CN108409531A - Utilize tail of semi coke production methanol, natural gas, the system and method for synthesizing ammonia - Google Patents
Utilize tail of semi coke production methanol, natural gas, the system and method for synthesizing ammonia Download PDFInfo
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- CN108409531A CN108409531A CN201810424895.XA CN201810424895A CN108409531A CN 108409531 A CN108409531 A CN 108409531A CN 201810424895 A CN201810424895 A CN 201810424895A CN 108409531 A CN108409531 A CN 108409531A
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- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 title claims abstract description 282
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 title claims abstract description 211
- 239000000571 coke Substances 0.000 title claims abstract description 95
- 229910021529 ammonia Inorganic materials 0.000 title claims abstract description 94
- 238000000034 method Methods 0.000 title claims abstract description 49
- 230000002194 synthesizing effect Effects 0.000 title claims abstract description 21
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 title claims description 41
- 238000004519 manufacturing process Methods 0.000 title claims description 22
- 239000003345 natural gas Substances 0.000 title description 3
- 239000007789 gas Substances 0.000 claims abstract description 145
- 239000003949 liquefied natural gas Substances 0.000 claims abstract description 109
- 230000015572 biosynthetic process Effects 0.000 claims abstract description 101
- 238000003786 synthesis reaction Methods 0.000 claims abstract description 101
- 238000000926 separation method Methods 0.000 claims abstract description 55
- 238000005261 decarburization Methods 0.000 claims abstract description 40
- 230000008569 process Effects 0.000 claims abstract description 17
- 238000002203 pretreatment Methods 0.000 claims abstract description 9
- 238000004176 ammonification Methods 0.000 claims abstract description 5
- 230000006835 compression Effects 0.000 claims description 50
- 238000007906 compression Methods 0.000 claims description 50
- 238000006243 chemical reaction Methods 0.000 claims description 32
- 229930195733 hydrocarbon Natural products 0.000 claims description 30
- 150000002430 hydrocarbons Chemical class 0.000 claims description 30
- 239000004215 Carbon black (E152) Substances 0.000 claims description 22
- 239000000428 dust Substances 0.000 claims description 19
- 238000001914 filtration Methods 0.000 claims description 19
- UCKMPCXJQFINFW-UHFFFAOYSA-N Sulphide Chemical compound [S-2] UCKMPCXJQFINFW-UHFFFAOYSA-N 0.000 claims description 17
- 238000006477 desulfuration reaction Methods 0.000 claims description 15
- 230000023556 desulfurization Effects 0.000 claims description 15
- 238000009434 installation Methods 0.000 claims description 15
- 229920002521 macromolecule Polymers 0.000 claims description 15
- 239000007788 liquid Substances 0.000 claims description 14
- 238000000746 purification Methods 0.000 claims description 11
- 239000012535 impurity Substances 0.000 claims description 9
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 8
- 238000012545 processing Methods 0.000 claims description 7
- 238000005915 ammonolysis reaction Methods 0.000 claims description 6
- 238000007710 freezing Methods 0.000 claims description 4
- 230000008014 freezing Effects 0.000 claims description 4
- 230000008676 import Effects 0.000 claims description 4
- 238000001816 cooling Methods 0.000 claims description 3
- 239000003610 charcoal Substances 0.000 claims description 2
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 abstract description 6
- 229910052757 nitrogen Inorganic materials 0.000 abstract description 3
- 239000000126 substance Substances 0.000 abstract description 3
- 239000002994 raw material Substances 0.000 abstract 1
- 201000003478 cholangiolocellular carcinoma Diseases 0.000 description 30
- 229910002092 carbon dioxide Inorganic materials 0.000 description 28
- 239000000047 product Substances 0.000 description 19
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 6
- 238000010586 diagram Methods 0.000 description 6
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 5
- 230000008859 change Effects 0.000 description 4
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 3
- 229910002091 carbon monoxide Inorganic materials 0.000 description 3
- 229910052739 hydrogen Inorganic materials 0.000 description 3
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 2
- UFWIBTONFRDIAS-UHFFFAOYSA-N Naphthalene Chemical compound C1=CC=CC2=CC=CC=C21 UFWIBTONFRDIAS-UHFFFAOYSA-N 0.000 description 2
- 230000008901 benefit Effects 0.000 description 2
- 239000003054 catalyst Substances 0.000 description 2
- 238000011109 contamination Methods 0.000 description 2
- 238000005262 decarbonization Methods 0.000 description 2
- 238000013461 design Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 238000003912 environmental pollution Methods 0.000 description 2
- 239000000446 fuel Substances 0.000 description 2
- 239000001257 hydrogen Substances 0.000 description 2
- 229910000069 nitrogen hydride Inorganic materials 0.000 description 2
- 125000001741 organic sulfur group Chemical group 0.000 description 2
- 231100000572 poisoning Toxicity 0.000 description 2
- 230000000607 poisoning effect Effects 0.000 description 2
- 230000000717 retained effect Effects 0.000 description 2
- 238000003860 storage Methods 0.000 description 2
- 229910052717 sulfur Inorganic materials 0.000 description 2
- 239000011593 sulfur Substances 0.000 description 2
- 239000002699 waste material Substances 0.000 description 2
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 1
- -1 Methyl methanol Chemical compound 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 150000001335 aliphatic alkanes Chemical class 0.000 description 1
- 238000013459 approach Methods 0.000 description 1
- 150000001555 benzenes Chemical class 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 238000001311 chemical methods and process Methods 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 239000008246 gaseous mixture Substances 0.000 description 1
- XLYOFNOQVPJJNP-ZSJDYOACSA-N heavy water Substances [2H]O[2H] XLYOFNOQVPJJNP-ZSJDYOACSA-N 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 238000010248 power generation Methods 0.000 description 1
- 238000007781 pre-processing Methods 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
Classifications
-
- 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
- C07C29/152—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 characterised by the reactor used
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01C—AMMONIA; CYANOGEN; COMPOUNDS THEREOF
- C01C1/00—Ammonia; Compounds thereof
- C01C1/02—Preparation, purification or separation of ammonia
- C01C1/04—Preparation of ammonia by synthesis in the gas phase
-
- 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
Abstract
The present invention provides a kind of using tail of semi coke co-producing methanol, liquefied natural gas (LNG), the system for synthesizing ammonia, includes gas pretreatment unit, converter unit, decarburization unit, methanol-fueled CLC and rectification cell, methanation unit, cryogenic separation unit and the synthesis ammonia unit being sequentially connected by pipeline.Above system is used to utilize tail of semi coke co-producing methanol, liquefied natural gas, the method for synthesizing ammonia, including gas pre-treatment step, shift step, decarbonation process, methanol-fueled CLC and rectification step, methanation step, cryogenic separation step and synthesis ammonia step the present invention also provides a kind of.The tail of semi coke that the present invention is high using nitrogen content, calorific value is low is raw material, by H therein2、CO、CO2And N2It is converted to methanol, liquefied natural gas (LNG), synthesis ammonification chemical product.
