CN105861086A - Process method for co-producing liquefied natural gas, methanol and liquid ammonia by using gasified coal gas and coke oven gas - Google Patents
Process method for co-producing liquefied natural gas, methanol and liquid ammonia by using gasified coal gas and coke oven gas Download PDFInfo
- Publication number
- CN105861086A CN105861086A CN201610305951.9A CN201610305951A CN105861086A CN 105861086 A CN105861086 A CN 105861086A CN 201610305951 A CN201610305951 A CN 201610305951A CN 105861086 A CN105861086 A CN 105861086A
- Authority
- CN
- China
- Prior art keywords
- gas
- coke
- hydrogen
- stove
- nitrogen
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
- 239000007789 gas Substances 0.000 title claims abstract description 243
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 title claims abstract description 117
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 title claims abstract description 92
- 238000000034 method Methods 0.000 title claims abstract description 51
- 239000003949 liquefied natural gas Substances 0.000 title claims abstract description 45
- 230000008569 process Effects 0.000 title claims abstract description 36
- 239000003034 coal gas Substances 0.000 title claims description 7
- 239000011335 coal coke Substances 0.000 title description 2
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims abstract description 170
- 239000001257 hydrogen Substances 0.000 claims abstract description 72
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 72
- 229910052757 nitrogen Inorganic materials 0.000 claims abstract description 70
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 68
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims abstract description 50
- 229910021529 ammonia Inorganic materials 0.000 claims abstract description 44
- 239000007788 liquid Substances 0.000 claims abstract description 37
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 35
- 229910002091 carbon monoxide Inorganic materials 0.000 claims abstract description 35
- 238000005406 washing Methods 0.000 claims abstract description 33
- 239000000571 coke Substances 0.000 claims abstract description 19
- 230000015572 biosynthetic process Effects 0.000 claims description 37
- 238000003786 synthesis reaction Methods 0.000 claims description 37
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims description 36
- 229910001873 dinitrogen Inorganic materials 0.000 claims description 30
- 238000002309 gasification Methods 0.000 claims description 25
- 238000004519 manufacturing process Methods 0.000 claims description 24
- WWYNJERNGUHSAO-XUDSTZEESA-N (+)-Norgestrel Chemical compound 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 claims description 21
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 18
- 229910052799 carbon Inorganic materials 0.000 claims description 18
- 229910002092 carbon dioxide Inorganic materials 0.000 claims description 18
- 238000005516 engineering process Methods 0.000 claims description 17
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 claims description 16
- 239000001569 carbon dioxide Substances 0.000 claims description 16
- 239000013589 supplement Substances 0.000 claims description 14
- 239000003245 coal Substances 0.000 claims description 13
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 claims description 12
- 239000000047 product Substances 0.000 claims description 12
- 238000001816 cooling Methods 0.000 claims description 11
- 239000012535 impurity Substances 0.000 claims description 8
- 238000006243 chemical reaction Methods 0.000 claims description 7
- 230000008676 import Effects 0.000 claims description 7
- 125000001741 organic sulfur group Chemical group 0.000 claims description 7
- 238000005204 segregation Methods 0.000 claims description 7
- 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 6
- QMMZSJPSPRTHGB-UHFFFAOYSA-N MDEA Natural products CC(C)CCCCC=CCC=CC(O)=O QMMZSJPSPRTHGB-UHFFFAOYSA-N 0.000 claims description 6
- 230000002745 absorbent Effects 0.000 claims description 6
- 239000002250 absorbent Substances 0.000 claims description 6
- 230000003139 buffering effect Effects 0.000 claims description 5
- 239000000428 dust Substances 0.000 claims description 5
- 229910000037 hydrogen sulfide Inorganic materials 0.000 claims description 5
- 230000009469 supplementation Effects 0.000 claims description 5
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims description 4
- 150000002431 hydrogen Chemical class 0.000 claims description 4
- 238000002156 mixing Methods 0.000 claims description 4
- 239000002994 raw material Substances 0.000 claims description 4
- 229910052717 sulfur Inorganic materials 0.000 claims description 4
- 239000011593 sulfur Substances 0.000 claims description 4
- 238000006356 dehydrogenation reaction Methods 0.000 claims description 3
- 239000002808 molecular sieve Substances 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
- 230000001502 supplementing effect Effects 0.000 claims description 3
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 claims 7
- 238000000926 separation method Methods 0.000 abstract description 10
- 238000004939 coking Methods 0.000 description 4
- 238000005261 decarburization Methods 0.000 description 4
- 238000006477 desulfuration reaction Methods 0.000 description 3
- 230000023556 desulfurization Effects 0.000 description 3
- 239000000126 substance Substances 0.000 description 3
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 2
- 230000008901 benefit Effects 0.000 description 2
- 230000008859 change Effects 0.000 description 2
- 239000000446 fuel Substances 0.000 description 2
- 230000035800 maturation Effects 0.000 description 2
- 229910052756 noble gas Inorganic materials 0.000 description 2
- 229910052760 oxygen Inorganic materials 0.000 description 2
- 239000001301 oxygen Substances 0.000 description 2
- 230000001105 regulatory effect Effects 0.000 description 2
- 229920006395 saturated elastomer Polymers 0.000 description 2
- 230000033228 biological regulation Effects 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 239000003610 charcoal Substances 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 238000007906 compression Methods 0.000 description 1
- 239000000470 constituent Substances 0.000 description 1
- 238000005262 decarbonization Methods 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000001035 drying Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000003345 natural gas Substances 0.000 description 1
- 238000010926 purge Methods 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 230000006641 stabilisation Effects 0.000 description 1
- 238000011144 upstream manufacturing Methods 0.000 description 1
- 239000002912 waste gas Substances 0.000 description 1
Classifications
-
- 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
