressure depropanizer include two-way pipeline, and one
Road pipeline is used for conveying high-pressure depropanizing tower kettle material, is connected to low pressure depropanizer；Another way pipeline is for conveying height
The gas phase of pressure-off propane column overhead, is connected to compressor；The compressor is connected to No. 1 cryogenic separator, No. 1 deep cooling
Condensate liquid is sent into pre- domethanizing column to separator by pipeline all the way, and low-temperature gaseous phase is sent into No. 2 cryogenic separators by another way pipeline；Institute
Pre- domethanizing column is stated by low temperature liquid phase feed separation into top gaseous phase material and tower bottom liquid phase material, pipeline is by gaseous phase materials all the way
It is sent into domethanizing column, controls propylene, materials at bottom of tower is sent into dethanizer by another way pipeline, and No. 2 cryogenic separators are all the way
Pipeline send condensate liquid to domethanizing column, and low-temperature gaseous phase material is entered No. 3 cryogenic separators by another way pipeline；No. 3 depths
Pipeline is by cryogenic liquid material feeding liquefied natural gas system all the way for cold separator, and pipeline is by low-temperature gaseous phase material through multistage all the way
Ice chest heat exchanger rewarming is sent into PSA unit；The domethanizing column is connected to pre- domethanizing column, No. 2 cryogenic separators respectively, described
Demethanizer column overhead generates low-temperature gaseous phase methane material, and tower bottom generates tower bottom low temperature methane material, and kettle material is sent into ethylene essence
Evaporate tower；The ethylene rectifying column is also connected to dethanizer, feeds two material of mixing carbon from domethanizing column tower reactor and de- second
Two material of mixing carbon of alkane column overhead, tower top control ethane content, output polymer grade ethylene, and tower bottom controls ethylene contents, output
Ethane product.
Further, pipeline is connect the low pressure depropanizer with debutanizing tower all the way, and the debutanizing tower receives low pressure
Depropanizing tower kettle material；The another way pipeline of pipeline and low pressure depropanizer is connected to propylene essence to the dethanizer all the way
Evaporate tower；The liquefied natural gas system connection carbon monoxide purification system is purified；
A kind of expense drags synthesis tail gas deep cooling recovery process, includes the following steps:
1) expense with certain pressure (1.0-2.5MPa) and temperature (30-40 DEG C) sent from upstream device drags synthesis tail
Gas enters oxide and acid gas removal system, removes oxide and carbon dioxide in tail gas；
2) Fischer-Tropsch process exhaust for removing sour gas is cooled to 12-15 DEG C and enters drying system, removed in tail gas
Moisture；
3) dry qualified expense hangover gas enters high pressure depropanizer, and tower top controls carbon four, and tower bottom controls ethylene；
4) high pressure depropanizer kettle material enters low pressure depropanizer, and tower top controls carbon four, and tower bottom controls propylene, tower pressure
Control is in 0.6, -0.8MPa, and 10-16 DEG C of tower top temperature；5) low pressure depropanizer tower top mixing carbon three is pumped up into propylene rectifying
Tower；
6) low pressure depropanizer kettle material is sent into debutanizing tower, and tower top controls light dydrocarbon content, and tower reactor controls four content of carbon,
The voltage-controlled 0.3-0.4MPA processed of tower, four product of tower top carbon are pumped up out, and tower reactor light dydrocarbon product is sent out through pump cooling；
7) high pressure depropanizer top gaseous phase boosts to 3.0-3.5MPa through compressor；
8) enter No. 1 cryogenic separator, pressure 3.0- after the carbon three of compression boosting and light-component gas are cooled down step by step
3.5MPa, temperature are down to -65--50 DEG C；Condensate liquid is sent into pre- domethanizing column, and low-temperature gaseous phase is sent into No. 2 cryogenic separators；
9) it continues to cool down into the low-temperature gaseous phase material of No. 2 cryogenic separators, pressure controls 3.0-3.5MPa, temperature drop
To -130--80 DEG C；Condensate liquid is sent to domethanizing column, and low-temperature gaseous phase material enters No. 3 cryogenic separators；
10) it continues to cool down into the low-temperature gaseous phase material of No. 3 cryogenic separators, pressure controls 3.0-3.5MPa, temperature
It is down to -180--150 DEG C；Cryogenic liquid material is sent into LNG unit, and low-temperature gaseous phase material is sent into through multistage ice chest heat exchanger rewarming
PSA unit；
11) into the gaseous phase materials of PSA unit through pressure-variable adsorption output purity higher hydrogen gas product and resolution gas, resolution gas
Boosting enters fuel gas pipe network；
12) the low temperature liquid phase material for being sent into LNG unit arrives LNG product and carbon monoxide tail gas, carbon monoxide through what is refined
Tail gas obtains the carbon monoxide product and combustible exhaust gas of higher degree through purification purification, and combustible exhaust gas is sent into fuel gas pipe network；
13) top gaseous phase material and tower bottom liquid phase material, gas are separated into the low temperature liquid phase material of pre- domethanizing column
Phase materials are sent into domethanizing column, control propylene, and materials at bottom of tower is sent into dethanizer, control methane, tower top pressure 3.0-
3.5MPa, -55--40 DEG C；
14) charging of domethanizing column is taken off from No. 2 cryogenic separator condensate liquids and pre- domethanizing column carbon two and light component
Methane column overhead generates low-temperature gaseous phase methane material, controls ethylene contents, and tower bottom liquid phase material controls methane, tower top pressure 2.9-
3.3MPa, -100--95 DEG C of temperature, tower bottom low temperature methane material enters expanding machine and provides cooling capacity for ice chest, and kettle material is sent into second
Alkene rectifying column；
15) deethanizer overhead pressure is 2.0-2.8MPA, and temperature is -24--14 DEG C, and tower top controls propylene content, tower bottom
Ethylene contents are controlled, two material of mixing carbon of tower top is sent into ethylene rectifying column, and the mixing carbon three of tower reactor is sent into propylene rectification tower；
16) mixing of mixing carbon two material and deethanizer overhead of the charging of ethylene rectifying column from domethanizing column tower reactor
Two material of carbon, tower top control ethane content, output polymer grade ethylene, and tower bottom controls ethylene contents, output ethane product, tower top pressure
Power 0.5-1.0MPA, -40--70 DEG C of temperature；
17) mixing carbon 3 material of the charging of propylene rectification tower from dethanizer tower reactor, tower top operating pressure 1.6-
1.9MPA, 36-49 DEG C of temperature, tower top output polymerization-grade propylene product, tower bottom output bromopropane product；
Further, expense drags the component of synthesis tail gas, the component of pressure and synthesis gas olefin product gas, pressure close；
Further, it includes that azeotrope refrigeration and nitrogen follow that expense, which drags refrigeration system used by tail gas cryogenic recovery process,
