CN1415531A - Method for producing synthesis gas by catalyzing and transforming natural gas and methane - Google Patents
Method for producing synthesis gas by catalyzing and transforming natural gas and methane Download PDFInfo
- Publication number
- CN1415531A CN1415531A CN 01133389 CN01133389A CN1415531A CN 1415531 A CN1415531 A CN 1415531A CN 01133389 CN01133389 CN 01133389 CN 01133389 A CN01133389 A CN 01133389A CN 1415531 A CN1415531 A CN 1415531A
- Authority
- CN
- China
- Prior art keywords
- gas
- oxygen
- sweet natural
- natural gas
- methane
- 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
Images
Landscapes
- Hydrogen, Water And Hydrids (AREA)
Abstract
A process for preparing synthetic gas from natural gas or methane by catalytic conversion includes such steps as mixing water vapour and/or CO2 with natural gas or methane, and reacting with the oxygen-contained gas on catalyst bed in fixed-bed reactor. It features that said raw gas and the part or all of the oxygen-contained gas are respectively introduced to said reaction system and more than 60% of the oxygen contained gas gradually comes in catalyst bed to prevent heat accumulation, resulting in high safety.
Description
Technical field:
The present invention relates to the method for Sweet natural gas (methane) catalyzed conversion preparing synthetic gas, specifically, provide a kind of will be mixed with in advance water vapour and or the Sweet natural gas (or methane) of carbonic acid gas separate with oxygen (or air or oxygen-rich air) and enter reaction system, place the oxygen distribution ware of beds that oxygen (or air or oxygen-rich air) substep is entered beds by use, the method that makes Sweet natural gas (methane) and oxygen substep mix gradually and react.
Background technology:
Since the nineties, preparing synthetic gas by partial oxidation of natural gas at home and abroad causes pays close attention to (Ashcroft A.T.et al., Nature, 344,319,1990 widely; Ashcroft A.T.et al., Nature, 352,225,1991; Hickman D.A., and Schmidt, L.D., Science, 259,343,1993.).This technological process is compared with traditional steam reforming method, because its grow heat absorption is gentle heat release, thereby has the low distinguishing feature of energy consumption, the air speed of this reaction is very big, thereby can reduce unit scale and plant investment, and in addition, H in the synthetic gas of this prepared
2/ CO=2/1 just is being suitable for doing the unstripped gas of methyl alcohol, dme and synthetic oil.
Yet, be thermopositive reaction and can under big air speed, operate just because of methane portion oxidation synthesis gas, thereby reaction will mainly concentrate on the catalyst inlet section and carry out, thereby catalyst inlet section bed heat is accumulated and made temperature too high even greater than 900 ℃, heat is to the mixing zone radiation, make catalyzer superjacent air space Sweet natural gas-oxygen mix system that the danger of blast be arranged on the one hand, will cause catalyzer superjacent air space generation gas phase oxidation on the other hand.No doubt can adopt mixing tank to place beds with methane and oxygen short mix and with mixing tank, but under high temperature like this design of Mixer difficulty relatively, prevent that particularly tempering is extremely difficult.
The technology contents of invention:
The invention provides the method for a kind of Sweet natural gas or methyl hydride catalyzed conversion preparing synthetic gas, Sweet natural gas or methane are mixed with water vapour, by beds in the fixed-bed reactor and oxygen-containing gas reaction, the preparation synthetic gas, it is characterized in that: the Sweet natural gas or the methane that will be mixed with water vapour in advance separate with most of or whole oxygen-containing gass, enter reaction system respectively, oxygen-containing gas more than 60% enters beds step by step, Sweet natural gas or methane and oxygen-containing gas substep is mixed gradually and reacts.