- C10L3/06—Natural gas; Synthetic natural gas obtained by processes not covered by C10G, C10K3/02 or C10K3/04
- C10L3/08—Production of synthetic natural gas
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
- C01B3/50—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
- C07C29/15—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively
- C07C29/151—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively with hydrogen or hydrogen-containing gases
- C07C29/1516—Multisteps
- C07C29/1518—Multisteps one step being the formation of initial mixture of carbon oxides and hydrogen for synthesis
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
- C01B2203/0415—Purification by absorption in liquids
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
- C01B2203/042—Purification by adsorption on solids
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
- C01B2203/046—Purification by cryogenic separation
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
- C01B2203/0465—Composition of the impurity
- C01B2203/0475—Composition of the impurity the impurity being carbon dioxide
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
- C01B2203/0465—Composition of the impurity
- C01B2203/048—Composition of the impurity the impurity being an organic compound
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
- C01B2203/0465—Composition of the impurity
- C01B2203/0485—Composition of the impurity the impurity being a sulfur compound
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
- C01B2203/0465—Composition of the impurity
- C01B2203/0495—Composition of the impurity the impurity being water
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Combustion & Propulsion (AREA)
- Inorganic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Industrial Gases (AREA)
- Carbon And Carbon Compounds (AREA)
- Separation By Low-Temperature Treatments (AREA)
Abstract
The process method for co-producing liquefied natural gas, methanol and liquid ammonia by using gasified gas and coke oven gas provided by the invention is characterized in that the liquefied natural gas, the methanol and the liquid ammonia are co-produced by using the coke oven gas, LNG is produced by using the coke oven gas, the methanol is produced by using the coke oven gas, the synthetic ammonia, cryogenic liquefaction separation, liquid nitrogen washing and the like are organically linked together through reasonable configuration, LNG is produced by using component methane in the coke oven gas, the methanol is produced by using component hydrogen and carbon monoxide in the coke oven gas, and the liquid ammonia is produced by using the hydrogen and nitrogen in the coke oven gas.
Description
Technical field
The invention belongs to coal chemical technology, particularly relate to one and utilize gasification gas and coke-stove gas co-production of liquefied
The process of natural gas, methanol and liquefied ammonia.
Background technology
Coke-stove gas also known as oven gas, refer to coal for coking in coke oven after high-temperature retorting, burnt in output
While charcoal and tar product, produced a kind of imflammable gas, is the side-product of coking industry.Coke-oven coal
The calorific value of gas is higher, is typically used as fuel or the town gas of high temperature industrial furnace.
Along with environmental requirement gradually steps up, the profit of new coking industry permit standard clear stipulaties coke-stove gas
Will be more than 98% by rate, coking industry recessed market simultaneously, production capacity surplus is serious, and people come to realise Jiao
The huge value of producer gas, therefore have developed many coke-stove gas and utilizes technology, such as coke-stove gas system
Liquefied natural gas, coke-stove gas methanol etc..
But, the main component of coke-stove gas is hydrogen (55-60%) and methane (23-27%), also has a small amount of
The components such as carbon monoxide, carbon dioxide, nitrogen, have the feature of " the few carbon of hydrogen-rich ".As only with monotechnics
Turning out a produce, constituent part can be caused not make full use of, the tail gas containing hydrogen partial need to separately be found out
Road or fuel can only be used as.It addition, produce single product to face bigger market risk, controllability is relatively
Difference.
Therefore, the existing resource situation of comprehensive consideration coal chemical enterprise (waste gas, useless solid), existing technology is (burnt
Producer gas LNG, coke-stove gas methanol, synthesis ammonia, cryogenic liquefying separation, liquid nitrogen washing) organic connections
Together, and certain technological means and regulating measure is taked to make each component reach suitable ratio, thus
Coproduction multiple product, on the one hand can realize efficiently making full use of of resource, reduces the pollution to environment, separately
On the one hand the impact that product price fluctuation brings can be successfully managed, greatly by adjusting the yield of each product
The big coal chemical enterprise that improves resists the ability of market risk.
Summary of the invention
In view of this, in order to overcome defect and the problem of prior art, the present invention provides one to utilize gasification of coal
Gas and coke-stove gas co-production of liquefied natural gas, methanol and the process of liquefied ammonia.
A kind of utilize gasification gas and coke-stove gas co-production of liquefied natural gas, methanol and the process of liquefied ammonia,
Comprise the steps: successively
Step S10: described coke-stove gas is sent into gas holder buffering so that it is pressure stability；
Step S20: the coke-stove gas after in step S10 is pressurized to 2.0～2.2Mpa；
Step S30: be inorganic sulfur by the organic sulfur conversion in the coke-stove gas after step S20；
Step S40: continue to be compressed to 2.5～3Mpa by the coke-stove gas after step S30；
Step S50: the sour gas in removing coke-stove gas after step S40, described sour gas includes:
Sulfur dioxide, hydrogen sulfide, carbon dioxide；
Step S60: the moisture in removing coke-stove gas after step S50, is down to its dew point
-65～-70 DEG C；
Step S70: separate the gas composition in coke-stove gas after step S60, respectively obtain LNG,
Hydrogen and nitrogen gas, rich carbon monoxide gas and hydrogen rich gas.
In certain embodiments, also comprise the steps:
Step S180: described hydrogen and nitrogen gas is sent to ammonia synthesis system, described rich carbon monoxide gas and hydrogen rich gas are sent to
System for methanol synthesis.
In certain embodiments, in step S10, in described coke-stove gas, methane volumetric mark is 20～30%,
Hydrogen volume mark is 40～60%, and carbon monoxide volume fraction is 8～15%, and surplus is nitrogen, carbon dioxide,
The organic sulfur of trace, SO2, tar, dust and steam.