Ring refrigeration, can also be using propylene, ethylene cascade refrigeration and nitrogen circulation refrigeration；
Further, in step 1), expense drags synthesis tail gas to select different acidity according to the content and type of sour gas
Gas removal method, such as washed with MDEA, sodium hydroxide solution and adsorbent of molecular sieve selective absorption；
Further, in step 2), take hangover air cooling to entering knockout drum, tank deck gaseous phase materials after 12-15 DEG C
Into gas phase drier, free water is discharged by Interface Control in tank bottom liquid phase material, and the above liquid phase hydro carbons in interface is by being pumped into coalescence
Device further removes free water, subsequently into liquid phase drier；
Further, step 3), 4) in, due to expense drag synthesis tail gas diene content few, there is no polymerization cokings to ask
Topic, can use single column depropanization；Tower pressure is 1.3-1.9MPA, and -23--15 DEG C of temperature, tower top controls carbon four, and tower bottom controls carbon
Three；Depropanizing tower kettle material enters debutanizing tower；
Further, step 3), 7) in, the carbon three of high pressure depropanizer tower top and light component enter expense hangover gas through rewarming
Compressor boosts to 3.0-3.5MPA；
Further, the reflux of step 3) high pressure depropanizer comes from No. 1 cryogenic separator, pressure 3.0-3.5MPA, temperature
- 40 to -30 DEG C of degree；
Further, in step 8), No. 1 cryogenic separator can condense different temperatures in -65--20 DEG C of temperature range
The condensate liquid of different component, respectively high pressure depropanizer provide the charging of phegma and pre- domethanizing column different location；
Further, in step 9), No. 2 cryogenic separators are different in -130--80 DEG C of temperature range condensation different temperatures
The condensate liquid of component is respectively corresponded into domethanizing column different location；
Further, step 8), 9) in, together with conventional ethylene cracker design and construction expense drag tail gas cryogenic to recycle
The condensate liquid of the different temperatures different component of No. 1 cryogenic separator can be sent into conventional ethylene cracker alkene point by device
The condensate liquid of the different temperatures different component of No. 2 cryogenic separators is sent into conventional ethylene cracking by the pre- domethanizing column from unit
The domethanizing column of device separation of olefins unit, in this way expense drag tail gas cryogenic recyclable device just do not have to the pre- domethanizing column of design-build,
Domethanizing column, dethanizer and the ethylene rectifying column in downstream and propylene rectification tower；
Further, in step 8), No. 1 cryogenic separator includes ice chest heat exchanger, gas-liquid separation equipment, in cryogenic gas
Tower or fractional condensation separator are used before leaving No. 1 cryogenic separator, so that the carbon three in low-temperature gaseous phase is dropped at the maximum temperature
To minimum, the reflux of tower is the lower condensate liquid of the lighter temperature of component that overhead condenser provides, and is also possible to from No. 2 deep coolings
The lower condensate liquid of the lighter temperature of the component of separator；
Further, in step 9), No. 2 cryogenic separators equally include ice chest heat exchanger, gas-liquid separation equipment, in low temperature
Gas uses tower or fractional condensation separator before leaving No. 2 cryogenic separators, so as at the maximum temperature the carbon in low-temperature gaseous phase
Two are preferably minimized, and the reflux of tower is the lower condensate liquid of the lighter temperature of component that overhead condenser provides, and are also possible to from No. 3
The lower condensate liquid of the lighter temperature of the component of cryogenic separator；
Further, in step 10), No. 3 cryogenic separators include ice chest heat exchanger and fractionating column, by azeotrope and liquid
Nitrogen provides cooling capacity, and setting fractionating column is mentioned the purpose is to reduce methane, the content of carbon monoxide and reduction liquid phase hydrogen content in hydrogen
The rate of recovery of high hydrogen, methane and carbon monoxide；
Further, in step 10), the cryogenic gas that No. 3 cryogenic separators generate meets after rewarming into synthesis gas
The condition of pipe network can be sent directly into synthesis gas pipe network, can also enter PSA hydrogen making product, not allow access into syngas tube
Net enters PSA unit hydrogen making；
Further, step 10), 11) in, hydrogen product can according to need be sent into synthesis gas pipe network, resolution gas be sent into
Fuel gas pipe network；
Further, in step 12), LNG unit includes lightness-removing column and CO purification system, and lightness-removing column is by No. 3 cryogenic separations
Device cryogenic liquid is separated into the low temperature richness CO gas of LNG product and tower top, and tower top cryogenic gas is laggard through ice chest re-heat
Enter CO purification system, CO purification system is other PSA device, and rich carbon monoxide gaseous phase materials are separated into higher degree one and are aoxidized
Carbon products and rich nitrogen resolution gas；
Further, in step 14), together with conventional ethylene cracker design and construction expense drag tail gas cryogenic recycling dress
It sets, the demethanizer column overhead low-temperature gaseous phase methane of conventional ethylene cracker separation of olefins unit can be introduced and take hangover gas depth
Cold recovery device expanding machine provides cooling capacity for ice chest；
Further, in step 16), ethylene distillation system using heat pump it is mating, pressure 0.5-1.0MPA, temperature -40 to -
70℃。
The beneficial effects of the present invention are: for expense drag synthesis tail gas the characteristics of, provide it is a kind of expense drag synthetic oil tail gas
Deep cooling deep cooling recovery process and system.Compared with traditional oil product alkene and MTO technology, Fischer-Tropsch synthesis oil
The feature of tail gas maximum is exactly pressure with higher, and therefore, expense drags synthetic oil tail gas not have to increase pressure progress oxide, acid
Property gas and moisture removing, tail gas can only be boosted to simple one section compression before entering cryogenic separation system
Required operating pressure；Expense drags alkynes and the diene content pole synthesized by tail gas compared with traditional oil product cracks alkene processed
Low, expense drags synthetic oil tail gas cryogenic recovery process only with simple one section of acetylene removal protection reactor even without acetylene hydrogenation
Reactor can reach the acetylene index of polymer grade ethylene product requirement；Expense drags synthetic oil tail gas compared with MTO technology
The light components content such as hydrogen, methane is higher, only just can guarantee effective recycling of low-carbon alkene using cryogenic separation.This Fischer-Tropsch closes
The economic values higher composition such as ethylene, propylene is not only recycled at oily tail gas cryogenic recovery process, also recycling expense drags synthetic reaction
Unstripped gas hydrogen and carbon monoxide, and LNG or CNG is made in methane therein.
