CN103483119B - Method for producing methanefrom hydrogen-rich synthetic gas - Google Patents
Method for producing methanefrom hydrogen-rich synthetic gas Download PDFInfo
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Abstract
The invention relates to a method for producing methane from hydrogen-rich synthetic gas, which mainly comprises the following steps: 1) hydrogen-rich synthetic gas is converted into purified gas, a raw material methanol is converted into methanol steam, and the purified gas and methanol steam are mixed into a gas mixture, wherein the methanol steam accounts for 20-50 vol% of the gas mixture; 2) part of gas mixture firstly enters a primary reactor to carry out primary reaction under the action of a catalyst; 3) the gas after the primary reaction and the rest of gas mixture enter a secondary reactor to carry out secondary reaction under the action of a catalyst; 4) the gas after the secondary reaction enters a tertiary reactor to carry out tertiary reaction; and 5) the gas after the tertiary reaction is subjected to gas-liquid separation, the released product gas is collected, the methanol separated from the liquid and the raw material methanol are mixed, and water is discharged out of the system.
Description
Technical field
The present invention relates to oxycarbide methanation field, particularly a kind of method of hydrogen rich gas producing firedamp by syngas.
Background technology
Methanation technology is applied in ammonia synthesis process the earliest to remove CO and CO in unstripped gas
2, the forties, just attach great importance to the research that qualified Sweet natural gas and town gas technology are produced in methanation abroad, the beginning of the seventies, carried out both at home and abroad, with the research of the substituting Sweet natural gas of the system such as coal, petroleum naphtha, developing series of process process.Updating in recent years due to methanation catalyst, makes technological process more perfect.
H in synthetic gas
2with CO, CO
2the raw methanogenic chemical equation of reaction is:
CO+3H
2→CH
4+H
2O，△H
θ=-206.2kJ/mol
CO
2+4H
2→CH
4+2H
2O，△H
θ=-165.0kJ/mol
From above-mentioned chemical equation, the CO consuming 1mol needs the H of 3mol
2, consume the CO of 1mol
2need the H of 4mol
2.H in a lot of synthetic gas
2amount more than CO and CO
2consumable H in methanation reaction
2amount, but do not utilize the method for these hydrogen more than needed so far very well.Such as:
Chinese patent CN1919985A discloses a kind of method utilizing preparing synthesis gas from coke-oven gas, utilizes methanation reaction CO, the CO in coke(oven)gas
2and H
2cH is produced in reaction
4, then PSA purification CH
4obtain synthetic natural gas, but the method makes the hydrogen in coke(oven)gas not make full use of, CO and CO in coke(oven)gas
2the H of wherein half can only be consumed
2.
Chinese patent CN1952082A, CN1935956A, CN1952083A, CN1952084A adopt mixed cold separation and PSA to purify and produce methane, and in coke(oven)gas, precious resources hydrogen does not all utilize.
US Patent No. 4318997 discloses the method for a kind of multiple stage fluidized-bed catalytic production of methane from coke(oven)gas synthetic natural gas, and the hydrogen in its coke(oven)gas is not also fully used.
Chinese patent CN101100622A has invented mend carbon technology, mends carbon and disposablely can fill into system, also can fill into multistage methanation several times intersegmental, mends the 10-15% that carbon amounts is coke(oven)gas volume.The hydrogen resource of this process makes full use, but this technique fills into the carbonic acid gas of system and product methane is not easily separated, and also in reaction process, thermal discharge is high, also needs to take cooling means, such as passes into a large amount of water vapour or the circulation of large-tonnage product gas.
Given this, needing to provide a kind of new technique, to avoid hydrogen utilization insufficient, or occurring above problem because mending carbon consumption hydrogen resource technique.
Summary of the invention
The object of the present invention is to provide a kind of method of hydrogen rich gas producing firedamp by syngas, to improve the defect existed in known technology.
For achieving the above object, the method for hydrogen rich gas producing firedamp by syngas provided by the invention, its key step is:
1) hydrogen rich gas Synthetic holography is become purified gas, material benzenemethanol changes into methanol steam, and purified gas and methanol steam are mixed into gas mixture; Wherein methanol steam accounts for the 20-50% of gas mixture cumulative volume;
2) part gas mixture is introduced into first stage reactor carries out first set reaction under catalyst action;
3) gas after first set reaction and remaining gas mixture enter second stage reactor to carry out second time and reacts under catalyst action;
3) second time reaction after gas enter three sections of reactors carry out third time react;
4) reacted gas is through gas-liquid separation for the third time, and be collected after gas product release, the methyl alcohol be separated in liquid mixes with material benzenemethanol, and water discharges system.
Method described in 1, wherein, hydrogen rich gas synthetic gas comprises H
2amount more than CO and CO
2consumable H in methanation reaction
2the gas of amount.
Described method, wherein, hydrogen rich gas synthetic gas is coke(oven)gas and methanol purge gas.
Described method, wherein, the gas inlet temperature of first stage reactor is 240 DEG C-320 DEG C, and pressure is 0.5-5.0MPa, and air speed is 6000-16000h
-1, reaction temperature out is 580 DEG C-700 DEG C.
Described method, wherein, the gas inlet temperature of second stage reactor is 240 DEG C-320 DEG C, and pressure is 0.5-5.0MPa, and air speed is 6000-16000h
-1, reaction temperature out is 580 DEG C-700 DEG C.
Described method, wherein, the gas inlet temperature of three sections of reactors is 240 DEG C-300 DEG C, and reaction temperature out is 400 DEG C-450 DEG C.
Described method, wherein, the catalyzer in first stage reactor, second stage reactor and three sections of reactors, each constituent mass percentage composition is respectively Al
2o
3: 0-70%; ZrO
2: 5-85%; NiO:12-30%; La
2o
3: 0.5-10%; CeO
2: 0.1-5%; CaO:0-3%; BaO:0-1%.
In method of the present invention, replace carbon with methyl alcohol, fill into hydrogen rich gas producing firedamp by syngas, with hydrogen remaining after consumption reaction.
Accompanying drawing explanation
Fig. 1 is the process flow sheet of hydrogen rich gas producing firedamp by syngas of the present invention;
Wherein, 1 thick thionizer; 2 feed heater; 3 fine de-sulfur towers; 4 purification and condensation devices; 5 first stage reactors; 6 one-levels are given up pot; 7 second stage reactors; 8 secondarys give up pot; 9 three sections of reactors; 10 methyl alcohol vaporizing devices; 11 product condensers; 12 gas-liquid separators; 13 methanol rectifying towers; Reboiler at the bottom of 14 stills; 15 overhead condensers.
Embodiment
Methyl alcohol is as industrial bulk product, and convenient transportation, clean, unmanned invention so far replaces carbon with it, fills into the producing firedamp by syngas process system of hydrogen rich gas, remaining hydrogen after consumption reaction.
Methyl alcohol is main under methane synthesis condition there is following reaction:
CH
3OH→CO+2H
2，△H
θ=90.7kJ/mol
Then CO+3H
2→ CH
4+ H
2o, △ H
θ=-206.2kJ/mol
Methyl alcohol post liquefaction is easily separated with methane, and methanolysis is thermo-negative reaction, and Undec part methanol steam can reduce CO, CO
2dividing potential drop, reduces exothermic heat of reaction amount, methanol steam is passed into system and both can play cooling effect, again as raw material, consume unnecessary hydrogen.
Hydrogen rich gas synthetic gas comprises coke(oven)gas, methanol periodic off-gases etc.
Coke(oven)gas composition changes to some extent according to coking coal character, coking process and operational condition difference, and it mainly forms (volume %) as table 1.
Table 1 coke(oven)gas typical case composition
| Composition | H 2 | CH 4 | CO | C nH m | CO 2 | N 2 | O 2 |
| Composition vol.% | 50-70 | 15-30 | 5-9 | 2-4 | 2-5 | 2-6 | 0.3-0.8 |
Simultaneously containing a small amount of H
2the impurity such as S, organosulfur, tar, naphthalene, benzene.
The each component concentration ranges of methanol purge gas is in table 2.
Table 2 methanol purge gas forms
The method of hydrogen rich gas producing firedamp by syngas of the present invention, technical process is described below:
First by synthetic gas after the detar of thick thionizer 1 conventional purification, thick desulfurization, deamination, de-benzene and de-naphthalene, be compressed to 0.5-5.0Mpa, be heated to 200 DEG C-350 DEG C through feed heater 2 and enter fine de-sulfur tower 3, purified gas is inorganic sulfur through catalyzer organic sulfur conversion further, and Co-Mo/ γ-Al selected usually by catalyzer
2o
3catalyzer, then carries out fine de-sulfur, usually selects ZnO desulfurizing agent.Purified gas after fine de-sulfur enters purification and condensation device 4 and lowers the temperature, methyl alcohol accounts for the 20%-50% of whole gaseous constituent after methyl alcohol vaporizing device 10 gasifies, two strands are divided into after methanol steam mixes with purified gas, 2/3 of gas is A-share, 1/3 is B stock, and A-share enters first stage reactor 5, and gas inlet temperature is 240 DEG C-320 DEG C, pressure is 0.5-5.0MPa, and air speed is 6000-16000h
-1, apparatus with catalyst inside, in this catalyzer, each constituent mass percentage composition is respectively: Al
2o
3: 0-70%; ZrO
2: 5-85%; NiO:12-30%; La
2o
3: 0.5-10%; CeO
2: 0.1-5%; CaO:0-3%; This catalyzer of BaO:0-1%(is catalyzer disclosed in Chinese patent ZL 201010252961.3, catalyzer in the second stage reactor below mentioned 7, three sections of reactors 9 is all identical), reaction temperature out is 580 DEG C-700 DEG C, give up after pot 6 is lowered the temperature through one-level after reaction and enter second stage reactor 7 with B stock gas and vapor permeation, temperature in is 240 DEG C-320 DEG C, pressure is 0.5-5.0MPa, and air speed is 6000 ~ 16000h
-1, apparatus with catalyst inside, reaction temperature out is 580 DEG C-700 DEG C, and giving up after pot 8 is lowered the temperature through secondary after reaction enters three sections of reactors 9, and temperature in is 240 DEG C-300 DEG C, and pressure is 0.5-5.0MPa, and air speed is 6000-16000h
-1apparatus with catalyst inside, reaction temperature out is 400 DEG C-450 DEG C, after reaction, gas is lowered the temperature through methyl alcohol vaporizing device 10, after lower the temperature through product condenser 11 again, then enter knockout drum 12, gas product is collected after the release of separating tank top, liquid flows into methanol rectifying tower 13 bottom separating tank, and the methyl alcohol be separated mixes with material benzenemethanol after overhead condenser 15, and water discharges system after reboiler at the bottom of still.
Below in conjunction with Figure of description, the present invention will be further described, is below only preferred embodiment of the present invention, can not limit scope of the present invention with this.Namely every change of doing according to the present patent application the scope of the claims and modification, all should still remain within the scope of the patent.
Embodiment 1
The coke(oven)gas of 5000 ten thousand Nm3/h, becomes to be grouped into as shown in table 3.
Table 3:
| Composition | H 2 | CH 4 | CO | C nH m | CO 2 | N 2 | O 2 |
| Composition vol.% | 55 | 30 | 6 | 2 | 3 | 3.7 | 0.3 |
First by coke(oven)gas after the detar of thick thionizer 1 conventional purification, thick desulfurization, deamination, de-benzene and de-naphthalene, be compressed to 2.0Mpa, be heated to 300 DEG C through feed heater 2 and enter fine de-sulfur tower 3, purified gas is inorganic sulfur through catalyzer organic sulfur conversion further, and Co-Mo/ γ-Al selected usually by catalyzer
2o
3catalyzer, then carries out fine de-sulfur, usually selects ZnO desulfurizing agent.Purified gas after fine de-sulfur enters purification and condensation device 4 and lowers the temperature, and methyl alcohol accounts for 20% of whole gaseous constituent after methyl alcohol vaporizing device 10 gasifies.Be divided into two strands after methanol steam mixes with purified gas, 2/3 of gas is A-share, and 1/3 is B stock, and A-share enters first stage reactor 5, and gas inlet temperature is 260 DEG C, and pressure is 2.0MPa, and air speed is 8000h
-1, apparatus with catalyst inside, reaction temperature out is 580 DEG C, and the transformation efficiency of methyl alcohol is 60%, to give up pot 6(and waste heat boiler after reaction through one-level) after cooling and B stock gas and vapor permeation enter second stage reactor 7, temperature in is 260 DEG C, and pressure is 2.0MPa, and air speed is 8000h
-1, apparatus with catalyst inside, reaction temperature out is 580 DEG C, and the transformation efficiency of methyl alcohol is 60%, and giving up after pot 8 is lowered the temperature through secondary after reaction enters three sections of reactors 9, and temperature in is 250 DEG C, and pressure is 2.0MPa, and air speed is 8000h
-1apparatus with catalyst inside, reaction temperature out is 400 DEG C, and the transformation efficiency of methyl alcohol is 40%, after reaction, gas is lowered the temperature through methyl alcohol vaporizing device 10, after lower the temperature through product condenser 11 again, then enter knockout drum 12, gas product is collected after the release of knockout drum 12 top, symbiosis methane phase 3,020 ten thousand Nm3/h, liquid flows into methanol rectifying tower 13 bottom knockout drum 12, and the methyl alcohol be separated mixes with material benzenemethanol after overhead condenser 15, and water discharges system after reboiler at the bottom of still 14.Gas product composition is in table 4.
Table 4:
| Composition | H 2 | CH 4 | N 2 | O 2 |
| Composition vol.% | 5.29 | 88.82 | 5.44 | 0.41 |
Embodiment 2
The coke(oven)gas of 5000 ten thousand Nm3/h, becomes to be grouped into as table 5.
Table 5:
| Composition | H 2 | CH 4 | CO | C nH m | CO 2 | N 2 | O 2 |
| Composition vol.% | 60 | 27 | 7 | 2 | 2 | 1.7 | 0.3 |
First by coke(oven)gas after the detar of thick thionizer 1 conventional purification, thick desulfurization, deamination, de-benzene and de-naphthalene, be compressed to 2.5Mpa, be heated to 320 DEG C through feed heater 2 and enter fine de-sulfur tower 3, purified gas is inorganic sulfur through catalyzer organic sulfur conversion further, and Co-Mo/ γ-Al selected usually by catalyzer
2o
3catalyzer, then carries out fine de-sulfur, usually selects ZnO desulfurizing agent.Purified gas after fine de-sulfur enters purification and condensation device 4 and lowers the temperature, methyl alcohol accounts for 25% of whole gaseous constituent after methyl alcohol vaporizing device 10 gasifies, two strands are divided into after methanol steam mixes with purified gas, 2/3 of gas is A-share, 1/3 is B stock, and A-share enters first stage reactor 5, and gas inlet temperature is 280 DEG C, pressure is 2.5MPa, and air speed is 10000h
-1, apparatus with catalyst inside, reaction temperature out is 600 DEG C, and the transformation efficiency of methyl alcohol is 65%, and giving up after pot 6 is lowered the temperature through one-level after reaction enters second stage reactor 7 with B stock gas and vapor permeation, and temperature in is 280 DEG C, and pressure is 2.5MPa, and air speed is 10000h
-1, apparatus with catalyst inside, reaction temperature out is 600 DEG C, and the transformation efficiency of methyl alcohol is 65%, and giving up after pot 8 is lowered the temperature through secondary after reaction enters three sections of reactors 9, and temperature in is 260 DEG C, and pressure is 2.5MPa, and air speed is 10000h
-1apparatus with catalyst inside, reaction temperature out is 410 DEG C, and the transformation efficiency of methyl alcohol is 45%, after reaction, gas is lowered the temperature through methyl alcohol vaporizing device 10, after lower the temperature through product condenser 11 again, then enter knockout drum 12, gas product is collected after the release of separating tank top, symbiosis methane phase 3,284 ten thousand Nm3/h, liquid flows into methanol rectifying tower 13 bottom separating tank, and the methyl alcohol be separated mixes with material benzenemethanol after overhead condenser 15, and water discharges system after reboiler at the bottom of still.
Gas product composition is as shown in table 6.
Table 6:
| Composition | H 2 | CH 4 | N 2 | O 2 |
| Composition vol.% | 2.86 | 94.27 | 2.44 | 0.43 |
Embodiment 3
The methanol purge gas of 5000 ten thousand Nm3/h, becomes to be grouped into as shown in table 7.
Table 7:
| Composition | H 2 | CH 4 | CO | CO 2 | N 2 | H2S |
| Composition vol.% | 75 | 14 | 7 | 3 | 0.7 | 0.3 |
First by methanol purge gas after the detar of thick thionizer 1 conventional purification, thick desulfurization, deamination, de-benzene and de-naphthalene, be compressed to 3.0MPa, be heated to 330 DEG C through feed heater 2 and enter fine de-sulfur tower 3, purified gas is inorganic sulfur through catalyzer organic sulfur conversion further, and Co-Mo/ γ-Al selected usually by catalyzer
2o
3catalyzer, then carries out fine de-sulfur, usually selects ZnO desulfurizing agent.Purified gas after fine de-sulfur enters purification and condensation device 4 and lowers the temperature, methyl alcohol accounts for 30% of whole gaseous constituent after methyl alcohol vaporizing device 10 gasifies, two strands are divided into after methanol steam mixes with purified gas, 2/3 of gas is A-share, 1/3 is B stock, and A-share enters first stage reactor 5, and gas inlet temperature is 300 DEG C, pressure is 3.0MPa, and air speed is 12000h
-1, apparatus with catalyst inside, reaction temperature out is 610 DEG C, and the transformation efficiency of methyl alcohol is 70%, and giving up after pot 6 is lowered the temperature through one-level after reaction enters second stage reactor 7 with B stock gas and vapor permeation, and temperature in is 300 DEG C, and pressure is 3.0MPa, and air speed is 12000h
-1, in-builtly state catalyzer, reaction temperature out is 610 DEG C, and the transformation efficiency of methyl alcohol is 70%, and giving up after pot 8 is lowered the temperature through secondary after reaction enters three sections of reactors 9, and temperature in is 270 DEG C, and pressure is 3.0MPa, and air speed is 12000h
-1apparatus with catalyst inside, reaction temperature out is 420 DEG C, and the transformation efficiency of methyl alcohol is 50%, after reaction, gas is lowered the temperature through methyl alcohol vaporizing device 10, after lower the temperature through product condenser 11 again, then enter knockout drum 12, gas product is collected after the release of separating tank top, symbiosis methane phase 3107.14 ten thousand Nm3/h, liquid flows into methanol rectifying tower 13 bottom separating tank, and the methyl alcohol be separated mixes with material benzenemethanol after overhead condenser 15, and water discharges system after reboiler at the bottom of still.
Gas product composition is as shown in table 8.
Table 8:
| Composition | H 2 | CH 4 | N 2 |
| Composition vol.% | 3.86 | 95.1 | 1.04 |
Embodiment 4
The methanol purge gas of 5000 ten thousand Nm3/h, becomes to be grouped into as shown in table 9.
Table 9:
| Composition | H 2 | CH 4 | CO | CO 2 | N 2 | H2S |
| Composition vol.% | 80 | 11 | 6 | 2 | 0.8 | 0.2 |
First by methanol purge gas after the detar of thick thionizer 1 conventional purification, thick desulfurization, deamination, de-benzene and de-naphthalene, be compressed to 3.5MPa, be heated to 340 DEG C through feed heater 2 and enter fine de-sulfur tower 3, purified gas is inorganic sulfur through catalyzer organic sulfur conversion further, and Co-Mo/ γ-Al selected usually by catalyzer
2o
3catalyzer, then carries out fine de-sulfur, usually selects ZnO desulfurizing agent.Purified gas after fine de-sulfur enters purification and condensation device 4 and lowers the temperature, methyl alcohol accounts for 35% of whole gaseous constituent after methyl alcohol vaporizing device 10 gasifies, two strands are divided into after methanol steam mixes with purified gas, 2/3 of gas is A-share, 1/3 is B stock, and A-share enters first stage reactor 5, and gas inlet temperature is 310 DEG C, pressure is 3.5MPa, and air speed is 14000h
-1, apparatus with catalyst inside, reaction temperature out is 620 DEG C, and the transformation efficiency of methyl alcohol is 75%, and giving up after pot 6 is lowered the temperature through one-level after reaction enters second stage reactor 7 with B stock gas and vapor permeation, and temperature in is 310 DEG C, and pressure is 3.5MPa, and air speed is 14000h
-1, apparatus with catalyst inside, reaction temperature out is 620 DEG C, and the transformation efficiency of methyl alcohol is 75%, and giving up after pot 8 is lowered the temperature through secondary after reaction enters three sections of reactors 9, and temperature in is 280 DEG C, and pressure is 3.5MPa, and air speed is 14000h
-1apparatus with catalyst inside, reaction temperature out is 430 DEG C, and the transformation efficiency of methyl alcohol is 50%, after reaction, gas is lowered the temperature through methyl alcohol vaporizing device 10, after lower the temperature through product condenser 11 again, then enter knockout drum 12, gas product is collected after the release of separating tank top, symbiosis methane phase 3124.24 ten thousand Nm3/h, liquid flows into methanol rectifying tower 13 bottom separating tank, and the methyl alcohol be separated mixes with material benzenemethanol after overhead condenser 15, and water discharges system after reboiler at the bottom of still.
Gas product composition is as shown in table 10.
Table 10:
| Composition | H 2 | CH 4 | N 2 |
| Composition vol.% | 2.77 | 96.14 | 1.09 |
Claims (3)
1. a method for hydrogen rich gas producing firedamp by syngas, its key step is:
1) hydrogen rich gas Synthetic holography is become purified gas, material benzenemethanol changes into methanol steam, and purified gas and methanol steam are mixed into gas mixture; Wherein methanol steam accounts for the 20-50% of gas mixture cumulative volume;
2) part gas mixture is introduced into first stage reactor carries out first set reaction under catalyst action, and the gas inlet temperature of first stage reactor is 240 DEG C-320 DEG C, and pressure is 0.5-5.0MPa, and air speed is 6000-16000h
-1, reaction temperature out is 580 DEG C-700 DEG C;
3) gas after first set reaction and remaining gas mixture enter second stage reactor to carry out second time and reacts under catalyst action, and the gas inlet temperature of second stage reactor is 240 DEG C-320 DEG C, and pressure is 0.5-5.0MPa, and air speed is 6000-16000h
-1, reaction temperature out is 580 DEG C-700 DEG C;
4) second time reaction after gas enter three sections of reactors carry out third time reaction, the gas inlet temperature of three sections of reactors is 240 DEG C-300 DEG C, react temperature out be 400 DEG C-450 DEG C;
5) reacted gas is through gas-liquid separation for the third time, and be collected after gas product release, the methyl alcohol be separated in liquid mixes with material benzenemethanol, and water discharges system;
Wherein, the catalyzer in first stage reactor, second stage reactor and three sections of reactors, each constituent mass percentage composition is respectively Al
2o
3: 0-70%; ZrO
2: 5-85%; NiO:12-30%; La
2o
3: 0.5-10%; CeO
2: 0.1-5%; CaO:0-3%; BaO:0-1%.
2. method according to claim 1, wherein, hydrogen rich gas synthetic gas comprises H
2amount more than CO and CO
2consumable H in methanation reaction
2the gas of amount.
3. method according to claim 1, wherein, hydrogen rich gas synthetic gas is coke(oven)gas and methanol purge gas.
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Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101100622A (en) * | 2007-07-16 | 2008-01-09 | 张文慧 | Method and device for synthesizing natural gas by using coke oven gas |
| CN101597527A (en) * | 2009-07-07 | 2009-12-09 | 山西科灵环境工程设计技术有限公司 | A kind of method of utilizing coke(oven)gas to produce synthetic natural gas |
| CN103131490A (en) * | 2011-12-02 | 2013-06-05 | 中国科学院大连化学物理研究所 | Technology of coke oven gas for methane production |
-
2013
- 2013-08-27 CN CN201310381313.1A patent/CN103483119B/en active Active
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101100622A (en) * | 2007-07-16 | 2008-01-09 | 张文慧 | Method and device for synthesizing natural gas by using coke oven gas |
| CN101597527A (en) * | 2009-07-07 | 2009-12-09 | 山西科灵环境工程设计技术有限公司 | A kind of method of utilizing coke(oven)gas to produce synthetic natural gas |
| CN103131490A (en) * | 2011-12-02 | 2013-06-05 | 中国科学院大连化学物理研究所 | Technology of coke oven gas for methane production |
Non-Patent Citations (2)
| Title |
|---|
| Development of Methanol Decomposition Catalysts for Production of H2 and CO;WU-HSUNCHENG;《Acc. Chem. Res.》;19990501;第32卷(第8期);685-691 * |
| 甲醇裂解催化剂的现状及发展;孙康波 等;《科技情报开发与经济》;20051231;第15卷(第13期);148-150 * |
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