In certain embodiments, in step S40, continue to be compressed to by the coke-stove gas after step S30
2.5～3Mpa, particularly as follows:
Reciprocating or centrifugal compressor is used to continue coke-stove gas to be compressed to 2.5～3MPa.
Sour gas in certain embodiments, in step S50, in removing coke-stove gas after step S40
Body, particularly as follows:
Using the sour gas in wet processing removing coke-stove gas, the absorbent in described wet processing is
MDEA solution.
In certain embodiments, in step S60, the moisture in removing coke-stove gas after step S50,
Its dew point is down to-70 DEG C, particularly as follows:
Use the moisture in molecular sieve adsorption technique removing coke-stove gas, its dew point is down to-65～-70 DEG C.
In certain embodiments, in step S70, separate the gas group in the coke-stove gas after step S60
Part, respectively obtain LNG, hydrogen and nitrogen gas, rich carbon monoxide gas and hydrogen rich gas, particularly as follows:
The gas group that the technology using cryogenic liquefying, cryogenic rectification and liquid nitrogen washing to combine realizes in coke-stove gas
Part separates, and obtains LNG, hydrogen and nitrogen gas, rich carbon monoxide gas and hydrogen rich gas.
In certain embodiments, the technology using cryogenic liquefying, cryogenic rectification and liquid nitrogen washing to combine realizes Jiao
Gas composition in producer gas separates, and obtains LNG, hydrogen and nitrogen gas, rich carbon monoxide gas and hydrogen rich gas, including
Following step:
Cooling: the coke-stove gas after step S60 is cooled to-150～-165 DEG C；
Dehydrogenation: use the technique of cryogenic rectification by hydrogen and carbon monoxide, nitrogen removing, the richness of isolated
Methane stream is sent to domethanizing column and refines further；A hydrogen rich gas part for isolated is delivered to liquid nitrogen washing and is refined,
Another part delivers to system for methanol synthesis；
Demethanation: use the technique of cryogenic rectification by the impurity removal in methane rich logistics, obtain at the bottom of methane tower tower
To pure LNG product, demethanizer column overhead tail gas is carbon monoxide, described impurity include hydrogen, nitrogen,
Carbon monoxide；
Liquid nitrogen washing: the carbon monoxide in liquid nitrogen washing removing process gas, methane gas, obtain pure hydrogen and
Nitrogen mixture-hydrogen and nitrogen gas, hydrogen rich off gas is after liquid nitrogen washing processes, and hydrogen and nitrogen gas delivers to ammonia synthesis system；Liquid nitrogen
Washing tail-gas then imports demethanation tail gas and delivers to system for methanol synthesis.
In certain embodiments, before carrying out step S10, comprise the steps: the most successively
Rich carbon gas supplements: supplementing carbon-rich gas in described coke-stove gas, described carbon-rich gas is coke gasification
One or more mixing therein of gas, coal gas of converter, blast furnace gas, coal synthesis gas；
Nitrogen supplements: the nitrogen required supplementation with delivers to the segregation apparatus that liquefies, and after cooling liquefaction, then delivers to liquid
Nitrogen is washed and is used as absorbent, imports the raw material as synthesis ammonia system in hydrogen and nitrogen gas simultaneously；
Nitrogen is finely tuned: the hydrogen and nitrogen gas obtained through liquid nitrogen washing, supplements appropriate nitrogen；
Carbon dioxide is finely tuned: supplement appropriate carbon dioxide in the rich CO gas that liquefaction segregation apparatus obtains.
What the present invention provided utilizes gasification gas and coke-stove gas co-production of liquefied natural gas, methanol and the work of liquefied ammonia
Process utilizes coke-stove gas co-production of liquefied natural gas, methanol and liquefied ammonia, by reasonable disposition by coke-stove gas
LNG processed, coke-stove gas methanol, the synthesis organic connections such as ammonia, cryogenic liquefying separation, liquid nitrogen washing together,
Component methane production LNG being utilized respectively in coke-stove gas, utilizes the component hydrogen in coke-stove gas and an oxygen
Change carbon and produce methanol, utilize hydrogen gas in coke oven gas and nitrogen production liquefied ammonia, relative to prior art, this
Bright have an advantage that
(1), the application comprehensively utilize existing Technology, coke-stove gas all components is carried out need not
In the case of being completely separated, it is achieved maximally utilizing of coke-stove gas, greatly reduce running cost.With
Time, because existing technique is entirely maturation process, this guarantees the feasibility of process route.
(2), liquid nitrogen washing technology is introduced in deep cooling process for separating by the application, it is ensured that the purity of unstripped gas,
Avoid bringing the noble gas such as carbon monoxide, methane into ammonia synthesis system.
(3), present applicant proposes multicomponent and supplement micro-tensioning system, enhance the scalable of whole set process system
Property and adaptability, subject range is extensive.
Accompanying drawing explanation
Fig. 1 utilizes gasification gas and coke-stove gas co-production of liquefied natural gas, methanol for the low temperature that the present invention provides
Flow chart of steps with the process of liquefied ammonia.
Fig. 2 utilizes gasification gas and coke-stove gas co-production of liquefied natural gas, methanol for the low temperature that the present invention provides
Process principle figure with the process of liquefied ammonia.
Fig. 3 is that the technology using cryogenic liquefying, cryogenic rectification and liquid nitrogen washing to combine realizes in coke-stove gas
The flow chart of steps that gas composition separates.
Fig. 4 is deep cooling process for separating schematic diagram for Fig. 2 that the present invention provides.
Detailed description of the invention
For the ease of understanding the present invention, below with reference to relevant drawings, the present invention is described more fully.
