JP2015007039A5 - - Google Patents
Download PDFInfo
- Publication number
- JP2015007039A5 JP2015007039A5 JP2014125647A JP2014125647A JP2015007039A5 JP 2015007039 A5 JP2015007039 A5 JP 2015007039A5 JP 2014125647 A JP2014125647 A JP 2014125647A JP 2014125647 A JP2014125647 A JP 2014125647A JP 2015007039 A5 JP2015007039 A5 JP 2015007039A5
- Authority
- JP
- Japan
- Prior art keywords
- methane
- methane synthesis
- methanol
- synthesis
- reactor
- 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
- 238000003786 synthesis reaction Methods 0.000 claims 57
- OKKJLVBELUTLKV-UHFFFAOYSA-N methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 claims 50
- 230000015572 biosynthetic process Effects 0.000 claims 47
- 230000002194 synthesizing Effects 0.000 claims 47
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims 43
- 239000007789 gas Substances 0.000 claims 15
- 239000003054 catalyst Substances 0.000 claims 10
- OKTJSMMVPCPJKN-UHFFFAOYSA-N carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims 9
- 229910052799 carbon Inorganic materials 0.000 claims 9
- 239000000571 coke Substances 0.000 claims 7
- 230000003009 desulfurizing Effects 0.000 claims 4
- 229910052739 hydrogen Inorganic materials 0.000 claims 4
- 239000001257 hydrogen Substances 0.000 claims 4
- UFHFLCQGNIYNRP-UHFFFAOYSA-N hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims 4
- 239000003345 natural gas Substances 0.000 claims 4
- 238000006243 chemical reaction Methods 0.000 claims 3
- 238000007906 compression Methods 0.000 claims 3
- 238000006477 desulfuration reaction Methods 0.000 claims 3
- 238000000034 method Methods 0.000 claims 3
- 238000000926 separation method Methods 0.000 claims 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims 3
- UGFAIRIUMAVXCW-UHFFFAOYSA-N carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims 2
- 239000007795 chemical reaction product Substances 0.000 claims 2
- 239000003546 flue gas Substances 0.000 claims 2
- 239000000203 mixture Substances 0.000 claims 2
- 239000003949 liquefied natural gas Substances 0.000 claims 1
- 239000007788 liquid Substances 0.000 claims 1
- 238000004519 manufacturing process Methods 0.000 claims 1
Claims (24)
(1)少なくとも1種のコークス炉ガスを前処理する工程、
(2)前処理したコークス炉ガスに少なくとも1種の炭素含有ガスを加えることにより、水素/炭素比を調整する工程、
(3)生じる混合ガスを圧縮及び脱硫し、次にメタノール合成反応を実施する工程、
(4)生じるメタノール合成反応生成物を高メタノール流と低メタノール流とに分離する工程、
(5)低メタノール流を、直列につながれた2つ又は3つのメタン合成反応器中でのメタン合成反応に付す工程、
(6)生じるメタン合成反応生成物から水を分離することにより、合成天然ガスを生産する工程
を含む方法。 A method of simultaneously producing methanol and synthetic natural gas with coke oven gas, the method comprising:
(1) a step of pretreating at least one coke oven gas;
(2) adjusting the hydrogen / carbon ratio by adding at least one carbon-containing gas to the pretreated coke oven gas;
(3) compressing and desulfurizing the resulting mixed gas, and then performing a methanol synthesis reaction;
(4) separating the resulting methanol synthesis reaction product into a high methanol stream and a low methanol stream;
(5) subjecting the low methanol stream to a methane synthesis reaction in two or three methane synthesis reactors connected in series;
(6) A method comprising the step of producing synthetic natural gas by separating water from the resulting methane synthesis reaction product.
第1のメタン合成反応器では:少なくとも1種のNi系メタン合成触媒が充填され、入口温度が250〜350℃であり、圧力が1.0〜8.5MPaであり、空間速度が2000〜15000h−1であるという条件で稼働する、固定床反応器を使用し;
第2のメタン合成反応器では:少なくとも1種のNi系メタン合成触媒が充填され、入口温度が250〜350℃であり、圧力が0.8〜8.3MPaであり、空間速度が2000〜10000h−1であるという条件で稼働し;
第2のメタン合成反応器は、第1のメタン合成反応器の稼働温度よりも低い温度で稼働する、固定床反応器を使用することを特徴とする、請求項1に記載の方法。 Using two methane synthesis reactors,
In the first methane synthesis reactor: at least one Ni-based methane synthesis catalyst is charged, the inlet temperature is 250 to 350 ° C., the pressure is 1.0 to 8.5 MPa, and the space velocity is 2000 to 15000 h. Using a fixed bed reactor operating at -1 conditions;
In the second methane synthesis reactor: at least one Ni-based methane synthesis catalyst is charged, the inlet temperature is 250 to 350 ° C., the pressure is 0.8 to 8.3 MPa, and the space velocity is 2000 to 10,000 h. Run on condition of -1 ;
The method according to claim 1, characterized in that the second methane synthesis reactor uses a fixed bed reactor which operates at a temperature lower than the operating temperature of the first methane synthesis reactor .