Detailed description of the invention
Fig. 1 is schematic structural view of the invention；
The reference numerals are as follows:
1, oxide and acid gas removal system, 2, drying system, 3, high pressure depropanizer, 4, low pressure depropanizer,
5, debutanizing tower, 6, propylene rectification tower, 7, compressor, 8, No. 1 cryogenic separators, 9, pre- domethanizing column, 10, No. 2 cryogenic separations
Device, 11, domethanizing column, 12, No. 3 cryogenic separators, 13, liquefied natural gas system, 14, PSA unit, 15, carbon monoxide purification
System, 16, dethanizer, 17, ethylene rectifying column；
Specific embodiment
The principle and features of the present invention will be described below with reference to the accompanying drawings, and the given examples are served only to explain the present invention, and
It is non-to be used to limit the scope of the invention.
As shown in Figure 1, a kind of expense drags synthesis tail gas deep cooling recyclable device, including gas inlet and with the gas inlet according to
The oxide and acid gas removal system, drying system and high pressure depropanizer of secondary connection, the high pressure depropanizer include
Two-way pipeline, pipeline is used for conveying high-pressure depropanizing tower kettle material all the way, is connected to low pressure depropanizer；Another way pipeline
For the gas phase of conveying high-pressure depropanizing tower tower top, it is connected to compressor；The compressor is connected to No. 1 cryogenic separator,
Condensate liquid is sent into pre- domethanizing column to No. 1 cryogenic separator by pipeline all the way, and low-temperature gaseous phase is sent into No. 2 depths by another way pipeline
Cold separator；The pre- domethanizing column at top gaseous phase material and tower bottom liquid phase material, manages low temperature liquid phase feed separation all the way
Gaseous phase materials are sent into domethanizing column by road, control propylene, and materials at bottom of tower is sent into dethanizer, No. 2 depths by another way pipeline
Pipeline send condensate liquid to domethanizing column to cold separator all the way, and low-temperature gaseous phase material is entered No. 3 cryogenic separations by another way pipeline
Device；Cryogenic liquid material is sent into liquefied natural gas system to No. 3 cryogenic separators by pipeline all the way, and pipeline is by low temperature gas all the way
Phase materials are sent into PSA unit through multistage ice chest heat exchanger rewarming；The domethanizing column divides with pre- domethanizing column, No. 2 deep coolings respectively
It is connected to from device, the demethanizer column overhead generates low-temperature gaseous phase methane material, and tower bottom generates tower bottom low temperature methane material, tower reactor object
Material is sent into ethylene rectifying column；The ethylene rectifying column is also connected to dethanizer, feeds the mixing carbon from domethanizing column tower reactor
Two material of mixing carbon of two materials and deethanizer overhead, tower top control ethane content, output polymer grade ethylene, and tower bottom controls second
Alkene content, output ethane product.