Accompanying drawing gives the better embodiment of the present invention.These are only the preferred embodiments of the present invention, and unprovoked
This limits the scope of the claims of the present invention, every equivalent structure utilizing description of the invention and accompanying drawing content to be made
Or equivalence flow process conversion, or directly or indirectly it is used in other relevant technical fields, the most in like manner it is included in this
In the scope of patent protection of invention.
Unless otherwise defined, all of technology used herein and scientific terminology and the technology belonging to the present invention
The implication that the technical staff in field is generally understood that is identical.The art used the most in the description of the invention
Language is intended merely to describe the purpose of specific embodiment, it is not intended that in limiting the present invention.Used herein
Term " and/or " include the arbitrary and all of combination of one or more relevant Listed Items.
Referring to Fig. 1 and Fig. 2, a preferred embodiment of the present invention provides one to utilize gasification gas and coke-stove gas
The process of co-production of liquefied natural gas, methanol and liquefied ammonia, comprises the steps: successively
Step S10: described coke-stove gas is sent into gas holder buffering so that it is pressure stability；
Preferably, in described coke-stove gas, methane content (volume fraction) is 20～30%, and hydrogen content is
40～60%, carbon monoxide content is 8～15%, and surplus is nitrogen, carbon dioxide, the organic sulfur of trace, SO2,
Tar, dust and steam.
It is appreciated that as ensureing stablizing of subsequent handling, coke-stove gas is sent into gas holder buffering, it is ensured that
Pressure stability so that subsequent technique is reliable and stable；
Step S20: the coke-stove gas after in step S10 is pressurized to 2.0～2.2Mpa；
It is appreciated that and the coke-stove gas after in step S10 can be pressurized to by compression process
2.0～2.2Mpa.
Step S30: be inorganic sulfur by the organic sulfur conversion in the coke-stove gas after step S20；
It is appreciated that the organic sulfur conversion being capable of in coke-stove gas by hydro-conversion is inorganic sulfur.
Step S40: continue to be compressed to 2.5～3Mpa by the coke-stove gas after step S30；
Preferably, reciprocating or centrifugal compressor is used to continue coke-stove gas to be compressed to 2.5～3MPa.
Step S50: the sour gas in removing coke-stove gas after step S40, described sour gas includes:
Sulfur dioxide, hydrogen sulfide, carbon dioxide；
Preferably, the sour gas in wet processing removing coke-stove gas, the suction in described wet processing are used
Receiving agent is MDEA solution.
Step S60: the moisture in removing coke-stove gas after step S50, is down to-65～-70 DEG C by its dew point；
Preferably, use the moisture in molecular sieve adsorption technique removing coke-stove gas, its dew point is down to-70 DEG C.
Step S70: separate the gas composition in coke-stove gas after step S60, respectively obtain LNG,
Hydrogen and nitrogen gas, rich carbon monoxide gas and hydrogen rich gas.
It is appreciated that LNG obtained above sells as product；Hydrogen and nitrogen gas is sent to ammonia synthesis system, is used for
Produce liquefied ammonia product；Rich carbon monoxide gas was first pressurized to for 2.0～2.5MPa (pressure mates) with hydrogen rich gas, with
Delivering to system for methanol synthesis after hydrogen rich gas mixing, be used for producing methanol product, methanol purge gas sends coke oven back to.
Preferably, the technology using cryogenic liquefying, cryogenic rectification and liquid nitrogen washing to combine realizes in coke-stove gas
Gas composition separate, obtain LNG, hydrogen and nitrogen gas, rich carbon monoxide gas and hydrogen rich gas.
Specifically, referring to Fig. 3, the technology using cryogenic liquefying, cryogenic rectification and liquid nitrogen washing to combine realizes
Gas composition in coke-stove gas separates, and obtains LNG, hydrogen and nitrogen gas, rich carbon monoxide gas and hydrogen rich gas, bag
Include following step:
Step S71: cooling: the coke-stove gas after step S60 is cooled to-150～-165 DEG C；
Step S72: dehydrogenation: use the technique of cryogenic rectification by hydrogen and carbon monoxide, nitrogen removing, separate
The methane rich logistics obtained is sent to domethanizing column and refines further；A hydrogen rich gas part for isolated delivers to liquid
Nitrogen is washed refined, and another part delivers to system for methanol synthesis；
Step S73: demethanation: use the technique of cryogenic rectification by the impurity removal in methane rich logistics, methane
Obtaining pure LNG product at the bottom of tower tower, demethanizer column overhead tail gas is carbon monoxide, and described impurity includes hydrogen
Gas, nitrogen, carbon monoxide；
Step S74: liquid nitrogen washing: the carbon monoxide in liquid nitrogen washing removing process gas, methane gas, obtains pure
Hydrogen and nitrogen mixture-hydrogen and nitrogen gas, hydrogen rich off gas through liquid nitrogen washing process after, hydrogen and nitrogen gas delivers to ammonia synthesis system
System；Liquid nitrogen washing tail gas then imports demethanation tail gas and delivers to system for methanol synthesis.
Further, refer to Fig. 4, before carrying out step S10, comprise the steps: the most successively
Rich carbon gas supplements: supplementing carbon-rich gas in described coke-stove gas, described carbon-rich gas is coke gasification
One or more mixing therein of gas, coal gas of converter, blast furnace gas, coal synthesis gas；Be appreciated that due to
Coke-stove gas has the feature of " the few carbon of hydrogen-rich ", and the tail gas composition after removing methane tends not to meet methanol-fueled CLC
Demand, it is therefore desirable to design mend carbon system.Carbon-rich gas can have multiple source, such as coal gas of converter, height
Producer gas, coal synthesis gas, coke gasification gas etc..Impurity content according to carbon-rich gas is different with pressure, point
Access system the most in place, as pressure is relatively low, fills into gas holder, accessible secondary liter as higher in pressure
Before pressure or before MDEA desulfurization and decarburization.Rich carbon gas can be coke gasification gas, coal synthesis gas, coal gas of converter,
Blast furnace gas.