第1のメタン合成反応器では:少なくとも1種のNi系メタン合成触媒が充填され、入口温度が250〜350℃であり、圧力が1.0〜8.5MPaであり、空間速度が2000〜15000h−1であるという条件で稼働する、固定床反応器を使用し;
第2のメタン合成反応器では:少なくとも1種のNi系メタン合成触媒が充填され、入口温度が250〜350℃であり、圧力が0.8〜8.3MPaであり、空間速度が2000〜10000h−1であるという条件で稼働する、固定床反応器を使用し;
第3のメタン合成反応器では:少なくとも1種のNi系メタン合成触媒が充填され、入口温度が250〜350℃であり、圧力が0.7〜8.2MPaであり、空間速度が2000〜10000h−1であるという条件で稼働する、固定床反応器を使用し;
第2のメタン合成反応器は、第1のメタン合成反応器の稼働温度よりも低い温度で稼働し;
第3のメタン合成反応器は、第2のメタン合成反応器の稼働温度よりも低い温度で稼働することを特徴とする、請求項1に記載の方法。 Using three methane synthesis reactors,
In the first methane synthesis reactor: at least one Ni-based methane synthesis catalyst is charged, the inlet temperature is 250 to 350 ° C., the pressure is 1.0 to 8.5 MPa, and the space velocity is 2000 to 15000 h. Using a fixed bed reactor operating at -1 conditions;
In the second methane synthesis reactor: at least one Ni-based methane synthesis catalyst is charged, the inlet temperature is 250 to 350 ° C., the pressure is 0.8 to 8.3 MPa, and the space velocity is 2000 to 10,000 h. Using a fixed bed reactor operating at -1 conditions;
In the third methane synthesis reactor: at least one Ni-based methane synthesis catalyst is charged, the inlet temperature is 250-350 ° C., the pressure is 0.7-8.2 MPa, and the space velocity is 2000-10000 h. Using a fixed bed reactor operating at -1 conditions;
The second methane synthesis reactor operates at a temperature lower than the operating temperature of the first methane synthesis reactor;
The method according to claim 1, wherein the third methane synthesis reactor is operated at a temperature lower than the operating temperature of the second methane synthesis reactor.
前記コークス炉ガス前処理ユニットの少なくとも1つの入口は、前記コーカーの少なくとも1つのコークス炉ガス出口と連通しており;
前記CO2捕捉ユニットの少なくとも1つの入口は、前記コーカーの少なくとも1つの煙道ガス出口と連通しており;
前記CO2捕捉ユニットの少なくとも1つの出口及び前記コークス炉ガス前処理ユニットの少なくとも1つの出口は、少なくとも1つの混合装置を介して、前記圧縮及び脱硫ユニットの少なくとも1つの入口と連通しており;
前記圧縮及び脱硫ユニットの少なくとも1つの出口は、前記メタノール合成ユニットの少なくとも1つの入口と連通しており;
前記メタノール合成ユニットの少なくとも1つの出口は、少なくとも1つの精製装置を介して、前記メタン合成ユニットの少なくとも1つの入口と連通しており;
前記メタン合成ユニットの少なくとも1つの出口は、場合により前記深冷分離ユニットの少なくとも1つの入口と連通している、プラント。 A plant for the simultaneous production of methanol and synthetic natural gas, wherein the plant is used in combination with at least one coker, wherein the plant comprises (1) at least one coke oven gas pretreatment unit, (2) at least one CO 2 capture unit, (3) at least one compression and desulfurization unit, (4) at least one methanol synthesis unit, (5) at least one methane synthesis unit, and (6) optionally at least one Including two cryogenic separation units;
At least one inlet of the coke oven gas pretreatment unit is in communication with at least one coke oven gas outlet of the coker;
At least one inlet of the CO 2 capture unit is in communication with at least one flue gas outlet of the coker;
At least one outlet of the CO 2 capture unit and at least one outlet of the coke oven gas pretreatment unit are in communication with at least one inlet of the compression and desulfurization unit via at least one mixing device;
At least one outlet of the compression and desulfurization unit is in communication with at least one inlet of the methanol synthesis unit;
At least one outlet of the methanol synthesis unit is in communication with at least one inlet of the methane synthesis unit via at least one purifier;
A plant, wherein at least one outlet of the methane synthesis unit is optionally in communication with at least one inlet of the cryogenic separation unit.