The invention provides the method for a kind of Sweet natural gas or methyl hydride catalyzed conversion preparing synthetic gas, with Sweet natural gas or methane and carbon dioxide mix, by beds in the fixed-bed reactor and oxygen-containing gas reaction, the preparation synthetic gas, it is characterized in that: the Sweet natural gas or the methane that will be mixed with carbonic acid gas in advance separate with most of or whole oxygen-containing gass, enter reaction system respectively, oxygen-containing gas more than 60% enters beds step by step, Sweet natural gas or methane and oxygen-containing gas substep is mixed gradually and reacts.
The invention provides the method for a kind of Sweet natural gas or methyl hydride catalyzed conversion preparing synthetic gas, Sweet natural gas or methane are mixed with water vapour and CO 2 raw material gas, by beds in the fixed-bed reactor and oxygen-containing gas reaction, the preparation synthetic gas, it is characterized in that: the Sweet natural gas or the methane that will be mixed with water vapour and carbonic acid gas in advance separate with most of or whole oxygen-containing gass, enter reaction system respectively, oxygen-containing gas more than 60% enters beds step by step, Sweet natural gas or methane and oxygen-containing gas substep is mixed gradually and reacts.
In the method for Sweet natural gas of the present invention or methyl hydride catalyzed conversion preparing synthetic gas, described oxygen-containing gas is oxygen, air or oxygen-rich air.When Sweet natural gas or methyl hydride catalyzed conversion and water vapour and (or) during the carbon dioxide reaction preparing synthetic gas, oxygen-containing gas also can be oxygen, air or the oxygen-rich air that contains water vapour and/or carbonic acid gas.
In the method for Sweet natural gas of the present invention or methyl hydride catalyzed conversion preparing synthetic gas, oxygen-containing gas is to enter beds step by step by the oxygen distribution ware that places beds.
The present invention has come down to provide a kind of mixed oxygen method that is used for Sweet natural gas or methyl hydride catalyzed conversion preparing synthetic gas.Owing to being separated with oxygen (or air or oxygen-rich air), Sweet natural gas (or methane) enters reaction system, place the oxygen distribution ware of beds that oxygen (or air or oxygen-rich air) substep is entered beds by use, Sweet natural gas (methane) and oxygen substep is mixed gradually and react, thereby avoided entrance beds heat to accumulate and make temperature too high and further cause the shortcoming of beds superjacent air space generation gas phase oxidation.The present invention since most of in addition all oxygen and raw natural gas be not pre-mixed, thereby also increased the security of reaction system.
Say that in principle the present invention is applicable to the catalyst system of any existing Sweet natural gas or methyl hydride catalyzed conversion preparing synthetic gas.
In addition, the present invention provides a kind of mixed oxygen method for the insulation fix bed reactor design of Sweet natural gas or methyl hydride catalyzed conversion preparing synthetic gas, promptly only need be on the basis of existing insulation fix bed reactor, adding an oxygen distribution ware gets final product, the design of oxygen distribution ware can letter can be numerous, thereby make this reactor possess Application feasibility, thereby can reduce the plant investment of Sweet natural gas catalyzed conversion preparing synthetic gas significantly.
Description of drawings:
Fig. 1 is the structure of reactor simplified schematic diagram;
Fig. 2 embodiment 1 reaction bed temperature distributes;
Fig. 3 embodiment 2 reaction bed temperatures distribute;
Fig. 4 embodiment 3 reaction bed temperatures distribute;
Fig. 5 embodiment 4 reaction bed temperatures distribute;
Fig. 6 embodiment 5 reaction bed temperatures distribute;
Fig. 7 embodiment 6 reaction bed temperatures distribute;
Fig. 8 embodiment 7 reaction bed temperatures distribute;
Fig. 9 embodiment 8 reaction bed temperatures distribute;
Embodiment:
A kind of fixed-bed reactor that simply are exclusively used in above-mentioned Sweet natural gas or methyl hydride catalyzed conversion preparing synthetic gas method have been adopted in the embodiment of the invention, see Fig. 1, top responds, and gas enters the mouth (1), the bottom is syngas outlet (2), catalyzer pallet (3) support catalyst bed (4) sets up one by the oxygen distribution ware (5) in the top insertion beds (4); Oxygen distribution ware (5) is a tubular structure, and the part of imbedding in the beds (4) has aperture along hoop step by step.This only is a kind ofly to realize design of the present invention, but never limits the present invention.