Nitrogen supplements: the nitrogen required supplementation with delivers to the segregation apparatus that liquefies, and after cooling liquefaction, then delivers to liquid
Nitrogen is washed and is used as absorbent, imports the raw material as synthesis ammonia system in hydrogen and nitrogen gas simultaneously；
It is appreciated that supplementary nitrogen, after cooling liquefaction, is delivered to liquid nitrogen washing and used as absorbent, simultaneously
Import again the raw material as synthesis ammonia system in hydrogen and nitrogen gas, there is the effect of two aspects.Nitrogen can be taken from
Air separation unit.
Nitrogen is finely tuned: the hydrogen and nitrogen gas obtained through liquid nitrogen washing, supplements appropriate nitrogen；
Be appreciated that through the hydrogen and nitrogen gas that liquid nitrogen washing obtains, its composition can not fully meet ammonia synthesis most preferably than
Example, requires supplementation with a small amount of nitrogen, is used for forming fine setting.Nitrogen can take from air separation unit.
Carbon dioxide is finely tuned: supplement appropriate carbon dioxide in the rich CO gas that liquefaction segregation apparatus obtains.
Be appreciated that rich CO gas and hydrogen rich gas after converging as the unstripped gas of system for methanol synthesis, its C/Hratio
The optimal proportion of methanol-fueled CLC can not be fully met, require supplementation with a small amount of carbon dioxide, be used for forming fine setting.
Carbon dioxide can take from the decarbonization device of process upstream.
What the present invention provided utilizes gasification gas and coke-stove gas co-production of liquefied natural gas, methanol and the work of liquefied ammonia
Process utilizes coke-stove gas co-production of liquefied natural gas, methanol and liquefied ammonia, by reasonable disposition by coke-stove gas
LNG processed, coke-stove gas methanol, the synthesis organic connections such as ammonia, cryogenic liquefying separation, liquid nitrogen washing together,
Component methane production LNG being utilized respectively in coke-stove gas, utilizes the component hydrogen in coke-stove gas and an oxygen
Change carbon and produce methanol, utilize hydrogen gas in coke oven gas and nitrogen production liquefied ammonia, relative to prior art, this
Bright have an advantage that
(1), the application comprehensively utilize existing Technology, coke-stove gas all components is carried out need not
In the case of being completely separated, it is achieved maximally utilizing of coke-stove gas, greatly reduce running cost.With
Time, because existing technique is entirely maturation process, this guarantees the feasibility of process route.
(2), liquid nitrogen washing technology is introduced in deep cooling process for separating by the application, it is ensured that the purity of unstripped gas,
Avoid bringing the noble gas such as carbon monoxide, methane into ammonia synthesis system.
(3), present applicant proposes multicomponent and supplement micro-tensioning system, enhance the scalable of whole set process system
Property and adaptability, subject range is extensive.
Embodiment
As shown in table 1, pressure is 1～5kPa (G) to typical coke-stove gas composition, and temperature is about 40 DEG C, stream
Amount is 34000Nm3/h.
The volume composition of table 1 coke-stove gas
| H2 | CO | CO2 | CH4 | CnHm | N2 |
| 53.82 | 10.74 | 4.68 | 22.57 | 3.15 | 4.63 |
| O2 | H2S | Add up to | Tar and dust | Steam | |
| 0.41 | Trace | 100 | Trace | Saturated |
Technique as shown in Figure 1, coke-stove gas is first fed into gas holder buffering, and after pressure stabilisation utilization is compressed
Machine is pressurized to about 2.0MPa, carries out hydro-conversion process, then carries out secondary booster to 2.8MPa, send
Enter MDEA desulfurization and decarburization device and carry out purified treatment, then deliver to drying device removing moisture, be then fed into deep
Cold liquefaction segregation apparatus carries out degree of depth separation, and gained each several part gas is sent to ammonia synthesis system respectively and methanol closes
One-tenth system, simultaneously output LNG product.Under the feed conditions of the present embodiment, LNG0.858 hundred million can be produced
Nm3/a, methanol 12.34 ten thousand t/a, liquefied ammonia 10.16 ten thousand t/a.
Hydrogen content in coke-stove gas is higher, and carbon monoxide, nitrogen equal size are relatively low, at the present embodiment
In, to intend using coke gasification gas to carry out mending carbon, its pressure is 3.0MPa, and temperature is 40 DEG C, and flow is 82000
Nm3/h, composition is as shown in table 2.
The volume composition of table 2 coke gasification gas
| H2 | CO | CO2 | CH4 | CnHm | N2 |
| 41.2 | 25.5 | 29 | 3.5 | - | 0.3 |
| O2 | H2S | Add up to | Tar and dust | Steam | |
| 0.3 | 0.2 | 100 | Trace | Saturated |
After the pressurized gasification of coke obtains the gas that gasifies, then the operation such as transformed, PSA decarburization processes, its pressure
It is about 2.8MPa, merges together with coke-stove gas before MDEA desulfurization and decarburization device.
From the pure nitrogen gas about 7800Nm3/h of air separation unit, send into cryogenic separation device, through heat exchanger progressively
After cooling liquefaction, send into liquid nitrogen washing tower by the impurity such as carbon monoxide, methane and Hydrogen Separation, simultaneously and hydrogen
Send into ammonia synthesis system together.