Description
Technical field
The present invention relates to chemical technology fields, and tail of semi coke co-producing methanol, liquefaction are utilized in particular to a kind of
Natural gas (LNG), the system and method for synthesizing ammonia.
Background technology
As China's semi-coke industry continues to develop, a large amount of tail of semi coke is produced in semi-coke production process, this part
Tail of semi coke never has good method and is efficiently used.It is primarily due to tail of semi coke N2Too high levels, about 50%, H2
Content about 24%, CO contents about 10%, CH4Content about 5%, other are hydro carbons and impurity, and calorific value is only 6100~8400kJ/
Nm3, this tail of semi coke should not be used as domestic gas, usually only directly burn as conventional fuel.
The semi-coke annual output in China is up to 50,000,000 tons or more, with 1 ton of semi-coke by-product 700Nm of every production3Tail of semi coke
It is calculated, the total amount that China produces tail of semi coke per year is up to 35,000,000,000 Nm3More than, the tail of semi coke direct emission of such flood tide
It to air or directly burns, not only results in the serious waste of resource, also allow the resource that can bring profit to enterprise by unrestrained in vain
Expense is fallen, and huge pollution can be caused to atmospheric environment.
Therefore as rationally how utilized tail of semi coke resource, this kind of semi-coke enterprise is solved while bringing more preferable profit for enterprise
Problem of environmental pollution, be badly in need of developing a kind of association system and method.
Invention content
Tail of semi coke co-producing methanol, liquefied natural gas (LNG), synthesis are utilized the purpose of the present invention is to provide a kind of
The system and method for ammonia, or provide a kind of system using tail of semi coke co-producing methanol and liquefied natural gas (LNG) and
Method, or a kind of system and method using tail of semi coke Joint Production liquefied natural gas (LNG) and synthesis ammonia is provided.
H in tail of semi coke2、CO、CH4Methanol, liquefied natural gas and synthesis ammonia or methanol and liquefaction day are synthesized by chemical process
The large chemical products such as right gas (LNG) or liquefied natural gas (LNG) and synthesis ammonia, bring more high profit, simultaneously for enterprise
Solve the problem of environmental pollution of this kind of semi-coke enterprise.
To solve the above-mentioned problems, the present invention provides following technical schemes：
A kind of system using tail of semi coke co-producing methanol, liquefied natural gas (LNG) and synthesis ammonia, including be used for
Tail of semi coke is pre-processed to obtain without tar, sulfide, the gas pretreatment unit of macromolecule hydro carbons, gas pretreatment unit
Including dust removal by filtration device, the first compression set, de-heavy hydrocarbon apparatus and the dry desulfurization device being sequentially connected in series；System further includes
Converter unit, converter unit are used to adjust the H in gas2Content；System further includes decarburization unit, and decarburization unit is for removing gas
Most of CO in body2；System further includes methanol-fueled CLC and rectification cell, and methanol-fueled CLC and rectification cell include being sequentially connected in series
Second compression set, methanol synthesizer and methanol rectifying system；System further includes methanation unit；System further includes deep cooling
Separative element, cryogenic separation unit include the purification devices being sequentially connected in series and liquefaction separation device；System further includes synthesis ammonia list
Member, synthesis ammonia unit includes the third compression set, synthetic ammonia installation and ammonia refrigerating plant being sequentially connected in series；The gas pretreatment
Unit, converter unit, decarburization unit, methanol-fueled CLC and rectification cell, methanation unit, cryogenic separation unit and synthesis ammonia unit
It is sequentially connected by pipeline.
Further, system can also form a kind of system only producing methanol and liquefied natural gas (LNG), do not include and close
Ammonification unit retains other units.That is, offer is a kind of to utilize tail of semi coke co-producing methanol and liquefied natural gas
(LNG) system, including be used to pre-process to obtain without tar, sulfide by tail of semi coke, the gas of macromolecule hydro carbons is located in advance
Unit is managed, gas pretreatment unit includes the dust removal by filtration device being sequentially connected in series, the first compression set, de-heavy hydrocarbon apparatus and does
Method desulfurizer；System further includes converter unit, and converter unit is used to adjust the H in gas2Content；System further includes decarburization list
Member, decarburization unit are used to remove most of CO in gas2；System further includes methanol-fueled CLC and rectification cell, methanol-fueled CLC and
Rectification cell includes the second compression set, methanol synthesizer and the methanol rectifying system being sequentially connected in series；System further includes methane
Change unit；System further includes cryogenic separation unit, and cryogenic separation unit includes the purification devices being sequentially connected in series and liquefaction separation dress
It sets；The gas pretreatment unit, converter unit, decarburization unit, methanol-fueled CLC and rectification cell, methanation unit and deep cooling
Separative element is sequentially connected by pipeline.
Further, system also provides a kind of only production liquefied natural gas (LNG) and the system for synthesizing ammonia, does not include methanol
Synthesis and rectification cell.Decarburization unit is directly connect with methanation unit, other are retained.That is, providing a kind of using blue
The system that charcoal combined tail gas produces liquefied natural gas (LNG) and synthesizes ammonia, including be used to pre-process tail of semi coke and be free of
Tar, sulfide, the gas pretreatment unit of macromolecule hydro carbons, gas pretreatment unit include the dust removal by filtration dress being sequentially connected in series
It sets, the first compression set, de-heavy hydrocarbon apparatus and dry desulfurization device；System further includes converter unit, and converter unit is for adjusting
H in gas2Content；System further includes decarburization unit, and decarburization unit is used to remove most of CO in gas2；System further includes
Methanation unit；System further includes cryogenic separation unit, and cryogenic separation unit includes the purification devices being sequentially connected in series and liquefaction point
From device；System further include synthesis ammonia unit, synthesis ammonia unit include the third compression set being sequentially connected in series, synthetic ammonia installation and
Ammonia refrigerating plant；The gas pretreatment unit, converter unit, decarburization unit, methanation unit, cryogenic separation unit and synthesis
Ammonia unit is sequentially connected by pipeline.