Embodiment and comparative example 1
Take by weighing through La
2O
3Ni/Al with the MgO modification
2O
3Catalyzer 15g, packing into has in the quartz reactor of oxygen distribution device, and the structure of reactor sketch is as shown in Figure 1.The oxygen distribution device is to be made by the silica tube that has 5 layers of aperture, every layer of aperture along 5 φ 0.3mm of tube wall distribution.Catalyst bed layer height 6cm.Catalyzer is through H
2700 ℃ of reduction activation half an hour, the unstripped gas of introducing Sweet natural gas/air/water steam (volume ratio)=1/2.4/0.8 reacts, and reaction pressure is 0.1Mpa, and gas discharge is 1000ml/min.The reaction bed temperature distribution results is seen Fig. 2, Fig. 2 has provided simultaneously and has not used the oxygen distribution device, the temperature distribution of reaction system will be entered after unstripped gas Sweet natural gas, water vapour and the air mixed simultaneously, the result shows, when entering reaction system simultaneously after unstripped gas mixes (Fig. 2 B), the catalyst inlet temperature reaches 819 ℃ immediately, and 1cm place temperature is up to 938 ℃ under the catalyst inlet; When measuring reaction bed temperature once more, because the beds temperature in is higher, heat is to the radiation of beds superjacent air space, catalyzer superjacent air space generation gas phase oxidation, make temperature distribution shown in Fig. 2 C, temperature is up to 1029 ℃ before unstripped gas enters beds; When adopting oxygen distribution ware to make air separately progress into beds, catalyzer superjacent air space gas temperature is about 700 ℃, beds ingress temperature is 692 ℃, progress into beds with air and rising gradually along the bed longitudinal temperature, hypomere in beds reaches 875 ℃ of top temperatures, then, because oxygen depletion, temperature begin to descend shown in Fig. 2 A.The reaction end gas composition sees Table 1.
Table 1 Sweet natural gas, air and steam reforming prepare the synthesis gas reaction result
Experiment CH
4CO
2H
2O CO H
2N
2
Mix oxygen 0.03 3.67 10.6 13.9 38.7 33.0
Oxygen distribution 0.02 3.31 10.4 14.6 39.6 32.1
Take by weighing through La
2O
3Ni/Al with the MgO modification
2O
3Catalyzer 15g, packing into has in the quartz reactor of oxygen distribution device, structure of reactor feature such as embodiment 1.Catalyzer is through H
2700 ℃ of reduction activation half an hour, the unstripped gas of introducing Sweet natural gas/oxygen steam (volume ratio)=1/0.5/0.8 reacts, reaction pressure is 0.1Mpa, gas discharge is 1000ml/min, Sweet natural gas mixes the back and enters reactor by the reaction gas inlet with water vapour, oxygen enters reactor by the oxygen distribution device.The reaction bed temperature distribution results is seen Fig. 3.The result shows, catalyzer superjacent air space gas temperature is lower than 700 ℃, beds ingress temperature is 690 ℃, progress into beds with oxygen and rising gradually along the bed longitudinal temperature, hypomere in beds reaches 881 ℃ of top temperatures, then, because oxygen depletion, temperature begin to descend.The reaction end gas composition sees Table 2.