It addition, be the feed composition of regulation ammonia synthesis system, 1500Nm3/h need to be supplemented before ammonia synthesis system
Pure nitrogen gas.For regulating the feed composition of system for methanol synthesis, 900Nm3/h need to be supplemented before system for methanol synthesis
Pure carbon dioxide.
Embodiment described above only have expressed the several embodiments of the present invention, and it describes more concrete and detailed,
But therefore can not be interpreted as the restriction to the scope of the claims of the present invention.It should be pointed out that, for this area
Those of ordinary skill for, without departing from the inventive concept of the premise, it is also possible to make some deformation and
Improving, these broadly fall into protection scope of the present invention.Therefore, the protection domain of patent of the present invention should be with appended
Claim is as the criterion.
Claims (8)
1. utilize gasification gas and coke-stove gas co-production of liquefied natural gas, methanol and a process for liquefied ammonia,
It is characterized in that, comprise the steps: successively
Step S10: described coke-stove gas is sent into gas holder buffering so that it is pressure stability；
Step S20: the coke-stove gas after in step S10 is pressurized to 2.0～2.2Mpa；
Step S30: be inorganic sulfur by the organic sulfur conversion in the coke-stove gas after step S20；
Step S40: continue to be compressed to 2.5～3Mpa by the coke-stove gas after step S30；
Step S50: the sour gas in removing coke-stove gas after step S40, described sour gas includes:
Sulfur dioxide, hydrogen sulfide, carbon dioxide；
Step S60: the moisture in removing coke-stove gas after step S50, is down to-65～-70 DEG C by its dew point；
Step S70: separate the gas composition in coke-stove gas after step S60, respectively obtain LNG,
Hydrogen and nitrogen gas, rich carbon monoxide gas and hydrogen rich gas；
Before carrying out step S10, comprise the steps: the most successively
Rich carbon gas supplements: supplementing carbon-rich gas in described coke-stove gas, described carbon-rich gas is coke gasification
One or more mixing therein of gas, coal gas of converter, blast furnace gas, coal synthesis gas；
Nitrogen supplements: the nitrogen required supplementation with delivers to the segregation apparatus that liquefies, and after cooling liquefaction, then delivers to liquid
Nitrogen is washed and is used as absorbent, imports the raw material as synthesis ammonia system in hydrogen and nitrogen gas simultaneously；
Nitrogen is finely tuned: the hydrogen and nitrogen gas obtained through liquid nitrogen washing, supplements appropriate nitrogen；
Carbon dioxide is finely tuned: supplement appropriate carbon dioxide in the rich CO gas that liquefaction segregation apparatus obtains.
2. low temperature as claimed in claim 1 utilizes gasification gas and coke-stove gas co-production of liquefied natural gas, first
Alcohol and the process of liquefied ammonia, it is characterised in that also comprise the steps:
Step S180: described hydrogen and nitrogen gas is sent to ammonia synthesis system, described rich carbon monoxide gas and hydrogen rich gas are sent to
System for methanol synthesis.
3. low temperature as claimed in claim 1 utilizes gasification gas and coke-stove gas co-production of liquefied natural gas, first
Alcohol and the process of liquefied ammonia, it is characterised in that in step S10, in described coke-stove gas, methane volumetric divides
Number is 20～30%, and hydrogen volume mark is 40～60%, and carbon monoxide volume fraction is 8～15%, and surplus is
Nitrogen, carbon dioxide, the organic sulfur of trace, SO2, tar, dust and steam.
4. low temperature as claimed in claim 1 utilizes gasification gas and coke-stove gas co-production of liquefied natural gas, first
Alcohol and the process of liquefied ammonia, it is characterised in that in step S40, by the coke-stove gas after step S30
Continue to be compressed to 2.5～3Mpa, particularly as follows:
Reciprocating or centrifugal compressor is used to continue coke-stove gas to be compressed to 2.5～3MPa.
5. low temperature as claimed in claim 1 utilizes gasification gas and coke-stove gas co-production of liquefied natural gas, first
Alcohol and the process of liquefied ammonia, it is characterised in that in step S50, removing coke-oven coal after step S40
Sour gas in gas, particularly as follows:
Using the sour gas in wet processing removing coke-stove gas, the absorbent in described wet processing is
MDEA solution.
6. low temperature as claimed in claim 1 utilizes gasification gas and coke-stove gas co-production of liquefied natural gas, first
Alcohol and the process of liquefied ammonia, it is characterised in that in step S60, removing coke-oven coal after step S50
Moisture in gas, is down to-65～-70 DEG C by its dew point, particularly as follows:
Use the moisture in molecular sieve adsorption technique removing coke-stove gas, its dew point is down to-70 DEG C.
7. low temperature as claimed in claim 1 utilizes gasification gas and coke-stove gas co-production of liquefied natural gas, first
Alcohol and the process of liquefied ammonia, it is characterised in that in step S70, separate the coke-oven coal after step S60
Gas composition in gas, respectively obtains LNG, hydrogen and nitrogen gas, rich carbon monoxide gas and hydrogen rich gas, particularly as follows:
The gas group that the technology using cryogenic liquefying, cryogenic rectification and liquid nitrogen washing to combine realizes in coke-stove gas
Part separates, and obtains LNG, hydrogen and nitrogen gas, rich carbon monoxide gas and hydrogen rich gas.