Preferably, above system further includes the bypass connecting line with valve, and the both ends for bypassing connecting line are connected to change
Change the import of unit and the outlet of converter unit.
Tail of semi coke co-producing methanol, liquefied natural gas (LNG), the side for synthesizing ammonia are utilized the present invention also provides a kind of
Method uses the above-mentioned system using tail of semi coke co-producing methanol, liquefied natural gas (LNG), synthesis ammonia, including walks as follows
Suddenly：
Gas pre-treatment step：Tail of semi coke enters filtering dust collecting device, after after the supercharging of the first compression set, through de- weight
Hydrocarbon device removes macromolecule impurity, then removes sulfide through dry desulfurization device；
Shift step：A part for tail of semi coke enters converting means after preprocessed step, by transformationreation by portion
Part CO in point tail of semi coke is reacted with vapor to be converted into H2；
Decarbonation process：Enter decarburization unit after transformed processing, removes CO therein2Afterwards, synthesis gas is obtained；
Methanol-fueled CLC and rectification step：Synthesis gas is after the supercharging of the second compression set, into methanol synthesizer, synthesis gas
H2With CO and CO2Reaction generates crude carbinol, and crude carbinol enters methanol rectification and is further separated out refined methanol product；
Methanation step：The tail gas that methanol reacts in methanol-fueled CLC and rectification step enters methanation unit, methanol-fueled exhaust
In H2With CO and CO2Further reaction generates methane, makes the CH in methanol-fueled exhaust4Content increases；
Cryogenic separation step：The purified device of the later gas of methanation removes CO2And water, remaining gas are N2、H2、
CH4, then through liquefaction separation device isolate liquid CH4, i.e. liquefied natural gas；
Synthesize ammonia step：Through remaining richness N in cryogenic separation step2With rich H2It is mixed into the conjunction of production synthesis ammonia in proportion
At gas, synthesis gas enters synthesis ammonia unit, and after the compression of third compression set, synthesis ammonia, attached ammonia are generated through synthetic ammonia installation
Refrigerating plant provides cold, finally obtains liquid synthesis ammonolysis product.
The present invention also provides a kind of methods using tail of semi coke co-producing methanol and liquefied natural gas, use
State the system using tail of semi coke co-producing methanol and liquefied natural gas (LNG), which is characterized in that include the following steps：
Gas pre-treatment step：Tail of semi coke enters filtering dust collecting device, after after the supercharging of the first compression set, through de- weight
Hydrocarbon device removes macromolecule impurity, then removes sulfide through dry desulfurization device；
Shift step：A part for tail of semi coke enters converting means after preprocessed step, by transformationreation by portion
Part CO in point tail of semi coke is reacted with vapor to be converted into H2；
Decarbonation process：Enter decarburization unit after transformed processing, removes CO therein2Afterwards, synthesis gas is obtained；
Methanol-fueled CLC and rectification step：Synthesis gas is after the supercharging of the second compression set, into methanol synthesizer, synthesis gas
H2With CO and CO2Reaction generates crude carbinol, and crude carbinol enters methanol rectification and is further separated out refined methanol product；
Methanation step：The tail gas that methanol reacts in methanol-fueled CLC and rectification step enters methanation unit, methanol-fueled exhaust
In H2With CO and CO2Further reaction generates methane, makes the CH in methanol-fueled exhaust4Content increases；
Cryogenic separation step：The purified device of the later gas of methanation removes CO2And water, remaining gas are N2、H2、
CH4, then through liquefaction separation device isolate liquid CH4, i.e. liquefied natural gas.
The present invention also provides a kind of methods using tail of semi coke Joint Production liquefied natural gas and synthesis ammonia, use
The above-mentioned system using tail of semi coke Joint Production liquefied natural gas (LNG) and synthesis ammonia includes the following steps：
Gas pre-treatment step：Tail of semi coke enters filtering dust collecting device, after after the supercharging of the first compression set, through de- weight
Hydrocarbon device removes macromolecule impurity, then removes sulfide through dry desulfurization device；
Shift step：A part for tail of semi coke enters converting means after preprocessed step, by transformationreation by portion
Part CO in point tail of semi coke is reacted with vapor to be converted into H2；
Decarbonation process：Enter decarburization unit after transformed processing, removes CO therein2Afterwards, synthesis gas is obtained；
Methanation step：Synthesis gas enters methanation unit after decarburization, the H in methanol-fueled exhaust2With CO and CO2It is further anti-
Methane should be generated, the CH in methanol-fueled exhaust is made4Content increases；
Cryogenic separation step：The purified device of the later gas of methanation removes CO2And water, remaining gas are N2、H2、
CH4, then through liquefaction separation device isolate liquid CH4, i.e. liquefied natural gas；
Synthesize ammonia step：Through remaining richness N in cryogenic separation step2With rich H2It is mixed into the conjunction of production synthesis ammonia in proportion
At gas, synthesis gas enters synthesis ammonia unit, and after the compression of third compression set, synthesis ammonia, attached ammonia are generated through synthetic ammonia installation
Refrigerating plant provides cold, finally obtains liquid synthesis ammonolysis product.
The present invention is reacted with vapor to be converted into H using converter unit CO2Depth adjustability, in adjustable gas
H2/CO.And then it is needed to adjust whole system methanol, liquefied natural gas (LNG), the yield for synthesizing ammonia according to market；Or methanol,
The yield of liquefied natural gas (LNG)；Or liquefied natural gas (LNG), the yield for synthesizing ammonia.
Further, the present invention takes full advantage of the N of tail of semi coke2With CO difficulty stalling characteristics, not before methanol-fueled CLC
Sequence unit carries out N2Removing, but by methanol device and methanation device CO be converted to methanol and (or) after methane,
Realize N2Separation, the sequence of system flow is reasonably scheduled so that the function of each device is achieved, while in each device
In abundant recovery system energy, optimize technological process, and reduce investment and energy consumption.
Description of the drawings
It, below will be to required use in embodiment in order to illustrate more clearly of the technical solution of embodiment of the present invention
Attached drawing be briefly described, it should be understood that the following drawings illustrates only certain embodiments of the present invention, therefore is not to be seen as
It is the restriction to range, it for those of ordinary skill in the art, without creative efforts, can be with root
Other relevant attached drawings are obtained according to these attached drawings.
Fig. 1 is the utilization tail of semi coke co-producing methanol, liquefied natural gas (LNG), synthesis of the offer of the embodiment of the present invention 1
The schematic diagram of the system of ammonia.
Fig. 2 is the utilization tail of semi coke co-producing methanol, liquefied natural gas (LNG), synthesis of the offer of the embodiment of the present invention 1
The flow diagram of ammonia.
Fig. 3 is that utilization tail of semi coke co-producing methanol, the liquefied natural gas (LNG) that the embodiment of the present invention 2 provides are
The schematic diagram of system.
Fig. 4 is the stream of the utilization tail of semi coke co-producing methanol of the offer of the embodiment of the present invention 2, liquefied natural gas (LNG)
Journey schematic diagram.
Fig. 5 is utilization tail of semi coke Joint Production liquefied natural gas (LNG), the synthesis ammonia that the embodiment of the present invention 2 provides
The schematic diagram of system.
Fig. 6 is utilization tail of semi coke Joint Production liquefied natural gas (LNG), the synthesis ammonia that the embodiment of the present invention 2 provides
Flow diagram.
Icon：100- gas pretreatment units；200- converter units；300- decarburization units；400- methanol-fueled CLCs and rectifying
Unit；500- methanation units；600- cryogenic separation units；700- synthesizes ammonia unit；110- dust removal by filtration devices；120- first
Compression set；130- de-heavy hydrocarbon apparatus；140- fine de-sulfur devices；The second compression sets of 410-；420- methanol synthesizers；430-
Methanol rectifying system；610- purification devices；620- liquefaction separation devices；710- third compression sets；720- synthetic ammonia installations；
730- ammonia refrigerating plants.
Specific implementation mode
To keep the purpose, technical scheme and advantage of embodiment of the present invention clearer, implement below in conjunction with the present invention
The technical solution in embodiment of the present invention is clearly and completely described in attached drawing in mode, it is clear that described reality
It is a part of embodiment of the present invention to apply mode only, rather than whole embodiments.Based on the embodiment in the present invention,
The every other embodiment that those of ordinary skill in the art are obtained without creative efforts belongs to this
Invent the range of protection.Therefore, the detailed description of the embodiments of the present invention to providing in the accompanying drawings is not intended to limit below
The range of claimed invention processed, but it is merely representative of the selected embodiment of the present invention.
In the description of the present invention, it is to be understood that, term " first ", " second ", " third " are used for description purposes only,
It is not understood to indicate or imply relative importance or implicitly indicates the quantity of indicated technical characteristic.It limits as a result,
There is the feature of " first ", " second ", " third " to can explicitly or implicitly include one or more this feature.In this hair
In bright description, the meaning of " plurality " is two or more, unless otherwise specifically defined.
In recent years, the continuous development of semi-coke industry, the approach that tail of semi coke utilizes continuously emerges.Present inventor
It was found that containing useful N in tail of semi coke2、H2, CO and CH4, GAS QUALITY is although bad, but its yield is huge, however many works
These gases are directly made fuel emptying by factory, cause serious waste, also cause the pollution of environment；Or combustion power generation, warp
Help inefficiencies.
As shown in Figure 1, the embodiment of the present invention 1 it is a kind of using tail of semi coke co-producing methanol, liquefied natural gas (LNG),
The system for synthesizing ammonia, including be used to pre-process to obtain without tar, sulfide by tail of semi coke, the gas of macromolecule hydro carbons is located in advance
Unit 100 is managed, gas pretreatment unit 100 includes passing sequentially through the dust removal by filtration device 110 of placed in series, for filtering semi-coke
The particulate contaminations such as the dust in tail gas；First compression set 120 is subsequently located for being compressed to tail of semi coke for system
Reason provides pressure；De-heavy hydrocarbon apparatus 130, macromolecule heavy hydrocarbon and benzene homologues for removing tail of semi coke etc.；Dry desulfurization device
140, the sulfide for removing tail of semi coke, to avoid the catalyst poisoning of subsequent conversion unit.
A pretreated tail of semi coke part is sent by pipeline to converter unit 200, converter unit 200 occur CO and
H2O reactions generate CO2And H2Reaction meet follow-up methanation unit 500, methanol-fueled CLC and rectification cell 400 and synthesis ammonia list
The needs of first 700 pairs of hydrogen.It is in the chemical reaction that this element-converter unit 200 occurs：
CO+H2O=H2+CO2
Preferably, it is adjusted to outlet bypass connecting line by the aperture of control valve by the import of converter unit 200
Into the tolerance of converter unit 200, and then the tolerance of transformationreation is adjusted, is the H in gas2Meet the needs of subsequent cell.
Further, the conversion gas come out by converter unit 200 is sent by pipeline to decarburization unit 300, decarburization unit 300
For removing most of CO in gas2, make the CO in gas after decarburization2Content meets methanol-fueled CLC and rectifying 3% or so
The needs of unit 400.
Further, it is sent to methanol-fueled CLC and rectification cell 400 by pipeline by the decarbonization gas of decarburization unit 300, through
The pressure that two compression sets 410 are compressed to methanol-fueled CLC needs is sent by pipeline to methanol synthesizer 420, in this H2With CO and
CO2Reaction generates crude carbinol, and the chemical reaction occurred herein is as follows：
2H2+ CO=CH3OH
3H2+CO2=CH3OH+H2O
Crude carbinol is sent by pipeline to methanol rectifying system 430 after being cached by storage tank.Pass through the isolated smart first of rectifying
Alcohol product.
Further, the tail gas of methanol-fueled CLC is sent by pipeline to methanation unit 500 from methanol synthesizer 420,
This H2With CO and CO2Reaction generates richness CH4, the chemical reaction occurred herein is as follows：
3H2+ CO=CH4+H2O
4H2+CO2=CH4+2H2O
Further, rich CH4Gas is sent by pipeline to cryogenic separation unit 600, and cryogenic separation unit 600 includes going here and there successively
The purification devices 610 of connection, for removing rich CH4A small amount of CO in gas2And H2O, gas after purification enter liquefaction separation device 620.
Liquefied natural gas (LNG) product is isolated by cryogenic separation unit 600.