More specifically, pipeline is connect the low pressure depropanizer with debutanizing tower all the way, and the debutanizing tower receives low pressure
Depropanizing tower kettle material；The another way pipeline of pipeline and low pressure depropanizer is connected to propylene essence to the dethanizer all the way
Evaporate tower；The liquefied natural gas system connection carbon monoxide purification system is purified；
The present invention also provides a kind of expenses to drag synthesis tail gas deep cooling recovery process, includes the following steps:
1) expense with certain pressure (1.0-2.5MPa) and temperature (30-40 DEG C) sent from upstream device drags synthesis tail
Gas enters oxide and acid gas removal system, removes oxide and carbon dioxide in tail gas；
2) Fischer-Tropsch process exhaust for removing sour gas is cooled to 12-15 DEG C and enters drying system, removed in tail gas
Moisture；
3) dry qualified expense hangover gas enters high pressure depropanizer, and tower top controls carbon four, and tower bottom controls ethylene；
4) high pressure depropanizer kettle material enters low pressure depropanizer, and tower top controls carbon four, and tower bottom controls propylene, tower pressure
Control is in 0.6, -0.8MPa, and 10-16 DEG C of tower top temperature；5) low pressure depropanizer tower top mixing carbon three is pumped up into propylene rectifying
Tower；
6) low pressure depropanizer kettle material is sent into debutanizing tower, and tower top controls light dydrocarbon content, and tower reactor controls four content of carbon,
The voltage-controlled 0.3-0.4MPA processed of tower, four product of tower top carbon are pumped up out, and tower reactor light dydrocarbon product is sent out through pump cooling；
7) high pressure depropanizer top gaseous phase boosts to 3.0-3.5MPa through compressor；
8) enter No. 1 cryogenic separator, pressure 3.0- after the carbon three of compression boosting and light-component gas are cooled down step by step
3.5MPa, temperature are down to -65--50 DEG C；Condensate liquid is sent into pre- domethanizing column, and low-temperature gaseous phase is sent into No. 2 cryogenic separators；
9) it continues to cool down into the low-temperature gaseous phase material of No. 2 cryogenic separators, pressure controls 3.0-3.5MPa, temperature drop
To -130--80 DEG C；Condensate liquid is sent to domethanizing column, and low-temperature gaseous phase material enters No. 3 cryogenic separators；
10) it continues to cool down into the low-temperature gaseous phase material of No. 3 cryogenic separators, pressure controls 3.0-3.5MPa, temperature
It is down to -180--150 DEG C；Cryogenic liquid material is sent into LNG unit, and low-temperature gaseous phase material is sent into through multistage ice chest heat exchanger rewarming
PSA unit；
11) into the gaseous phase materials of PSA unit through pressure-variable adsorption output purity higher hydrogen gas product and resolution gas, resolution gas
Boosting enters fuel gas pipe network；
12) the low temperature liquid phase material for being sent into LNG unit arrives LNG product and carbon monoxide tail gas, carbon monoxide through what is refined
Tail gas obtains the carbon monoxide product and combustible exhaust gas of higher degree through purification purification, and combustible exhaust gas is sent into fuel gas pipe network；
13) top gaseous phase material and tower bottom liquid phase material, gas are separated into the low temperature liquid phase material of pre- domethanizing column
Phase materials are sent into domethanizing column, control propylene, and materials at bottom of tower is sent into dethanizer, control methane, tower top pressure 3.0-
3.5MPa, -55--40 DEG C；
14) charging of domethanizing column is taken off from No. 2 cryogenic separator condensate liquids and pre- domethanizing column carbon two and light component
Methane column overhead generates low-temperature gaseous phase methane material, controls ethylene contents, and tower bottom liquid phase material controls methane, tower top pressure 2.9-
3.3MPa, -100--95 DEG C of temperature, tower bottom low temperature methane material enters expanding machine and provides cooling capacity for ice chest, and kettle material is sent into second
Alkene rectifying column；
15) deethanizer overhead pressure is 2.0-2.8MPA, and temperature is -24--14 DEG C, and tower top controls propylene content, tower bottom
Ethylene contents are controlled, two material of mixing carbon of tower top is sent into ethylene rectifying column, and the mixing carbon three of tower reactor is sent into propylene rectification tower；
16) mixing of mixing carbon two material and deethanizer overhead of the charging of ethylene rectifying column from domethanizing column tower reactor
Two material of carbon, tower top control ethane content, output polymer grade ethylene, and tower bottom controls ethylene contents, output ethane product, tower top pressure
Power 0.5-1.0MPA, -40--70 DEG C of temperature；
17) mixing carbon 3 material of the charging of propylene rectification tower from dethanizer tower reactor, tower top operating pressure 1.6-
1.9MPA, 36-49 DEG C of temperature, tower top output polymerization-grade propylene product, tower bottom output bromopropane product；
Further, expense drags the component of synthesis tail gas, the component of pressure and synthesis gas olefin product gas, pressure close；
Further, it includes that azeotrope refrigeration and nitrogen follow that expense, which drags refrigeration system used by tail gas cryogenic recovery process,
Ring refrigeration, can also be using propylene, ethylene cascade refrigeration and nitrogen circulation refrigeration；
Further, in step 1), expense drags synthesis tail gas to select different acidity according to the content and type of sour gas
Gas removal method, such as washed with MDEA, sodium hydroxide solution and adsorbent of molecular sieve selective absorption；
Further, in step 2), take hangover air cooling to entering knockout drum, tank deck gaseous phase materials after 12-15 DEG C
Into gas phase drier, free water is discharged by Interface Control in tank bottom liquid phase material, and the above liquid phase hydro carbons in interface is by being pumped into coalescence
Device further removes free water, subsequently into liquid phase drier；
Further, step 3), 4) in, due to expense drag synthesis tail gas diene content few, there is no polymerization cokings to ask
Topic, can use single column depropanization；Tower pressure is 1.3-1.9MPA, and -23--15 DEG C of temperature, tower top controls carbon four, and tower bottom controls carbon
Three；Depropanizing tower kettle material enters debutanizing tower；
Further, step 3), 7) in, the carbon three of high pressure depropanizer tower top and light component enter expense hangover gas through rewarming
Compressor boosts to 3.0-3.5MPA；
Further, the reflux of step 3) high pressure depropanizer comes from No. 1 cryogenic separator, pressure 3.0-3.5MPA, temperature
- 40 to -30 DEG C of degree；
Further, in step 8), No. 1 cryogenic separator can condense different temperatures in -65--20 DEG C of temperature range
The condensate liquid of different component, respectively high pressure depropanizer provide the charging of phegma and pre- domethanizing column different location；
Further, in step 9), No. 2 cryogenic separators are different in -130--80 DEG C of temperature range condensation different temperatures
The condensate liquid of component is respectively corresponded into domethanizing column different location；
Further, step 8), 9) in, together with conventional ethylene cracker design and construction expense drag tail gas cryogenic to recycle
The condensate liquid of the different temperatures different component of No. 1 cryogenic separator can be sent into conventional ethylene cracker alkene point by device
The condensate liquid of the different temperatures different component of No. 2 cryogenic separators is sent into conventional ethylene cracking by the pre- domethanizing column from unit
The domethanizing column of device separation of olefins unit, in this way expense drag tail gas cryogenic recyclable device just do not have to the pre- domethanizing column of design-build,
Domethanizing column, dethanizer and the ethylene rectifying column in downstream and propylene rectification tower；
Further, in step 8), No. 1 cryogenic separator includes ice chest heat exchanger, gas-liquid separation equipment, in cryogenic gas
Tower or fractional condensation separator are used before leaving No. 1 cryogenic separator, so that the carbon three in low-temperature gaseous phase is dropped at the maximum temperature
To minimum, the reflux of tower is the lower condensate liquid of the lighter temperature of component that overhead condenser provides, and is also possible to from No. 2 deep coolings
The lower condensate liquid of the lighter temperature of the component of separator；
Further, in step 9), No. 2 cryogenic separators equally include ice chest heat exchanger, gas-liquid separation equipment, in low temperature
Gas uses tower or fractional condensation separator before leaving No. 2 cryogenic separators, so as at the maximum temperature the carbon in low-temperature gaseous phase
Two are preferably minimized, and the reflux of tower is the lower condensate liquid of the lighter temperature of component that overhead condenser provides, and are also possible to from No. 3
The lower condensate liquid of the lighter temperature of the component of cryogenic separator；
Further, in step 10), No. 3 cryogenic separators include ice chest heat exchanger and fractionating column, by azeotrope and liquid
Nitrogen provides cooling capacity, and setting fractionating column is mentioned the purpose is to reduce methane, the content of carbon monoxide and reduction liquid phase hydrogen content in hydrogen
The rate of recovery of high hydrogen, methane and carbon monoxide；
Further, in step 10), the cryogenic gas that No. 3 cryogenic separators generate meets after rewarming into synthesis gas
The condition of pipe network can be sent directly into synthesis gas pipe network, can also enter PSA hydrogen making product, not allow access into syngas tube
Net enters PSA unit hydrogen making；
Further, further, step 10), 11) in, hydrogen product can according to need be sent into synthesis gas pipe network, solution
Gassing is sent into fuel gas pipe network；
Further, in step 12), LNG unit includes lightness-removing column and CO purification system, and lightness-removing column is by No. 3 cryogenic separations
Device cryogenic liquid is separated into the low temperature richness CO gas of LNG product and tower top, and tower top cryogenic gas is laggard through ice chest re-heat
Enter CO purification system, CO purification system is other PSA device, and rich carbon monoxide gaseous phase materials are separated into higher degree one and are aoxidized
Carbon products and rich nitrogen resolution gas；
Further, in step 14), together with conventional ethylene cracker design and construction expense drag tail gas cryogenic recycling dress
It sets, the demethanizer column overhead low-temperature gaseous phase methane of conventional ethylene cracker separation of olefins unit can be introduced and take hangover gas depth
Cold recovery device expanding machine provides cooling capacity for ice chest；
Further, in step 16), ethylene distillation system using heat pump it is mating, pressure 0.5-1.0MPA, temperature -40 to -
70℃.The foregoing is merely presently preferred embodiments of the present invention, is not intended to limit the invention, all in the spirit and principles in the present invention
Within, any modification, equivalent replacement, improvement and so on should all be included in the protection scope of the present invention.
Claims (21)
1. a kind of expense drags synthesis tail gas deep cooling recyclable device, it is characterised in that: including gas inlet and with the gas inlet according to
The oxide and acid gas removal system, drying system and high pressure depropanizer of secondary connection, the high pressure depropanizer include
Two-way pipeline, pipeline is used for conveying high-pressure depropanizing tower kettle material all the way, is connected to low pressure depropanizer；Another way pipeline
For the gas phase of conveying high-pressure depropanizing tower tower top, it is connected to compressor；The compressor is connected to No. 1 cryogenic separator,
Condensate liquid is sent into pre- domethanizing column to No. 1 cryogenic separator by pipeline all the way, and low-temperature gaseous phase is sent into No. 2 depths by another way pipeline
Cold separator；The pre- domethanizing column at top gaseous phase material and tower bottom liquid phase material, manages low temperature liquid phase feed separation all the way
Gaseous phase materials are sent into domethanizing column by road, control propylene, and materials at bottom of tower is sent into dethanizer, No. 2 depths by another way pipeline
Pipeline send condensate liquid to domethanizing column to cold separator all the way, and low-temperature gaseous phase material is entered No. 3 cryogenic separations by another way pipeline
Device；Cryogenic liquid material is sent into liquefied natural gas system to No. 3 cryogenic separators by pipeline all the way, and pipeline is by low temperature gas all the way
Phase materials are sent into PSA unit through multistage ice chest heat exchanger rewarming；The domethanizing column divides with pre- domethanizing column, No. 2 deep coolings respectively
It is connected to from device, the demethanizer column overhead generates low-temperature gaseous phase methane material, and tower bottom generates tower bottom low temperature methane material, tower reactor object
Material is sent into ethylene rectifying column；The ethylene rectifying column is also connected to dethanizer, feeds the mixing carbon from domethanizing column tower reactor
Two material of mixing carbon of two materials and deethanizer overhead, tower top control ethane content, output polymer grade ethylene, and tower bottom controls second
Alkene content, output ethane product.
2. a kind of expense according to claim 1 drags synthesis tail gas deep cooling recyclable device, it is characterised in that: the low pressure de- third
Pipeline is connect alkane tower with debutanizing tower all the way, and the debutanizing tower receives low pressure depropanizer kettle material；The dethanizer
The another way pipeline of pipeline and low pressure depropanizer is connected to propylene rectification tower all the way；The liquefied natural gas system connection one
Carbonoxide purification system is purified.
3. a kind of expense drags synthesis tail gas deep cooling recovery process, which comprises the steps of:
1) expense with certain pressure (1.0-2.5MPa) and temperature (30-40 DEG C) sent from upstream device drag synthesis tail gas into
Enter oxide and acid gas removal system, removes oxide and carbon dioxide in tail gas；
2) Fischer-Tropsch process exhaust for removing sour gas is cooled to 12-15 DEG C and enters drying system, remove the moisture in tail gas；
3) dry qualified expense hangover gas enters high pressure depropanizer, and tower top controls carbon four, and tower bottom controls ethylene；
4) high pressure depropanizer kettle material enters low pressure depropanizer, and tower top controls carbon four, and tower bottom controls propylene, the voltage-controlled system of tower
In 0.6, -0.8MPa, 10-16 DEG C of tower top temperature；5) low pressure depropanizer tower top mixing carbon three is pumped up into propylene rectification tower；
6) low pressure depropanizer kettle material is sent into debutanizing tower, and tower top controls light dydrocarbon content, and tower reactor controls four content of carbon, tower pressure
0.3-0.4MPA is controlled, four product of tower top carbon is pumped up out, and tower reactor light dydrocarbon product is sent out through pump cooling；
7) high pressure depropanizer top gaseous phase boosts to 3.0-3.5MPa through compressor；
8) enter No. 1 cryogenic separator, pressure 3.0- after the carbon three of compression boosting and light-component gas are cooled down step by step
3.5MPa, temperature are down to -65--50 DEG C；Condensate liquid is sent into pre- domethanizing column, and low-temperature gaseous phase is sent into No. 2 cryogenic separators；
9) it continuing to cool down into the low-temperature gaseous phase materials of No. 2 cryogenic separators, pressure controls 3.0-3.5MPa, and temperature is down to-
130--80℃；Condensate liquid is sent to domethanizing column, and low-temperature gaseous phase material enters No. 3 cryogenic separators；
10) it continuing to cool down into the low-temperature gaseous phase materials of No. 3 cryogenic separators, pressure controls 3.0-3.5MPa, and temperature is down to-
180--150℃；Cryogenic liquid material is sent into LNG unit, and low-temperature gaseous phase material is mono- through multistage ice chest heat exchanger rewarming feeding PSA
Member；
11) into the gaseous phase materials of PSA unit through pressure-variable adsorption output purity higher hydrogen gas product and resolution gas, resolution gas boosting
Into fuel gas pipe network；
12) the low temperature liquid phase material for being sent into LNG unit arrives LNG product and carbon monoxide tail gas, carbon monoxide tail gas through what is refined
The carbon monoxide product and combustible exhaust gas of higher degree are obtained through purification purification, combustible exhaust gas is sent into fuel gas pipe network；
13) top gaseous phase material and tower bottom liquid phase material, gas gas-phase objects are separated into the low temperature liquid phase material of pre- domethanizing column
Material feeding domethanizing column, control propylene, materials at bottom of tower feeding dethanizer, control methane, tower top pressure 3.0-3.5MPa ,-
55--40℃；
14) charging of domethanizing column is from No. 2 cryogenic separator condensate liquids and pre- domethanizing column carbon two and light component, demethanation
Column overhead generates low-temperature gaseous phase methane material, controls ethylene contents, and tower bottom liquid phase material controls methane, tower top pressure 2.9-
3.3MPa, -100--95 DEG C of temperature, tower bottom low temperature methane material enters expanding machine and provides cooling capacity for ice chest, and kettle material is sent into second
Alkene rectifying column；
15) deethanizer overhead pressure is 2.0-2.8MPA, and temperature is -24--14 DEG C, and tower top controls propylene content, tower bottom control
Ethylene contents, two material of mixing carbon of tower top are sent into ethylene rectifying column, and the mixing carbon three of tower reactor is sent into propylene rectification tower；
16) the mixing carbon two of mixing carbon two material and deethanizer overhead of the charging of ethylene rectifying column from domethanizing column tower reactor
Material, tower top control ethane content, output polymer grade ethylene, and tower bottom controls ethylene contents, output ethane product, tower top pressure
0.5-1.0MPA, -40--70 DEG C of temperature；
17) mixing carbon 3 material of the charging of propylene rectification tower from dethanizer tower reactor, tower top operating pressure 1.6-1.9MPA,
36-49 DEG C of temperature, tower top output polymerization-grade propylene product, tower bottom output bromopropane product.
4. a kind of expense according to claim 3 drags synthesis tail gas deep cooling recyclable device, it is characterised in that: expense drags synthesis tail gas
Component, the component of pressure and synthesis gas olefin product gas, pressure it is close.
5. a kind of expense according to claim 3 drags synthesis tail gas deep cooling recyclable device, it is characterised in that: expense drags tail gas cryogenic
Refrigeration system used by recovery process includes azeotrope refrigeration and nitrogen circulation refrigeration, propylene, ethylene can also be used multiple
Fold cold and nitrogen circulation refrigeration.
6. a kind of expense according to claim 3 drags synthesis tail gas deep cooling recyclable device, it is characterised in that: in step 1), take
It drags synthesis tail gas to select different acid gas removal methods according to the content and type of sour gas, such as uses MDEA, hydroxide
The washings such as sodium solution and adsorbent of molecular sieve selective absorption.
7. a kind of expense according to claim 3 drags synthesis tail gas deep cooling recyclable device, it is characterised in that: in step 2), take
For air cooling of trailing to entering knockout drum after 12-15 DEG C, tank deck gaseous phase materials enter gas phase drier, tank bottom liquid phase material by
Free water is discharged in Interface Control, and the above liquid phase hydro carbons in interface further removes free water by being pumped into coalescer, subsequently into liquid
Phase drier.
8. it is according to claim 3 it is a kind of expense drag synthesis tail gas deep cooling recyclable device, it is characterised in that: step 3), 4) in,
Since expense drags synthesis tail gas diene content few, polymerization coking problem is not present, single column depropanization can be used；Tower pressure is
1.3-1.9MPA, -23 to -15 DEG C of temperature, tower top controls carbon four, and tower bottom controls carbon three；Depropanizing tower kettle material enters de- fourth
Alkane tower.
9. it is according to claim 3 it is a kind of expense drag synthesis tail gas deep cooling recyclable device, it is characterised in that: step 3), 7) in,
The carbon three and light component of high pressure depropanizer tower top enter expense hangover air compressor through rewarming and boost to 3.0-3.5MPA.