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
CN201310240935.2 | 2013-06-18 | ||
CN201310240935.2A CN104232195B (en) | 2013-06-18 | 2013-06-18 | Method for jointly producing methanol and synthetic natural gas by utilizing coke oven gas |
Publications (3)
Publication Number | Publication Date |
---|---|
JP2015007039A JP2015007039A (en) | 2015-01-15 |
JP2015007039A5 true JP2015007039A5 (en) | 2017-06-22 |
JP6347995B2 JP6347995B2 (en) | 2018-06-27 |
Family
ID=52221107
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
JP2014125647A Active JP6347995B2 (en) | 2013-06-18 | 2014-06-18 | Method for simultaneous production of methanol and synthetic natural gas with coke oven gas and plant for achieving the method |
Country Status (3)
Country | Link |
---|---|
JP (1) | JP6347995B2 (en) |
CN (1) | CN104232195B (en) |
UA (1) | UA118650C2 (en) |
Families Citing this family (16)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CN104418703B (en) * | 2013-09-04 | 2017-02-15 | 中国石油化工股份有限公司 | Serial methanol and methane synthesis process taking coke-oven gas as raw material |
CN104447196B (en) * | 2014-12-19 | 2016-03-30 | 北京宝塔三聚能源科技有限公司 | A kind of take coke(oven)gas as the technique of raw material combined production of methanol and methane |
JP6134347B2 (en) * | 2015-03-30 | 2017-05-24 | 積水化学工業株式会社 | Valuables generation method and apparatus |
CN105016297B (en) * | 2015-07-03 | 2017-09-19 | 赛鼎工程有限公司 | A kind of preparation method of synthesis gas |
CN105061142B (en) * | 2015-07-31 | 2018-02-06 | 赛鼎工程有限公司 | A kind of technique by coke-stove gas synthesis of low-carbon alcohol and by-product hydrogen |
FR3050206B1 (en) | 2016-04-15 | 2018-05-11 | Engie | HYDROGENATION DEVICE AND METHOD FOR PRODUCING METHANOL AND DEVICE AND METHOD FOR COGENERATION OF METHANOL AND SYNTHETIC METHANE |
CN106281519B (en) * | 2016-10-21 | 2021-09-14 | 山西高碳能源低碳化利用研究设计院有限公司 | Coke oven gas methanation device with membrane separator and method |
CN106753628A (en) * | 2017-01-19 | 2017-05-31 | 上海华西化工科技有限公司 | A kind of method and device of coke-stove gas LNG combined production of methanol |
CN108101749A (en) * | 2017-07-19 | 2018-06-01 | 湖北申昙环保新材料有限公司 | The method that coke-stove gas produces methanol |
CN108409531A (en) * | 2018-05-07 | 2018-08-17 | 陈峰华 | Utilize tail of semi coke production methanol, natural gas, the system and method for synthesizing ammonia |
CN110182761B (en) * | 2019-05-05 | 2023-03-21 | 杨皓 | Process for preparing synthesis gas by converting coke-oven gas |
WO2021045101A1 (en) * | 2019-09-03 | 2021-03-11 | 国立大学法人静岡大学 | Methane producing method and production system |
CN112742336B (en) * | 2020-11-27 | 2022-12-02 | 中国煤层气集团有限公司 | Hydrocarbon gasification reactor |
CN113150849A (en) * | 2021-05-26 | 2021-07-23 | 杨皓 | Improved process for producing LNG (liquefied Natural gas) from coke-oven gas |
CN114773154A (en) * | 2022-06-09 | 2022-07-22 | 迁安市乾元科技有限公司 | Method for co-producing LNG and methanol by using coke oven gas |
CN115888313B (en) * | 2022-11-11 | 2024-05-31 | 西南化工研究设计院有限公司 | Energy production regulating process for preparing fuel cell hydrogen and pipeline natural gas from coke oven gas |
Family Cites Families (10)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
DE2729921C3 (en) * | 1977-07-02 | 1985-01-03 | Metallgesellschaft Ag, 6000 Frankfurt | Process for generating a gas that is exchangeable with natural gas |
JPH04243845A (en) * | 1991-01-25 | 1992-08-31 | Nippon Steel Corp | Production of methanol from iron manufacture waste gas and coke oven gas |
JP2000109440A (en) * | 1998-08-06 | 2000-04-18 | Nippon Steel Corp | Synthesis of methanol |
CN1373113A (en) * | 2002-03-20 | 2002-10-09 | 郭拥军 | Process for synthesizing methanol from coke oven gas |