Further, cryogenic separation unit 600 also isolates N2With rich H2, a part of nitrogen emptying, remaining N2With rich H2It is mixed
Synthesis gas of the synthesis for producing synthesis ammonia, synthesis gas are compressed to the pressure of synthetic ammonia installation 720 by third compression set 710
Power, compressed synthesis gas reacts in synthetic ammonia installation 720 generates NH3, ammonia is liquefied ammonia by the freezing of ammonia refrigerating plant 730
Product.It is as follows in the reaction that this element occurs：
3H2+N2=2N H3
Further, the system that another only production methanol and liquefied natural gas (LNG) can also be formed in the present invention is (real
Apply example 2), embodiment 2 and embodiment 1 difference lies in：The system of embodiment 2 does not include synthesis ammonia unit 700, retains other lists
Member is shown in attached drawing 3.
Further, another only production liquefied natural gas (LNG) and the system for synthesizing ammonia can also be formed in the present invention
(embodiment 3), embodiment 3 and embodiment 1 difference lies in：The system of embodiment 3 does not include methanol-fueled CLC and rectification cell
400, decarburization unit 300 is directly connect with methanation unit 500, other units are retained.
Tail of semi coke co-producing methanol, liquefied natural gas (LNG), the side for synthesizing ammonia are utilized the present invention also provides a kind of
Method (see Fig. 2), tail of semi coke enter filtering dust collecting device 110, after through the first compression set 120 supercharging after, through de-heavy hydrocarbon apparatus
130 remove heavy hydrocarbon impurity, then remove sulfide through dry desulfurization device 140；Then a part for pretreated tail of semi coke
Into converter unit 200, the part CO in tail of semi coke is reacted with vapor to be converted into H by transformationreation2；Into de-
Carbon unit 300 removes major part CO therein2Afterwards, synthesis gas is obtained；Synthesis gas is pressurized through the second compression set 410, into first
Alcohol synthesizer 420, synthesis gas H2With CO and CO2Reaction generates crude carbinol, and it is further that crude carbinol enters methanol rectifying system 430
Isolate refined methanol product；The tail gas of methanol reaction enters methanation unit 500, the H in methanol-fueled exhaust2With CO and CO2Further
Reaction generates methane, makes the CH in methanol-fueled exhaust4Content increases；The purified device 610 of the later gas of methanation removes CO2With
Water, remaining gas are N2、H2、CH4, then through liquefaction separation device 620 isolate liquid CH4, i.e. liquefied natural gas.It is remaining
A part of N2Emptying, another part N2With rich H2It is mixed into the synthesis gas of production synthesis ammonia in proportion, synthesis gas enters synthesis ammonia list
Member 700 generates synthesis ammonia, attached ammonia refrigerating plant 730 is provided after the compression of third compression set 710 through synthetic ammonia installation 720
Cold finally obtains liquid synthesis ammonolysis product.
Further, the present invention utilizes converter unit 200, is reacted with vapor to be converted into H by CO2Depth it is adjustable
Whole property, the H in adjustable gas2/CO.And then it needs to adjust whole system methanol according to market, liquefied natural gas (LNG), close
The yield of ammonification；Or the yield of methanol, liquefied natural gas (LNG)；Or liquefied natural gas (LNG), the yield for synthesizing ammonia.
Further, another method for only producing methanol and liquefied natural gas (LNG) can also be provided in the present invention, seen
Fig. 4, this method do not include synthesis ammonia unit 700, protect compared with producing methanol, liquefied natural gas (LNG), synthesizing the method for ammonia
Other units are stayed to be connected by pipeline.
Further, another only production liquefied natural gas (LNG) and the method for synthesizing ammonia can also be provided in the present invention,
See Fig. 6, this method does not include methanol-fueled CLC and rectifying compared with producing methanol, liquefied natural gas (LNG), synthesizing the method for ammonia
Unit 400 retains other units and is connected by pipeline.
Specifically,
Embodiment 1
Shown in referring to Figures 1 and 2, tail of semi coke co-producing methanol, liquefied natural gas are utilized the present invention provides a kind of
(LNG), the system and method for synthesizing ammonia, the system include for pre-processing to obtain without tar, sulfide, high tail of semi coke
The gas pretreatment unit 100 of molecular hydrocarbon, gas pretreatment unit 100 include passing sequentially through the dust removal by filtration dress of placed in series
110 are set, for filtering the particulate contaminations such as the dust in tail of semi coke；First compression set 120, for being carried out to tail of semi coke
Compression, pressure is provided for system subsequent processing；De-heavy hydrocarbon apparatus 130, macromolecule heavy hydrocarbon and benzene series for removing tail of semi coke
Object etc.；Dry desulfurization device 140, the sulfide for removing tail of semi coke, to avoid the catalyst poisoning of subsequent conversion unit.
A part for pretreated tail of semi coke is sent by pipeline to converter unit 200, and CO and H occurs for converter unit 2002O reacts
Generate CO2And H2Reaction meet follow-up methanation unit 500, methanol-fueled CLC and rectification cell 400 and synthesis ammonia unit 700 it is right
The needs of hydrogen.Import by converter unit 200 is adjusted by the aperture of control valve into change to bypass connecting line is exported
The tolerance of unit 200 is changed, and then adjusts the tolerance of transformationreation, is the H in gas2Meet the needs of subsequent cell.By converting
The conversion gas that unit 200 comes out is sent by pipeline to decarburization unit 300, and decarburization unit 300 is used to remove the major part in gas
CO2, make the CO in gas after decarburization2Content meets the needs of methanol-fueled CLC and rectification cell 400 3% or so.By decarburization list
The decarbonization gas of member by pipeline send to methanol-fueled CLC and rectification cell 400 (including be sequentially connected the second compression set 410, first
Alcohol synthesizer 420 and methanol rectifying system 430), the pressure that methanol-fueled CLC needs are compressed to through the second compression set 410 passes through
Pipeline is sent to methanol synthesizer 420, and crude carbinol is sent by pipeline to methanol rectifying system 430 after being cached by storage tank, is passed through
The isolated refined methanol product of rectifying.The tail gas of methanol-fueled CLC is sent by pipeline to methanation unit from methanol synthesizer 420
500, in this H2With CO and CO2Reaction generates richness CH4, rich CH4Gas is sent by pipeline to cryogenic separation unit 600, cryogenic separation list
Member 600 includes the purification devices 610 being sequentially connected in series, for removing rich CH4A small amount of CO in gas2And H2O, gas after purification enter
Liquefaction separation device 620.Liquefied natural gas (LNG) product is isolated by cryogenic separation unit 600.Cryogenic separation unit 600
Also isolate N2With rich H2, a part of nitrogen emptying, remaining N2With rich H2It is mixed into the synthesis gas for producing synthesis ammonia, synthesis
Gas is compressed to the pressure of synthetic ammonia installation 720 by third compression set 710, and compressed synthesis gas is in synthetic ammonia installation 720
Middle reaction generates NH3, ammonia is liquefied ammonia product by the freezing of ammonia refrigerating plant 730.