8. low temperature as claimed in claim 7 utilizes gasification gas and coke-stove gas co-production of liquefied natural gas, first
Alcohol and the process of liquefied ammonia, it is characterised in that use cryogenic liquefying, cryogenic rectification and liquid nitrogen washing to combine
Technology realize gas composition in coke-stove gas and separate, obtain LNG, hydrogen and nitrogen gas, rich carbon monoxide gas and
Hydrogen rich gas, comprises the steps:
Cooling: the coke-stove gas after step S60 is cooled to-150～-165 DEG C；
Dehydrogenation: use the technique of cryogenic rectification by hydrogen and carbon monoxide, nitrogen removing, the richness of isolated
Methane stream is sent to domethanizing column and refines further；A hydrogen rich gas part for isolated is delivered to liquid nitrogen washing and is refined,
Another part delivers to system for methanol synthesis；
Demethanation: use the technique of cryogenic rectification by the impurity removal in methane rich logistics, obtain at the bottom of methane tower tower
To pure LNG product, demethanizer column overhead tail gas is carbon monoxide, described impurity include hydrogen, nitrogen,
Carbon monoxide；
Liquid nitrogen washing: the carbon monoxide in liquid nitrogen washing removing process gas, methane gas, obtain pure hydrogen and
Nitrogen mixture-hydrogen and nitrogen gas, hydrogen rich off gas is after liquid nitrogen washing processes, and hydrogen and nitrogen gas delivers to ammonia synthesis system；Liquid nitrogen
Washing tail-gas then imports demethanation tail gas and delivers to system for methanol synthesis.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610305951.9A CN105861086B (en) | 2016-05-10 | 2016-05-10 | Process method for co-producing liquefied natural gas, methanol and liquid ammonia by using gasified coal gas and coke oven gas |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610305951.9A CN105861086B (en) | 2016-05-10 | 2016-05-10 | Process method for co-producing liquefied natural gas, methanol and liquid ammonia by using gasified coal gas and coke oven gas |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN105861086A true CN105861086A (en) | 2016-08-17 |
| CN105861086B CN105861086B (en) | 2019-04-26 |
Family
ID=56631705
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201610305951.9A Active CN105861086B (en) | 2016-05-10 | 2016-05-10 | Process method for co-producing liquefied natural gas, methanol and liquid ammonia by using gasified coal gas and coke oven gas |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN105861086B (en) |
Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106811238A (en) * | 2017-01-06 | 2017-06-09 | 河北中翔能源有限公司 | A kind of process of preparing LNG from coke oven tail gas and hydrogen rich off gas liquefied ammonia |
| CN107215848A (en) * | 2017-06-09 | 2017-09-29 | 杨皓 | A kind of carbon black tail gas and calcium carbide stove exhaust combined production of ammonia alcohol synthesis gas process |
| CN107235473A (en) * | 2017-06-09 | 2017-10-10 | 杨皓 | A kind of carbon black tail gas and coke oven tail gas combined production of ammonia alcohol synthesis gas process |
| CN107244651A (en) * | 2017-06-09 | 2017-10-13 | 杨皓 | A kind of blast furnace tail gas and coke oven tail gas combined production of ammonia alcohol synthesis gas process |
| CN107267706A (en) * | 2017-07-06 | 2017-10-20 | 中冶华天南京工程技术有限公司 | Coal gas of converter cooling system and its cooling means |
| CN109206295A (en) * | 2018-09-17 | 2019-01-15 | 陕西黑猫焦化股份有限公司 | A kind of synthesis ammonolysis gassing matches the method and system of coke-stove gas methanol |
| CN109595878A (en) * | 2018-12-10 | 2019-04-09 | 内蒙古博大实地化学有限公司 | A method of synthesis ammonia, urea co-production liquid CO 2 |
| CN111676069A (en) * | 2020-06-18 | 2020-09-18 | 中冶西北工程技术有限公司 | Coke oven gas purification system |
| CN112850645A (en) * | 2021-02-08 | 2021-05-28 | 赛鼎工程有限公司 | System and method for preparing synthetic ammonia by deeply purifying coke oven gas |
Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2006199838A (en) * | 2005-01-21 | 2006-08-03 | Teruie Fujiwara | Water gas-producing apparatus and water-gas producing method as well as waste processing method |
| CN1962586A (en) * | 2006-12-11 | 2007-05-16 | 山西丰喜肥业（集团）股份有限公司临猗分公司 | Methanol production process |
| CN101575540A (en) * | 2009-06-01 | 2009-11-11 | 中国科学院理化技术研究所 | Method for simultaneously producing liquefied natural gas and methanol |
| CN203229501U (en) * | 2013-03-04 | 2013-10-09 | 西安四联能源科技有限公司 | Device for preparing liquid natural gas from coke oven gas |
| CN103588221A (en) * | 2013-11-16 | 2014-02-19 | 山西阳煤丰喜肥业(集团)有限责任公司 | Method and device for co-production of synthetic ammonia and LNC (liquefied natural gas) by coke gas |
| CN105066585A (en) * | 2015-08-20 | 2015-11-18 | 上海尧兴投资管理有限公司 | Purifying and separating device and method for synthesis gas |
| CN105152864A (en) * | 2015-07-31 | 2015-12-16 | 赛鼎工程有限公司 | Technology for producing low carbon alcohol as well as by-product natural gas and liquefied ammonia from coke oven gas and synthetic gas |
-
2016
- 2016-05-10 CN CN201610305951.9A patent/CN105861086B/en active Active
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2006199838A (en) * | 2005-01-21 | 2006-08-03 | Teruie Fujiwara | Water gas-producing apparatus and water-gas producing method as well as waste processing method |
| CN1962586A (en) * | 2006-12-11 | 2007-05-16 | 山西丰喜肥业（集团）股份有限公司临猗分公司 | Methanol production process |
| CN101575540A (en) * | 2009-06-01 | 2009-11-11 | 中国科学院理化技术研究所 | Method for simultaneously producing liquefied natural gas and methanol |