CN101550052B (en) * | 2008-11-19 | 2013-04-03 | 新奥新能(北京)科技有限公司 | Process for producing methanol and coproducing methane by using synthesis gas containing methane |
CN101597527B (en) * | 2009-07-07 | 2012-12-19 | 山西科灵环境工程设计技术有限公司 | Method for making synthetic natural gas by utilizing coke oven gas |
CN101607859B (en) * | 2009-07-21 | 2012-09-05 | 太原理工大学 | Process employing coke-oven gas for production of methane |
CN101704712B (en) * | 2009-10-29 | 2012-09-05 | 山西焦化股份有限公司 | Technological method for preparing methanol by combining coke oven gas with water gas |
CN102079689B (en) * | 2009-11-30 | 2012-04-25 | 四川达兴能源股份有限公司 | Method and equipment for producing methanol |
CN102585951B (en) * | 2012-03-07 | 2014-03-12 | 四川天一科技股份有限公司 | Process for co-production of liquefied synthesis gas, pure hydrogen and methanol from coke-oven gas |
-
2013
- 2013-06-18 CN CN201310240935.2A patent/CN104232195B/en active Active
-
2014
- 2014-06-18 JP JP2014125647A patent/JP6347995B2/en active Active
- 2014-06-18 UA UAA201406869A patent/UA118650C2/en unknown
Similar Documents
Publication | Publication Date | Title |
---|---|---|
JP2015007039A5 (en) | ||
JP6347995B2 (en) | Method for simultaneous production of methanol and synthetic natural gas with coke oven gas and plant for achieving the method | |
CN104449920B (en) | The method utilizing coke-stove gas and blast furnace gas Joint Production natural gas with liquefied ammonia | |
JP2015025206A5 (en) | ||
RU2015129604A (en) | PARALLEL PRODUCTION OF HYDROGEN, CARBON MONOXIDE AND CARBON-CONTAINING PRODUCT | |
CN102703108B (en) | Technical method for Fischer-Tropsch synthesis and tail gas utilization | |
CA2879442A1 (en) | Process for comprehensively utilizing low carbon emission fischer-tropsch synthesis tail gas | |
RU2014138380A (en) | METHOD FOR PRODUCING SYNTHESIS GAS FOR AMMONIA SYNTHESIS AND THE APPROPRIATE EXTERNAL SECTION OF THE INSTALLATION FOR AMMONIA | |
WO2014000503A1 (en) | Method for preparing liquid hydrocarbon product from biomass-produced synthetic gas | |
RU2012121923A (en) | METHOD FOR PRODUCING AMMONIA | |
CN103351894A (en) | Natural gas synthesizing technology adopting coke oven gas and coal gasifier gas | |
RU2014152338A (en) | METHOD FOR PRODUCING CO, H2 AND METHANOL FROM SYNTHESIS GAS, IN PARTICULAR, FROM THE WASTE GAS OF THE PRODUCTION OF ACETYLENE | |
RU2017132708A (en) | METHOD FOR PRODUCING AMMONIA | |
CN105883851A (en) | Novel gasification and pyrolysis coupling gas poly-generation process | |
CN101704714B (en) | Method for preparing synthesis gas after pure oxygen catalytic partial oxidation of purge gas in methanol synthesis loop to increase yield of methanol, and device | |
RU2011117064A (en) | METHOD FOR PRODUCING SYNTHESIS GAS FOR THE PRODUCTION OF AMMONIA | |
RU2016138631A (en) | SYSTEM FOR THE PRODUCTION OF AROMATIC COMPOUND AND METHOD FOR PRODUCING IT | |
CA2897557C (en) | Method and apparatus for producing combustion fuel for a gas turbine | |
RU2648331C2 (en) | Method of producing synthetic liquid hydrocarbons from natural gas | |
CN209854029U (en) | Device for preparing methanol from synthesis gas without conversion system | |
RU2017107429A (en) | The method of producing synthesis gas | |
GB2489362A (en) | Two stage process for the conversion of synthesis gas using a cobalt catalyst the first stage and a supported ruthenium in the second stage | |
US9334454B2 (en) | Method for producing synthesis natural gas using straw gas | |
MY183949A (en) | Process for making a synthesis gas by reforming of a hydrocarbon and including recovery of carbon dioxide at high temperature | |
CN106553995B (en) | Natural gas and carbon dioxide dry reforming process for preparing synthetic gas |