See Fig. 2, tail of semi coke co-producing methanol, liquefied natural gas (LNG), synthesis are utilized the present invention also provides a kind of
The method of ammonia, the process employs above-mentioned system, this method includes tail of semi coke pre-treatment step, shift step, decarburization step
Suddenly, methanol-fueled CLC and rectification step, methanation step, cryogenic separation step, synthesis ammonia step, are finally reached Joint Production first
Alcohol, liquefied natural gas (LNG), the mesh for synthesizing ammonia.Specifically,
Gas pre-treatment step：Tail of semi coke enters filtering dust collecting device 110, and solid content is less than 10mg/Nm in gas3With
Under, it is pressurized to 0.8MpaG through the first compression set 120, removes heavy hydrocarbon impurity through de-heavy hydrocarbon apparatus 130, naphthalene is removed to 10mg/
Nm3Below, tar is removed to 10mg/Nm3Hereinafter, removing the H of wherein most through dry desulfurization device 140 again2S and organic sulfur
Deng, and by the total sulfur content (H in gas2S and organic sulfur summation) control 0.1ppm (V) below.It is pretreated by gas
Tail of semi coke enters shift step.
Shift step：Enter converter unit 200 by the pretreated part tail of semi coke of gas, converter unit occur CO and
H2O generates CO2And H2Reaction, the H in gas2/ CO ratios are 2.8 or so.Conversion gas enters decarbonation process.
Decarbonation process：Into decarburization unit 300, CO therein is removed2Afterwards, the content of the carbon dioxide in gas is made to exist
3% or so, obtain methyl methanol syngas；Methyl methanol syngas enters methanol-fueled CLC and rectification step.
Methanol-fueled CLC and rectification step：Synthesis gas is pressurized to 8.0MPaG through the second compression set 410, into methanol-fueled CLC
Device 420, synthesis gas H2With CO and CO2Reaction generates crude carbinol, crude carbinol concentration about 85%, and crude carbinol enters methanol rectification dress
It sets 430 and is further separated out refined methanol product.The tail gas of methanol reaction enters methanation step.
Methanation step：Methanol-fueled exhaust enters methanation device, the H in tail gas2With CO and CO2Further reaction generates first
Alkane makes the CH in methanol-fueled exhaust4Content increases, and the carbon monoxide in gas reacts completely, CO2Content is less than 50ppm or less.First
Gaseous mixture after alkanisation enters cryogenic separation step.
Cryogenic separation step：The purified device 610 of the later gas of methanation removes CO2And water, remaining gas are N2、
H2、CH4, then through liquefaction separation device 620 isolate liquid CH4, i.e. liquefied natural gas (LGN).Remaining a part of N2Emptying,
Another part part N2With rich H2It is mixed into the synthesis gas of production synthesis ammonia in proportion, synthesis gas enters synthesis ammonia step.
Synthesize ammonia step：Synthesis gas is compressed to 15.0MPaG through third compression set 710, is generated through synthetic ammonia installation 720
Ammonia, attached ammonia refrigerating plant 730 provide cold, finally obtain liquid synthesis ammonolysis product.
Embodiment 2
Further, see Fig. 3 and Fig. 4, the present invention can also provide it is another using tail of semi coke only produce methanol with
The system and method for liquefied natural gas (LNG), system do not include synthesis ammonia unit 700, retain other units and are connected by pipeline；
This method does not include synthesis ammonia step.The 1 identical figure of technique effect and embodiment of realization principle and generation, to briefly describe, this
Embodiment does not refer to place, can refer to corresponding contents in embodiment 1.
A kind of tail of semi coke of utilization that can also be obtained by above-mentioned design only produces methanol and liquefied natural gas (LNG)
System, requirement of the designer according to enterprise to product further adjust product structure by adjusting flow with reference to Fig. 3 and Fig. 4, only
The system for producing methanol and liquefied natural gas (LNG).
Embodiment 3
Further, see Fig. 5 and Fig. 6, can also provide another kind in the present invention only produces liquefaction day using tail of semi coke
Right gas (LNG) and the system and method for synthesizing ammonia, the system do not include methanol-fueled CLC and rectification cell 400, retain other units
It is connected by pipeline, this method does not include methanol-fueled CLC and rectification step.The technique effect and embodiment 1 of realization principle and generation
Identical figure, to briefly describe, the present embodiment does not refer to place, can refer to corresponding contents in embodiment 1.
A kind of utilization tail of semi coke of utilization that can also be obtained by above-mentioned design only produces liquefied natural gas (LNG) and closes
The system of ammonification, requirement of the designer according to enterprise to product further adjust product knot referring to figure 5 and figure 6 by adjusting flow
Structure, the system for only producing liquefied natural gas (LNG) and synthesizing ammonia.
The foregoing is merely the preferred embodiment of the present invention, are not intended to restrict the invention, for this field
For technical staff, the invention may be variously modified and varied.All within the spirits and principles of the present invention, any made by
Modification, equivalent replacement, improvement etc., should all be included in the protection scope of the present invention.