Table 2 Sweet natural gas, oxygen and steam reforming prepare the synthesis gas reaction result
CH
4 CO
2 H
2O CO H
2
0.08 5.32 15.8 21.0 57.8
Take by weighing through La
2O
3Ni/Al with the MgO modification
2O
3Catalyzer 25g, packing into has in the stainless steel reactor of oxygen distribution device, and the structure of reactor sketch is also as shown in Figure 1.The oxygen distribution device is to be made by the stainless steel tube that has 5 layers of aperture, every layer of aperture along 6 φ 0.3mm of tube wall distribution.Catalyst bed layer height 6cm.Catalyzer is through H
2700 ℃ of reduction activation half an hour, the unstripped gas of introducing Sweet natural gas/air/water steam (volume ratio)=1/2.4/0.8 and Sweet natural gas/oxygen steam (volume ratio)=1/0.5/0.8 respectively reacts, reaction pressure is 0.8Mpa, gas discharge is 1700ml/min, Sweet natural gas mixes the back and enters reactor by the reaction gas inlet with water vapour, air enters reactor by the oxygen distribution device.The reaction bed temperature distribution results is seen Fig. 4.The reaction end gas composition sees Table 3.
Table 3 Sweet natural gas, oxygen (air) and steam reforming prepare the synthesis gas reaction result
Experiment CH
4CO
2H
2O CO H
2N
2
Oxygen 2.11 5.23 16.6 20.8 55.2-
Air 0.71 3.43 11.2 14.0 38.2 32.5
Take by weighing La
2O
3Ni/Al with the MgO modification
2O
3Catalyzer 25g, packing into has in the stainless steel reactor of oxygen distribution device, structure of reactor feature such as embodiment 3.Catalyst bed layer height 6cm.Catalyzer is through H
2700 ℃ of reduction activation half an hour, the unstripped gas of introducing Sweet natural gas/air/water steam/carbonic acid gas (volume ratio)=1/2.4/0.8/0.4 and Sweet natural gas/oxygen steam/carbonic acid gas (volume ratio)=1/0.5/0.8/0.35 respectively reacts, wherein carbonic acid gas and Sweet natural gas and water vapour are pre-mixed and enter reaction system, and air or oxygen enters reaction system from the oxygen distribution device.Reaction pressure is 1.0Mpa, and gas discharge is 1700ml/min.The reaction bed temperature distribution results is seen Fig. 5.The reaction end gas composition sees Table 4.As seen, H in the reaction end gas
2/ CO is about 2/1, is suitable for the synthetic of methyl alcohol, dme and synthetic oil.
Table 4 Sweet natural gas, oxygen (air), water vapour and carbonic acid gas transform preparation synthesis gas reaction result
Experiment CH
4CO
2H
2O CO H
2N
2
Oxygen 1.65 9.07 21.2 22.9 45.2-
Air 0.68 6.20 14.0 16.0 31.5 31.6
Take by weighing through La
2O
3Change living Ni/Al with MgO
2O
3Catalyzer 25g, packing into has in the stainless steel reactor of oxygen distribution device, structure of reactor feature such as embodiment 3.Catalyst bed layer height 6cm.Catalyzer is through H
2700 ℃ of reduction activation half an hour, the unstripped gas of introducing Sweet natural gas/oxygen-rich air/water vapour=1/1.46/2.0 respectively reacts, reaction pressure is 1.5Mpa, gas discharge is 1700ml/min, Sweet natural gas mixes the back and enters reactor by the reaction gas inlet with water vapour, oxygen-rich air enters reactor by the oxygen distribution device.The reaction bed temperature distribution results is seen Fig. 6.The reaction end gas composition sees Table 5.Form as seen (CO+H from tail gas
2)/N
2=3.03, be suitable for doing the unstripped gas of synthetic ammonia.
Table 5 Sweet natural gas, oxygen-rich air and steam reforming prepare the synthesis gas reaction result
CH
4 CO
2 H
2O CO H
2 N
2
0.71 6.30 28.6 10.1 38.3 16.0
Take by weighing through CeO
2Ni/Al with the MgO modification
2O
3Catalyzer 25g, packing into has in the stainless steel reactor of oxygen distribution device, structure of reactor feature such as embodiment 3.Catalyst bed layer height 6cm.Catalyzer is through H
2700 ℃ of reduction activation half an hour, the unstripped gas of introducing Sweet natural gas/oxygen steam/carbonic acid gas (volume ratio)=1/0.5/0.8/0.35 respectively reacts, wherein Sweet natural gas and water vapour are pre-mixed and enter reaction system, and carbonic acid gas and oxygen mix enter reaction system from the oxygen distribution device.Reaction pressure is 1.0Mpa, and gas discharge is 1700ml/min.The reaction bed temperature distribution results is seen Fig. 7.The reaction end gas composition sees Table 6.As seen, H in the reaction end gas
2/ CO is about 2/1, is suitable for the synthetic of methyl alcohol, dme and synthetic oil.
Table 6 Sweet natural gas, oxygen, water vapour and carbonic acid gas transform preparation synthesis gas reaction result
CH
4 CO
2 H
2O CO H
2
1.26 9.52 21.0 23.4 44.8
With embodiment 6, difference is that the carbonic acid gas with the water vapour of Sweet natural gas and 70% and 50% is pre-mixed and enters reaction system, enters reaction system from the oxygen distribution device after water vapour with other 30% and other 50% the carbon dioxide mix.The reaction bed temperature distribution results is seen Fig. 8.The reaction end gas composition sees Table 7.As seen, H in the reaction end gas
2/ CO is about 2/1, is suitable for the synthetic of methyl alcohol, dme and synthetic oil.
Table 7 Sweet natural gas, oxygen, water vapour and carbonic acid gas transform preparation synthesis gas reaction result
CH
4 CO
2 H
2O CO H
2
1.05 9.27 21.0 23.7 45.0
Embodiment 8
Take by weighing through La
20
3Ni/Al with the MgO modification
20
3Catalyzer 25g, packing into has in the stainless steel reactor of oxygen distribution device, structure of reactor feature such as embodiment 3.Catalyst bed layer height 6cm.Catalyzer is through H
2700 ℃ of reduction activation half an hour, the unstripped gas of introducing Sweet natural gas/oxygen-rich air/water vapour=1/1.46/2.0 respectively reacts, wherein about 30% oxygen-rich air mixes with Sweet natural gas and water vapour, other 70% oxygen-rich air enters beds from the oxygen distribution device, reaction pressure is 1.0Mpa, and gas discharge is 1700ml/min.The reaction bed temperature distribution results is seen Fig. 9.The reaction end gas composition sees Table 8.Form as seen (CO+H from tail gas
2)/N
2=3.04, be suitable for doing the unstripped gas of synthetic ammonia.
Table 8 Sweet natural gas, oxygen-rich air and steam reforming prepare the synthesis gas reaction result
CH
4 CO
2 H
2O CO H
2 N
2
0.35 6.22 27.9 10.3 39.0 16.2
Embodiment 9
Take by weighing through CeO
2Change living Ni/Al with MgO
2O
3Catalyzer 25g, packing into has in the stainless steel reactor of oxygen distribution device, structure of reactor feature such as embodiment 3.Catalyst bed layer height 6cm.Catalyzer is through H
2700 ℃ of reduction activation half an hour, the unstripped gas of introducing Sweet natural gas/oxygen/carbonic acid gas (volume ratio)=1/0.5/1.5 respectively reacts, and wherein Sweet natural gas and carbonic acid gas are pre-mixed and enter reaction system, and oxygen enters reaction system from the oxygen distribution device.Reaction pressure is 0.8Mpa, and gas discharge is 1700ml/min.The reaction end gas composition sees Table 9.As seen, utilize this reaction system can prepare the synthetic gas that is rich in carbon monoxide.
Table 9 Sweet natural gas, oxygen and carbonic acid gas transform preparation synthesis gas reaction result
CH
4 CO
2 H
2O CO H
2
0.51 18.1 16.0 37.5 27.8
Claims (5)
1, the method for a kind of Sweet natural gas or methyl hydride catalyzed conversion preparing synthetic gas, Sweet natural gas or methane are mixed with water vapour, by beds in the fixed-bed reactor and oxygen-containing gas reaction, the preparation synthetic gas, it is characterized in that: the Sweet natural gas or the methane that will be mixed with water vapour in advance separate with most of or whole oxygen-containing gass, enter reaction system respectively, the oxygen-containing gas more than 60% enters beds step by step, Sweet natural gas or methane and oxygen-containing gas substep is mixed gradually and reacts.
2, the method for a kind of Sweet natural gas or methyl hydride catalyzed conversion preparing synthetic gas, with Sweet natural gas or methane and carbon dioxide mix, by beds in the fixed-bed reactor and oxygen-containing gas reaction, the preparation synthetic gas, it is characterized in that: the Sweet natural gas or the methane that will be mixed with carbonic acid gas in advance separate with most of or whole oxygen-containing gass, enter reaction system respectively, oxygen-containing gas more than 60% enters beds step by step, Sweet natural gas or methane and oxygen-containing gas substep is mixed gradually and reacts.
3, the method for a kind of Sweet natural gas or methyl hydride catalyzed conversion preparing synthetic gas, Sweet natural gas or methane are mixed with water vapour and CO 2 raw material gas, by beds in the fixed-bed reactor and oxygen-containing gas reaction, the preparation synthetic gas, it is characterized in that: the Sweet natural gas or the methane that will be mixed with water vapour and carbonic acid gas in advance separate with most of or whole oxygen-containing gass, enter reaction system respectively, oxygen-containing gas more than 60% enters beds step by step, Sweet natural gas or methane and oxygen-containing gas substep is mixed gradually and reacts.
4, according to the method for claim 1,2 or 3 described Sweet natural gases or methyl hydride catalyzed conversion preparing synthetic gas, it is characterized in that: described oxygen-containing gas is oxygen, air, oxygen-rich air, perhaps contains oxygen, air, the oxygen-rich air of water vapour and/or carbonic acid gas.
5, according to the method for claim 1,2 or 3 described Sweet natural gases or methyl hydride catalyzed conversion preparing synthetic gas, it is characterized in that: oxygen-containing gas is entered beds step by step by the oxygen distribution ware that places beds.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB011333898A CN1191987C (en) | 2001-11-01 | 2001-11-01 | Method for producing synthesis gas by catalyzing and transforming natural gas and methane |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB011333898A CN1191987C (en) | 2001-11-01 | 2001-11-01 | Method for producing synthesis gas by catalyzing and transforming natural gas and methane |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1415531A true CN1415531A (en) | 2003-05-07 |
| CN1191987C CN1191987C (en) | 2005-03-09 |
Family
ID=4671771
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNB011333898A Expired - Fee Related CN1191987C (en) | 2001-11-01 | 2001-11-01 | Method for producing synthesis gas by catalyzing and transforming natural gas and methane |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1191987C (en) |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101913560A (en) * | 2010-08-16 | 2010-12-15 | 合肥工业大学 | Distributed natural gas hydrogen production reactor |
| CN101905865B (en) * | 2009-06-05 | 2012-07-18 | 中国石油天然气股份有限公司 | Method for preparing synthesis gas from natural gas or methane containing carbon dioxide |
| CN101723324B (en) * | 2009-12-16 | 2012-07-18 | 中国石油大学(北京) | Method for preparing synthetic gas by utilizing thermal coupling fixed bed device |
| WO2014111310A1 (en) | 2013-01-17 | 2014-07-24 | Shell Internationale Research Maatschappij B.V. | Process for the preparation of synthesis gas |
| CN104709876A (en) * | 2013-12-13 | 2015-06-17 | 中国科学院上海高等研究院 | Process method for preparing synthesis gas by using zero carbon or negative carbon emission system |
-
2001
- 2001-11-01 CN CNB011333898A patent/CN1191987C/en not_active Expired - Fee Related
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101905865B (en) * | 2009-06-05 | 2012-07-18 | 中国石油天然气股份有限公司 | Method for preparing synthesis gas from natural gas or methane containing carbon dioxide |
| CN101723324B (en) * | 2009-12-16 | 2012-07-18 | 中国石油大学(北京) | Method for preparing synthetic gas by utilizing thermal coupling fixed bed device |
| CN101913560A (en) * | 2010-08-16 | 2010-12-15 | 合肥工业大学 | Distributed natural gas hydrogen production reactor |
| CN101913560B (en) * | 2010-08-16 | 2012-07-25 | 合肥工业大学 | Distributed natural gas hydrogen production reactor |
| WO2014111310A1 (en) | 2013-01-17 | 2014-07-24 | Shell Internationale Research Maatschappij B.V. | Process for the preparation of synthesis gas |
| CN104709876A (en) * | 2013-12-13 | 2015-06-17 | 中国科学院上海高等研究院 | Process method for preparing synthesis gas by using zero carbon or negative carbon emission system |
Also Published As
| Publication number | Publication date |
|---|---|
| CN1191987C (en) | 2005-03-09 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN1482997A (en) | Integrated process and installation for the production of synthesis gas | |
| EP3658493B1 (en) | Process for the co-production of methanol and ammonia | |
| CN1113681C (en) | Autothermic reactor comprising oxygen ion conducting dense ceramic membrane and process using autothermic reactor for producing synthesis gas | |
| CN1308224C (en) | Method of preparing synthetic gas | |
| RU2014138380A (en) | METHOD FOR PRODUCING SYNTHESIS GAS FOR AMMONIA SYNTHESIS AND THE APPROPRIATE EXTERNAL SECTION OF THE INSTALLATION FOR AMMONIA | |
| MY183147A (en) | Process and plant for producing methanol | |
| CN1655865A (en) | Membrane systems containing an oxygen transport membrane and catalyst | |
| DK3034485T3 (en) | Reaction of carbon dioxide with hydrogen using a permselective membrane | |
| RU2015129604A (en) | PARALLEL PRODUCTION OF HYDROGEN, CARBON MONOXIDE AND CARBON-CONTAINING PRODUCT | |
| CN1111597A (en) | Process for the catalytic partial oxidation of hydrocarbons | |
| DE60036936D1 (en) | METHOD FOR THE CONTINUOUS PREPARATION OF A DIALKYL CARBONATE AND DIOL | |
| CN102659500B (en) | Method for producing ethylene and ethane and catalytic reactor | |
| CN103979492A (en) | Technical method for preparation of synthetic gas by carbon dioxide-methane autothermal reforming | |
| MY145837A (en) | Method to start a process for producing hydrocarbons from synthesis gas | |
| RU2011127911A (en) | COMPLETE INSTALLATION FOR GAS PROCESSING | |
| IL151139A (en) | Process for decomposing n2o, catalyst therefor and process for its production | |
| WO2013095130A1 (en) | Process for producing ammonia and urea | |
| CN1191987C (en) | Method for producing synthesis gas by catalyzing and transforming natural gas and methane | |
| CN102198935A (en) | Method for preparing hydrogen by reforming methanol and water | |
| US9745235B2 (en) | Method for hydrogenation of CO2 in adiabatic metal reactors | |
| CN1173462A (en) | Direct oxygen infection in nitric acid production | |
| JP5315515B2 (en) | Ethanol synthesis method and apparatus | |
| CN101905865A (en) | Method for preparing synthesis gas from natural gas or methane containing carbon dioxide | |
| CN103896210B (en) | A kind of CH 4-CO 2catalytic reforming reaction device and technique thereof | |
| CN1789111A (en) | Preparation method for hydrogen from coal-seam gas |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| C17 | Cessation of patent right | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20050309 Termination date: 20121101 |