10. a kind of expense according to claim 3 drags synthesis tail gas deep cooling recyclable device, it is characterised in that: step 3) high pressure
The reflux of depropanizing tower come from No. 1 cryogenic separator, pressure 3.0-3.5MPA, -40 to -30 DEG C of temperature.
11. a kind of expense according to claim 3 drags synthesis tail gas deep cooling recyclable device, it is characterised in that: in step 8), 1
Number cryogenic separator can be in the condensate liquid of -65--20 DEG C of temperature range condensation different temperatures different component, respectively high pressure
Depropanizing tower provides the charging of phegma and pre- domethanizing column different location.
12. a kind of expense according to claim 3 drags synthesis tail gas deep cooling recyclable device, it is characterised in that: in step 9), 2
Number cryogenic separator is respectively corresponded in the condensate liquid of -130--80 DEG C of temperature range condensation different temperatures different component into de-
Methane tower different location.
13. a kind of expense according to claim 3 drags synthesis tail gas deep cooling recyclable device, it is characterised in that: step 8), 9)
In, together with conventional ethylene cracker design and construction expense drag tail gas cryogenic recyclable device, can be No. 1 cryogenic separator
The condensate liquid of different temperatures different component is sent into the pre- domethanizing column of conventional ethylene cracker separation of olefins unit, No. 2 depths
The condensate liquid of the different temperatures different component of cold separator is sent into the domethanizing column of conventional ethylene cracker separation of olefins unit,
Expense drags tail gas cryogenic recyclable device just not have to the pre- domethanizing column of design-build, domethanizing column, dethanizer and downstream in this way
Ethylene rectifying column and propylene rectification tower.
14. a kind of expense according to claim 3 drags synthesis tail gas deep cooling recyclable device, it is characterised in that: in step 8), 1
Number cryogenic separator includes ice chest heat exchanger, gas-liquid separation equipment, and tower is used before cryogenic gas leaves No. 1 cryogenic separator
Or fractional condensation separator, so that the carbon three in low-temperature gaseous phase is preferably minimized at the maximum temperature, the reflux of tower is overhead condenser
The lower condensate liquid of the lighter temperature of the component of offer is also possible to lower from the lighter temperature of the component of No. 2 cryogenic separators
Condensate liquid.
15. a kind of expense according to claim 3 drags synthesis tail gas deep cooling recyclable device, it is characterised in that: in step 9), 2
Number cryogenic separator equally includes ice chest heat exchanger, gas-liquid separation equipment, is adopted before cryogenic gas leaves No. 2 cryogenic separators
With tower or fractional condensation separator, so that the carbon two in low-temperature gaseous phase is preferably minimized at the maximum temperature, the reflux of tower is that tower top is cold
The lower condensate liquid of the lighter temperature of component that condenser provides, is also possible to from the lighter temperature of the component of No. 3 cryogenic separators more
Low condensate liquid.
16. a kind of expense according to claim 3 drags synthesis tail gas deep cooling recyclable device, it is characterised in that: in step 10), 3
The purpose of number cryogenic separator includes ice chest heat exchanger and fractionating column, is provided cooling capacity by azeotrope and liquid nitrogen, fractionating column is arranged be
Methane in hydrogen, the content of carbon monoxide and reduction liquid phase hydrogen content are reduced, the recycling of hydrogen, methane and carbon monoxide is improved
Rate.
17. a kind of expense according to claim 3 drags synthesis tail gas deep cooling recyclable device, it is characterised in that: in step 10), 3
The condition that the cryogenic gas that number cryogenic separator generates meets after rewarming into synthesis gas pipe network can be sent directly into synthesis gas
Pipe network can also enter PSA hydrogen making product, not allow access into synthesis gas pipe network and enter PSA unit hydrogen making.
18. a kind of expense according to claim 3 drags synthesis tail gas deep cooling recyclable device, it is characterised in that: further, step
It is rapid 10), 11) in, hydrogen product can according to need be sent into synthesis gas pipe network, resolution gas be sent into fuel gas pipe network.
19. a kind of expense according to claim 3 drags synthesis tail gas deep cooling recyclable device, it is characterised in that: in step 12),
LNG unit includes lightness-removing column and CO purification system, and No. 3 cryogenic separator cryogenic liquids are separated into LNG product and tower by lightness-removing column
The low temperature richness CO gas on top, tower top cryogenic gas enter CO purification system after ice chest re-heat, and CO purification system is another
Rich carbon monoxide gaseous phase materials are separated into higher degree carbon monoxide product and rich nitrogen resolution gas by outer PSA device.
20. a kind of expense according to claim 3 drags synthesis tail gas deep cooling recyclable device, it is characterised in that: in step 14),
Together with conventional ethylene cracker design and construction expense drag tail gas cryogenic recyclable device, can be by conventional ethylene cracker alkene
The demethanizer column overhead low-temperature gaseous phase methane of hydrocarbon separative unit introduces expense and tail gas cryogenic recyclable device expanding machine is dragged to provide for ice chest
Cooling capacity.
21. a kind of expense according to claim 3 drags synthesis tail gas deep cooling recyclable device, it is characterised in that: in step 16),
Ethylene distillation system is mating using heat pump, pressure 0.5-1.0MPA, and -40 to -70 DEG C of temperature.
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Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
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| CN112361715A (en) * | 2020-10-19 | 2021-02-12 | 中国石油化工股份有限公司 | Cryogenic recovery method for ethylene |
| CN113548939A (en) * | 2020-04-24 | 2021-10-26 | 中国石化工程建设有限公司 | Method and device for reducing temperature of high-pressure depropanizing tower kettle of ethylene device |
| CN114087849A (en) * | 2021-11-25 | 2022-02-25 | 北京恒泰洁能科技有限公司 | Pyrolysis gas cryogenic separation method |
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| CN115253612A (en) * | 2022-08-25 | 2022-11-01 | 国家能源集团宁夏煤业有限责任公司 | Fischer-Tropsch synthesis tail gas separation and recovery system and method |
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Citations (13)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101434507A (en) * | 2008-11-19 | 2009-05-20 | 上海惠生化工工程有限公司 | Separation method for fischer-tropsch synthesis tail gas |
| CN101559320A (en) * | 2009-04-15 | 2009-10-21 | 上海惠生化工工程有限公司 | Separation method of Fischer-Tropsch synthesis gas by combining rectification and solvent absorption |
| CN104628508A (en) * | 2015-01-30 | 2015-05-20 | 华南理工大学 | System and process for preparing alkene from raw materials of coal and natural gas by virtue of synthesis |
| CN204509155U (en) * | 2015-01-30 | 2015-07-29 | 华南理工大学 | A kind of with coal and Sweet natural gas for raw material is through the system of synthetic gas alkene |
| US20150322350A1 (en) * | 2014-05-09 | 2015-11-12 | Siluria Technologies, Inc. | Fischer-Tropsch Based Gas to Liquids Systems and Methods |
| CN105779046A (en) * | 2014-12-16 | 2016-07-20 | 中科合成油工程股份有限公司 | Method for preparing LNG (Liquefied Natural Gas) by using Fischer-Tropsch synthesis tail gas as raw material |
| CN105838465A (en) * | 2016-05-20 | 2016-08-10 | 北京中科瑞奥能源科技股份有限公司 | Process and system for preparing liquefied natural gas by utilizing Fischer-Tropsch synthesis tail gas |
| CN106256813A (en) * | 2015-06-16 | 2016-12-28 | 中国石化工程建设有限公司 | A kind of separation and recovery method of Fischer-Tropsch process exhaust |
| CN106316750A (en) * | 2015-06-16 | 2017-01-11 | 中国石化工程建设有限公司 | Recovery device of Fischer-Tropsch synthesis tail gas |
| CN106800275A (en) * | 2015-11-25 | 2017-06-06 | 神华集团有限责任公司 | A kind of method for processing high temperature fischer-tropsch synthesis tail gas |
| CN108017481A (en) * | 2016-11-03 | 2018-05-11 | 中国石油化工股份有限公司 | By the separator and method of the product gas of the direct producing light olefins of synthesis gas |
| CN108276236A (en) * | 2017-01-06 | 2018-07-13 | 中国石化工程建设有限公司 | A kind of Fischer-Tropsch process exhaust cryogenic separation recovery method of volume increase alkene |
| CN208883740U (en) * | 2018-09-28 | 2019-05-21 | 北京恒泰洁能科技有限公司 | A kind of expense drags synthesis tail gas deep cooling recyclable device |
-
2018
- 2018-09-28 CN CN201811140277.9A patent/CN109111336B/en active Active
Patent Citations (13)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101434507A (en) * | 2008-11-19 | 2009-05-20 | 上海惠生化工工程有限公司 | Separation method for fischer-tropsch synthesis tail gas |
| CN101559320A (en) * | 2009-04-15 | 2009-10-21 | 上海惠生化工工程有限公司 | Separation method of Fischer-Tropsch synthesis gas by combining rectification and solvent absorption |
| US20150322350A1 (en) * | 2014-05-09 | 2015-11-12 | Siluria Technologies, Inc. | Fischer-Tropsch Based Gas to Liquids Systems and Methods |
| CN105779046A (en) * | 2014-12-16 | 2016-07-20 | 中科合成油工程股份有限公司 | Method for preparing LNG (Liquefied Natural Gas) by using Fischer-Tropsch synthesis tail gas as raw material |
| CN104628508A (en) * | 2015-01-30 | 2015-05-20 | 华南理工大学 | System and process for preparing alkene from raw materials of coal and natural gas by virtue of synthesis |
| CN204509155U (en) * | 2015-01-30 | 2015-07-29 | 华南理工大学 | A kind of with coal and Sweet natural gas for raw material is through the system of synthetic gas alkene |
| CN106316750A (en) * | 2015-06-16 | 2017-01-11 | 中国石化工程建设有限公司 | Recovery device of Fischer-Tropsch synthesis tail gas |
| CN106256813A (en) * | 2015-06-16 | 2016-12-28 | 中国石化工程建设有限公司 | A kind of separation and recovery method of Fischer-Tropsch process exhaust |
| CN106800275A (en) * | 2015-11-25 | 2017-06-06 | 神华集团有限责任公司 | A kind of method for processing high temperature fischer-tropsch synthesis tail gas |
| CN105838465A (en) * | 2016-05-20 | 2016-08-10 | 北京中科瑞奥能源科技股份有限公司 | Process and system for preparing liquefied natural gas by utilizing Fischer-Tropsch synthesis tail gas |
| CN108017481A (en) * | 2016-11-03 | 2018-05-11 | 中国石油化工股份有限公司 | By the separator and method of the product gas of the direct producing light olefins of synthesis gas |
| CN108276236A (en) * | 2017-01-06 | 2018-07-13 | 中国石化工程建设有限公司 | A kind of Fischer-Tropsch process exhaust cryogenic separation recovery method of volume increase alkene |
| CN208883740U (en) * | 2018-09-28 | 2019-05-21 | 北京恒泰洁能科技有限公司 | A kind of expense drags synthesis tail gas deep cooling recyclable device |
Cited By (11)
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|---|---|---|---|---|
| CN110054153A (en) * | 2019-04-18 | 2019-07-26 | 裴栋中 | A kind of device of refinery factory refinery dry gas purification hydrogen manufacturing |
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| CN112361715A (en) * | 2020-10-19 | 2021-02-12 | 中国石油化工股份有限公司 | Cryogenic recovery method for ethylene |
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| CN115253612A (en) * | 2022-08-25 | 2022-11-01 | 国家能源集团宁夏煤业有限责任公司 | Fischer-Tropsch synthesis tail gas separation and recovery system and method |
| CN115253612B (en) * | 2022-08-25 | 2024-02-02 | 国家能源集团宁夏煤业有限责任公司 | Fischer-Tropsch synthesis tail gas separation and recovery system and method |
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