Claims (7)
1. it is a kind of utilize tail of semi coke co-producing methanol, liquefied natural gas and synthesize ammonia system, which is characterized in that including with
It pre-processes to obtain without tar, sulfide, the gas pretreatment unit of macromolecule hydro carbons in by tail of semi coke, the gas is located in advance
It includes the dust removal by filtration device being sequentially connected in series, the first compression set, de-heavy hydrocarbon apparatus and dry desulfurization device to manage unit；System
Further include converter unit, the converter unit is used to adjust the H in gas2Content；System further includes decarburization unit, the decarburization
Unit is used to remove most of CO in gas2；System further includes methanol-fueled CLC and rectification cell, the methanol-fueled CLC and rectifying
Unit includes the second compression set, methanol synthesizer and the methanol rectifying system being sequentially connected in series；System further includes methanation list
Member；System further includes cryogenic separation unit, and the cryogenic separation unit includes the purification devices being sequentially connected in series and liquefaction separation dress
It sets；System further include synthesis ammonia unit, the synthesis ammonia unit include the third compression set being sequentially connected in series, synthetic ammonia installation and
Ammonia refrigerating plant；The wherein described gas pretreatment unit, converter unit, decarburization unit, methanol-fueled CLC and rectification cell, methanation
Unit, cryogenic separation unit and synthesis ammonia unit are sequentially connected by pipeline.
2. a kind of system using tail of semi coke co-producing methanol and liquefied natural gas, which is characterized in that including be used for will be blue
Charcoal tail gas pre-processes to obtain without tar, sulfide, the gas pretreatment unit of macromolecule hydro carbons, the gas pretreatment unit
Including dust removal by filtration device, the first compression set, de-heavy hydrocarbon apparatus and the dry desulfurization device being sequentially connected in series；System further includes
Converter unit, the converter unit are used to adjust the H in gas2Content；System further includes decarburization unit, and the decarburization unit is used
In removing most of CO in gas2；System further includes methanol-fueled CLC and rectification cell, the methanol-fueled CLC and rectification cell packet
Include the second compression set, methanol synthesizer and the methanol rectifying system being sequentially connected in series；System further includes methanation unit；System
System further includes cryogenic separation unit, and the cryogenic separation unit includes the purification devices being sequentially connected in series and liquefaction separation device；Its
Described in gas pretreatment unit, converter unit, decarburization unit, methanol-fueled CLC and rectification cell, methanation unit and deep cooling point
It is sequentially connected by pipeline from unit.
3. it is a kind of utilize tail of semi coke Joint Production liquefied natural gas and synthesis ammonia system, which is characterized in that including be used for by
Tail of semi coke pre-processes to obtain without tar, sulfide, the gas pretreatment unit of macromolecule hydro carbons, and the gas pretreatment is single
Member includes dust removal by filtration device, the first compression set, de-heavy hydrocarbon apparatus and the dry desulfurization device being sequentially connected in series；System is also wrapped
Converter unit is included, the converter unit is used to adjust the H in gas2Content；System further includes decarburization unit, the decarburization unit
For removing most of CO in gas2；System further includes methanation unit；System further includes cryogenic separation unit, the depth
Cold separative element includes the purification devices being sequentially connected in series and liquefaction separation device；System further includes synthesis ammonia unit, the synthesis
Ammonia unit includes the third compression set, synthetic ammonia installation and ammonia refrigerating plant being sequentially connected in series；The wherein described gas pretreatment is single
Member, converter unit, decarburization unit, methanation unit, cryogenic separation unit and synthesis ammonia unit are sequentially connected by pipeline.
4. according to the system described in one of claim 1-3, further includes the bypass connecting line with valve, bypass connecting line
Both ends are connected to the import of converter unit and the outlet of converter unit.
5. a kind of use system according to claim 1 or 4 with natural using tail of semi coke co-producing methanol, liquefaction
Gas, the method for synthesizing ammonia, which is characterized in that include the following steps：
Gas pre-treatment step：Tail of semi coke enters filtering dust collecting device, after after the supercharging of the first compression set, filled through de- heavy hydrocarbon
Removing macromolecule impurity is set, then sulfide is removed through dry desulfurization device；
Shift step：Enter converting means after preprocessed step, by transformationreation by the part CO in the tail of semi coke of part
It is reacted with vapor to be converted into H2；
Decarbonation process：Enter decarburization unit after transformed processing, removes CO therein2Afterwards, synthesis gas is obtained；
Methanol-fueled CLC and rectification step：Synthesis gas is after the supercharging of the second compression set, into methanol synthesizer, synthesis gas H2With
CO and CO2Reaction generates crude carbinol, and crude carbinol enters methanol rectification and is further separated out refined methanol product；
Methanation step：The tail gas that methanol reacts in methanol-fueled CLC and rectification step enters methanation unit, the H in methanol-fueled exhaust2
With CO and CO2Further reaction generates methane, makes the CH in methanol-fueled exhaust4Content increases；
Cryogenic separation step：The purified device of the later gas of methanation removes CO2And water, remaining gas are N2、H2、CH4, then
Liquid CH is isolated through liquefaction separation device4, i.e. liquefied natural gas；
Synthesize ammonia step：Through remaining richness N in cryogenic separation step2With rich H2It is mixed into the synthesis gas of production synthesis ammonia in proportion,
Synthesis gas enters synthesis ammonia unit, and after the compression of third compression set, synthesis ammonia, attached ammonia freezing dress are generated through synthetic ammonia installation
Offer cold is provided, liquid synthesis ammonolysis product is finally obtained.
6. a kind of use system according to claim 2 or 4 with natural using tail of semi coke co-producing methanol and liquefaction
The method of gas, which is characterized in that include the following steps：
Gas pre-treatment step：Tail of semi coke enters filtering dust collecting device, after after the supercharging of the first compression set, filled through de- heavy hydrocarbon
Removing macromolecule impurity is set, then sulfide is removed through dry desulfurization device；
Shift step：Enter converting means after preprocessed step, by transformationreation by the part CO in the tail of semi coke of part
It is reacted with vapor to be converted into H2；
Decarbonation process：Enter decarburization unit after transformed processing, removes CO therein2Afterwards, synthesis gas is obtained；
Methanol-fueled CLC and rectification step：Synthesis gas is after the supercharging of the second compression set, into methanol synthesizer, synthesis gas H2With
CO and CO2Reaction generates crude carbinol, and crude carbinol enters methanol rectification and is further separated out refined methanol product；
Methanation step：The tail gas that methanol reacts in methanol-fueled CLC and rectification step enters methanation unit, the H in methanol-fueled exhaust2
With CO and CO2Further reaction generates methane, makes the CH in methanol-fueled exhaust4Content increases；
Cryogenic separation step：The purified device of the later gas of methanation removes CO2And water, remaining gas are N2、H2、CH4, then
Liquid CH is isolated through liquefaction separation device4, i.e. liquefied natural gas.
7. a kind of using system according to claim 3 or 4 to utilize tail of semi coke Joint Production liquefied natural gas and conjunction
The method of ammonification, which is characterized in that include the following steps：
Gas pre-treatment step：Tail of semi coke enters filtering dust collecting device, after after the supercharging of the first compression set, filled through de- heavy hydrocarbon
Removing macromolecule impurity is set, then sulfide is removed through dry desulfurization device；
Shift step：Enter converting means after preprocessed step, by transformationreation by the part CO in the tail of semi coke of part
It is reacted with vapor to be converted into H2；
Decarbonation process：Enter decarburization unit after transformed processing, removes CO therein2Afterwards, synthesis gas is obtained；
Methanation step：Synthesis gas enters methanation unit after decarburization, the H in methanol-fueled exhaust2With CO and CO2Further reaction life
At methane, make the CH in methanol-fueled exhaust4Content increases；
Cryogenic separation step：The purified device of the later gas of methanation removes CO2And water, remaining gas are N2、H2、CH4, then
Liquid CH is isolated through liquefaction separation device4, i.e. liquefied natural gas；
Synthesize ammonia step：Through remaining richness N in cryogenic separation step2With rich H2It is mixed into the synthesis gas of production synthesis ammonia in proportion,
Synthesis gas enters synthesis ammonia unit, and after the compression of third compression set, synthesis ammonia, attached ammonia freezing dress are generated through synthetic ammonia installation
Offer cold is provided, liquid synthesis ammonolysis product is finally obtained.
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109438181A (en) * | 2018-11-08 | 2019-03-08 | 鄂尔多斯市瀚博科技有限公司 | A method of methanol is produced using silicomanganese furnace exhaust gas |
| CN110078076A (en) * | 2019-04-21 | 2019-08-02 | 刘伟 | A kind of process of tail of semi coke classification sub-prime comprehensive utilization Poly-generation chemicals |
| CN114891546A (en) * | 2022-06-08 | 2022-08-12 | 佛燃能源集团股份有限公司 | System and method for preparing hydrogen and fuel-grade natural gas by using purge gas of synthetic ammonia |
Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102776042A (en) * | 2012-07-30 | 2012-11-14 | 西南化工研究设计院有限公司 | Method for producing liquefied natural gas (LNG) by using semi-coke tail gas |
| CN102924228A (en) * | 2012-11-28 | 2013-02-13 | 西南化工研究设计院有限公司 | Method for producing methanol from semi-coke furnace tail gas |
| CN103316563A (en) * | 2013-06-03 | 2013-09-25 | 浙江西子联合工程有限公司 | Desulfurization and purification device for semi-coke tail gas and usage method of same |
| JP2015007039A (en) * | 2013-06-18 | 2015-01-15 | 中国石油化工股▲ふん▼有限公司 | Method of co-producing methanol and synthetic natural gas by coke oven gas, and plant for achieving the same |
| CN104974810A (en) * | 2014-04-02 | 2015-10-14 | 石家庄新华能源环保科技股份有限公司 | Method for producing liquefied natural gas (LNG) from semi-coke exhaust and calcium carbide furnace gas |
| CN105296036A (en) * | 2015-12-03 | 2016-02-03 | 南京国昌化工科技有限公司 | Polygeneration method for synthesizing methanol, natural gas and ammonia |
| CN105733715A (en) * | 2014-12-11 | 2016-07-06 | 中国石油化工股份有限公司 | Process for synthesizing LNG (Liquefied Natural Gas) and coproducing liquid ammonia by using methanol purge gas |
| CN107365602A (en) * | 2017-07-18 | 2017-11-21 | 宝鸡市泰和石化工程有限公司 | Tail of semi coke polychotomy integrates after-treatment system and new technology |
-
2018
- 2018-05-07 CN CN201810424895.XA patent/CN108409531A/en active Pending
Patent Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102776042A (en) * | 2012-07-30 | 2012-11-14 | 西南化工研究设计院有限公司 | Method for producing liquefied natural gas (LNG) by using semi-coke tail gas |
| CN102924228A (en) * | 2012-11-28 | 2013-02-13 | 西南化工研究设计院有限公司 | Method for producing methanol from semi-coke furnace tail gas |
| CN103316563A (en) * | 2013-06-03 | 2013-09-25 | 浙江西子联合工程有限公司 | Desulfurization and purification device for semi-coke tail gas and usage method of same |
| JP2015007039A (en) * | 2013-06-18 | 2015-01-15 | 中国石油化工股▲ふん▼有限公司 | Method of co-producing methanol and synthetic natural gas by coke oven gas, and plant for achieving the same |
| CN104974810A (en) * | 2014-04-02 | 2015-10-14 | 石家庄新华能源环保科技股份有限公司 | Method for producing liquefied natural gas (LNG) from semi-coke exhaust and calcium carbide furnace gas |
| CN105733715A (en) * | 2014-12-11 | 2016-07-06 | 中国石油化工股份有限公司 | Process for synthesizing LNG (Liquefied Natural Gas) and coproducing liquid ammonia by using methanol purge gas |
| CN105296036A (en) * | 2015-12-03 | 2016-02-03 | 南京国昌化工科技有限公司 | Polygeneration method for synthesizing methanol, natural gas and ammonia |
| CN107365602A (en) * | 2017-07-18 | 2017-11-21 | 宝鸡市泰和石化工程有限公司 | Tail of semi coke polychotomy integrates after-treatment system and new technology |
Non-Patent Citations (1)
| Title |
|---|
| 亢玉红;李健;任国瑜;马亚军;: "兰炭尾气资源化利用技术途径" * |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109438181A (en) * | 2018-11-08 | 2019-03-08 | 鄂尔多斯市瀚博科技有限公司 | A method of methanol is produced using silicomanganese furnace exhaust gas |
| CN110078076A (en) * | 2019-04-21 | 2019-08-02 | 刘伟 | A kind of process of tail of semi coke classification sub-prime comprehensive utilization Poly-generation chemicals |
| CN114891546A (en) * | 2022-06-08 | 2022-08-12 | 佛燃能源集团股份有限公司 | System and method for preparing hydrogen and fuel-grade natural gas by using purge gas of synthetic ammonia |
| CN114891546B (en) * | 2022-06-08 | 2022-12-09 | 佛燃能源集团股份有限公司 | System and method for preparing hydrogen and fuel-grade natural gas by using purge gas of synthetic ammonia |
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