| CN203229501U (en) * | 2013-03-04 | 2013-10-09 | 西安四联能源科技有限公司 | Device for preparing liquid natural gas from coke oven gas |
| CN103588221A (en) * | 2013-11-16 | 2014-02-19 | 山西阳煤丰喜肥业(集团)有限责任公司 | Method and device for co-production of synthetic ammonia and LNC (liquefied natural gas) by coke gas |
| CN105152864A (en) * | 2015-07-31 | 2015-12-16 | 赛鼎工程有限公司 | Technology for producing low carbon alcohol as well as by-product natural gas and liquefied ammonia from coke oven gas and synthetic gas |
| CN105066585A (en) * | 2015-08-20 | 2015-11-18 | 上海尧兴投资管理有限公司 | Purifying and separating device and method for synthesis gas |
Non-Patent Citations (1)
| Title |
|---|
| 《化工百科全书》编辑委员会: "《化工百科全书》", 31 March 1993, 化学工业出版社 * |
Cited By (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106811238A (en) * | 2017-01-06 | 2017-06-09 | 河北中翔能源有限公司 | A kind of process of preparing LNG from coke oven tail gas and hydrogen rich off gas liquefied ammonia |
| CN107215848A (en) * | 2017-06-09 | 2017-09-29 | 杨皓 | A kind of carbon black tail gas and calcium carbide stove exhaust combined production of ammonia alcohol synthesis gas process |
| CN107235473A (en) * | 2017-06-09 | 2017-10-10 | 杨皓 | A kind of carbon black tail gas and coke oven tail gas combined production of ammonia alcohol synthesis gas process |
| CN107244651A (en) * | 2017-06-09 | 2017-10-13 | 杨皓 | A kind of blast furnace tail gas and coke oven tail gas combined production of ammonia alcohol synthesis gas process |
| CN107267706A (en) * | 2017-07-06 | 2017-10-20 | 中冶华天南京工程技术有限公司 | Coal gas of converter cooling system and its cooling means |
| CN109206295A (en) * | 2018-09-17 | 2019-01-15 | 陕西黑猫焦化股份有限公司 | A kind of synthesis ammonolysis gassing matches the method and system of coke-stove gas methanol |
| CN109595878A (en) * | 2018-12-10 | 2019-04-09 | 内蒙古博大实地化学有限公司 | A method of synthesis ammonia, urea co-production liquid CO 2 |
| CN111676069A (en) * | 2020-06-18 | 2020-09-18 | 中冶西北工程技术有限公司 | Coke oven gas purification system |
| CN111676069B (en) * | 2020-06-18 | 2021-05-04 | 中冶西北工程技术有限公司 | Coke oven gas purification system |
| CN112850645A (en) * | 2021-02-08 | 2021-05-28 | 赛鼎工程有限公司 | System and method for preparing synthetic ammonia by deeply purifying coke oven gas |
| CN112850645B (en) * | 2021-02-08 | 2022-09-06 | 赛鼎工程有限公司 | System and method for preparing synthetic ammonia by deeply purifying coke oven gas |
Also Published As
| Publication number | Publication date |
|---|---|
| CN105861086B (en) | 2019-04-26 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN105861086A (en) | Process method for co-producing liquefied natural gas, methanol and liquid ammonia by using gasified coal gas and coke oven gas | |
| KR101304652B1 (en) | Method for simultaneously producing hydrogen and carbon monoxide | |
| CN104449920B (en) | The method utilizing coke-stove gas and blast furnace gas Joint Production natural gas with liquefied ammonia | |
| US20220152552A1 (en) | Method for purifying biogas through membranes at negative temperatures | |
| US10302357B2 (en) | Process and apparatus for the production of CO and CO2 | |
| KR101265916B1 (en) | cryogenic separation of synthesis gas | |
| US8636922B2 (en) | Process for recovering hydrogen and carbon dioxide from a syngas stream | |
| US11525628B2 (en) | Process for producing biomethane from a biogas stream, comprising solidification of the impurities | |
| CN102112391B (en) | Process and apparatus for generating and purifying syngas | |
| CN105018164A (en) | Method for co-producing liquefied natural gas and urea by means of coke oven gas and converter gas | |
| CN105293436A (en) | Process for preparation of metallurgical reduction gas and co-production of liquefied natural gas through coke gas | |
| CN107399737B (en) | Preparation method of high-pressure gas-phase carbon dioxide for high-pressure pulverized coal gasification | |
| CN210560161U (en) | Fischer-Tropsch synthesis tail gas recycling device | |
| CN205774370U (en) | System for coproduction of liquefied natural gas, methanol and liquid ammonia by utilizing gasified coal gas and coke oven gas | |
| CN117685697A (en) | System and process for preparing green low-carbon methanol and co-producing LNG (liquefied Natural gas) from coke oven gas | |
| CN108431184B (en) | Method for preparing natural gas at gas pressure reduction station to produce Liquid Natural Gas (LNG) | |
| CN107311173B (en) | Preparation method of high-pressure gas-phase carbon dioxide for pulverized coal gasification unit | |
| CN209052640U (en) | It is a kind of to utilize coke-stove gas synthesis of methanol with joint production LNG, richness H2Device | |
| CN113061475B (en) | Liquefaction process method and device capable of adjusting carbon dioxide concentration and separating carbon dioxide from critical methane | |
| US20070245630A1 (en) | Method for generating carbon monoxide from synthesis gas | |
| US12109527B2 (en) | Process and apparatus for the separation of two gaseous streams each containing carbon monoxide, hydrogen and at least one acid gas | |
| CN212316051U (en) | Poly-generation device for producing natural gas by using underground gasified gas | |
| CN104151202B (en) | A kind of process for separation and purification of urea | |
| CN108826830B (en) | Intermediate feeding coke oven gas recovery system utilizing liquefied natural gas cold energy | |
| CN109028757B (en) | Tower top feeding coke oven gas recovery system utilizing liquefied natural gas cold energy |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |