CN205115038U - Synthetic reaction unit of methane chemistry chain system of reforming - Google Patents
Synthetic reaction unit of methane chemistry chain system of reforming Download PDFInfo
- Publication number
- CN205115038U CN205115038U CN201520880921.1U CN201520880921U CN205115038U CN 205115038 U CN205115038 U CN 205115038U CN 201520880921 U CN201520880921 U CN 201520880921U CN 205115038 U CN205115038 U CN 205115038U
- Authority
- CN
- China
- Prior art keywords
- reactor
- gas
- methane
- oxygen
- reactor shell
- 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.)
- Active
Links
Abstract
The utility model discloses a synthetic reaction unit of methane chemistry chain system of reforming, including the reactor barrel, be provided with the cellular carrier of oxygen pore that the cellular carrier of oxygen and a plurality of run through the reactor barrel in the reactor barrel, reactor barrel one end is provided with gaseous memory area, and gaseous memory area is provided with the reactor gas access, and the other end is provided with the gas collection district, and the gas collection district is provided with the tail gas export. The utility model has the advantages that: methane chemistry chain reformation reaction unit reforms with traditional steam or CO2 and compares, has saved vapor and pure oxygen preparation link, and the cost is showing and reduces, the danger that methane and gaseous phase oxygen direct contact probably blasted has been avoided moreover to the easy isothermal run of realization response, need not drive the catalyst granules hangs down equipment long service life at reactor mesocycle, energy loss, the cellular carrier of oxygen has the heat accumulation function in the reaction, the reaction temperature is maintain to the help reactor, is favorable to the stability of reaction to be gone on.
Description
Technical field
The utility model relates to fuel clean burning, functional materials, environmental protection technical field, especially relates to a kind of methane chemical chain reformation synthetic reaction device processed.
Background technology
Methane is the main component of Sweet natural gas, coal-seam gas and gas hydrate, along with the day by day exhaustion of petroleum resources, the methane resource of reserves relative abundance will become one of substitute energy that rare-view set-up most wishes, and exploration shows, China's coal-seam gas reserves are about 35,000,000,000,000 m
3, Sweet natural gas prospective reserves reaches 43,000,000,000,000 m
3, therefore, economic, the efficient methane conversion technology of research and development has great strategic importance.And to be an important channel of liquid fuel and chemical by methane conversion be is first synthetic gas (H by methane conversion
2+ CO), then synthetic gas is further converted to liquid fuel and chemical, so synthetic gas is the important intermediate of gas chemical industry through means such as Fischer-Tropsch synthesis.
Traditional gas renormalizing is by methane and water vapour (steammethanereforming, SMR) or CO
2there is reforming reaction and generate synthetic gas in (carbondioxidereforming, CDR), then by liquid fuels etc. such as synthetic gas hydrogen manufacturing, methyl alcohol, synthetic ammonia and gasoline.SMR and CDR is strong thermo-negative reaction, equipment bulky complex, and process cost is expensive, and wherein synthetic gas preparation accounts for the 60%-70% of whole gas chemical industry's gross investment and production cost.Therefore, study more economical, more efficient methane conversion technology and just seem extremely urgent.
It is a kind of methane synthetic gas technology that development in recent years is got up that methane chemical chain is reformed, and its essence is methane portion oxidation synthesis gas.It is the principle of reacting according to chemical looping that chemical chain is reformed, and utilizes the lattice oxygen in metal oxide molecule, as oxygen source, methane portion oxidation is become synthetic gas; Then, lose the metal oxide oxidation by air recovery lattice oxygen again of lattice oxygen, complete chain circulation reaction.Visible, reform and methane steam or CO at methane chemical chain
2reformation is compared, and eliminates pure oxygen and prepares link, is a gentle thermopositive reaction, can realizes high conversion and the H of methane under the condition of less energy-consumption
2, CO highly selective, have that less investment, efficiency are high, low power consumption and other advantages, but also avoid methane and directly contact with gas phase oxygen the danger that may blast.
It is pointed out that traditional methane reforming circulating fluid bed reactor needs constantly to drive catalyzer Rapid Circulation, not only energy consumption is comparatively large, also very serious to the wearing and tearing of equipment, not easily realizes isothermal operation simultaneously.And a kind of good methane reforming reactor device is not only wanted to realize efficient fuel reforming, also should be taken into account the energy consumption of device and the isothermal operation of reaction.Therefore, a kind of novel methane chemical chain reformation synthetic reaction device processed is needed to solve the problems referred to above.
Summary of the invention
The purpose of this utility model is to provide a kind of methane chemical chain and reforms synthetic reaction device processed, and it does not need the preparation of pure oxygen, does not need promotion catalyzer to circulate answering between device, reduce energy consumption, reaction temperature and, easily realize isothermal operation, overcome the defect of prior art.
Technical solution of the present utility model is: a kind of methane chemical chain reformation synthetic reaction device processed, comprise reactor shell, it is characterized in that: be provided with cellular oxygen carrier in described reactor shell and several run through the cellular oxygen carrier duct of described reactor shell, described reactor shell one end is provided with atmosphere storage district, described atmosphere storage district is provided with gas reactor entrance, the other end is provided with plenum zone, and described plenum zone is provided with offgas outlet.Methane and air carry out the transmission of lattice oxygen and heat alternately through oxygen carrier duct, realize the reformation of fuel.
Offgas outlet is for connecting the equipment such as residual heat boiler for exchanging heat and purified synthesis gas pressurizing device, and the synthetic gas after purification can pressurized storage or enter synthesizing section.
The reaction unit that the utility model proposes only need regulate the air input of gas reactor entrance in operational process, gas flow rate and temperature of reaction can realize the stable isothermal operation continued, pure oxygen is not needed to prepare, do not need to drive the larger energy consumption needed for granules of catalyst circulation, extend the work-ing life of reactor wall, avoid methane and directly contact with gas phase oxygen the danger that may blast, solve the energy consumption existed in current fluidized-bed reactor preferably large, easy to wear, fluctuation of service, the problem that the fluctuation of temperature each point is larger, as substituted air with water during oxygen carrier regeneration in reactor, also can obtain comparatively pure hydrogen, can be used for fuel cell.
Described atmosphere storage district is also provided with gas radiation formula pre-distributor, and described gas radiation formula pre-distributor is connected with described gas reactor entrance.Gas for entering gas reactor entrance distributes again, makes gas uniform stably enter cellular oxygen carrier duct.
Preferably, described reactor shell and described atmosphere storage district removably connect, and reactor shell and described atmosphere storage district pass through Flange joint.
Preferably, described reactor shell and described plenum zone removably connect, and described reactor shell and described plenum zone pass through Flange joint.The maintenance can be convenient in production process that removably connects of reactor shell and described atmosphere storage district and reactor shell and plenum zone operates with other.
Preferably, described reactor shell is outside equipped with heating unit.Reactor shell outer wall by the heat supply of hearth-type heating system, to maintain the temperature needed for reaction.
Preferably, described cellular oxygen carrier is selected from La
0.7sr
0.3mnO
3, La
0.7sr
0.3niO
3and LaFeO
3in one, cellular oxygen carrier is formed by composite transition metal oxide compacting sintering.Cellular oxygen carrier is made up of composite transition metal oxide, structure has a large amount of Lacking oxygen and there is larger specific surface area, by center to the isometrical evenly distributed cylindrical bore of periphery, duct is with axially parallel, the reversible absorption of energy and transmission oxygen when high temperature, to fuel such as methane, there is higher catalytic activity, there is good thermodynamic stability and suitable physical strength, negatively charged ion, electronics, room are demonstrated to the transport properties of mixed type, therefore, be suitable for carrying out chemical chain reformation in oxygen carrier reactor.Existing experiment shows, composition metal compound can be reformed for the chemical chain of methane and be provided enough lattice oxygen, and has outstanding structural stability and good oxidation reduction cycle reactive behavior.
The beneficial effects of the utility model are:
1) methane chemical chain is reformed and traditional water vapor or CO
2reformation is compared, and eliminates water vapour and link prepared by pure oxygen, and cost significantly reduces;
2) be easy to the isothermal operation of realization response, but also avoid methane and directly contact with gas phase oxygen the danger that may blast;
3) do not need to drive granules of catalyst to circulate in the reactor, energy waste is low, and service life of equipment is long;
4), during oxygen carrier regeneration, as used water vapour to replace air, steam cracking can generate comparatively pure hydrogen, can be used for fuel cell;
5) cellular oxygen carrier has heat accumulation function in the reaction, reactor can be helped to maintain temperature of reaction, alleviate the thermal load of external heat equipment, is conducive to the stable of reaction and carries out.
Accompanying drawing explanation
Accompanying drawing 1 is the structural representation of the utility model methane chemical chain reformation synthetic reaction device processed;
1, gas reactor entrance, 2, gas radiation formula pre-distributor, 3, atmosphere storage district, the 4, first flange, 5, reactor shell, 6, cellular oxygen carrier, 7, cellular oxygen carrier duct, the 8, second flange, 9, plenum zone, 10, offgas outlet.
Embodiment
Below in conjunction with accompanying drawing, the present invention will be further described, and the direction of arrow in Fig. 1 is the direction of gas flow.
Embodiment 1
Consult Fig. 1, a kind of methane chemical chain reformation synthetic reaction device processed, is made up of reactor shell 5, cellular oxygen carrier 6, entrance radiant gas pre-distributor 2, atmosphere storage district 3, plenum zone 9, offgas outlet 10, first flange 4 and the second flange 8.Cellular oxygen carrier 6 is provided with and several run through the cellular oxygen carrier duct 7 of reactor shell 5 in reactor shell 5, cellular oxygen carrier 6 is fixed in the middle of methane chemical chain reformation synthetic reaction device processed, and the partial reaction heat in the gaseous oxygen in air, the lattice oxygen needed for fuel and fuel reaction district is exchanged by cellular oxygen carrier.Methane and air carry out the transmission of lattice oxygen and heat alternately through oxygen carrier duct, realize the reformation of fuel.
Atmosphere storage district 3 is provided with gas reactor entrance 1.Gas reactor entrance 1 is controlled by three-way solenoid valve.Gas reactor entrance 1 is for connecting the storage of gas with various, pressurization and treating plant respectively.Plenum zone is provided with offgas outlet 10, and offgas outlet 10 is for connecting the equipment such as residual heat boiler for exchanging heat and purified synthesis gas pressurizing device, and the synthetic gas after purification can pressurized storage or enter synthesizing section.
This device of reaction unit that the utility model proposes have employed cellular oxygen carrier and air, methane alternation response design carry out methane reforming producing synthesis gas, lattice oxygen and heat is transmitted by cellular oxygen carrier, the air input of fuel metering gas reactor entrance 1 is only needed in operational process, gas flow rate and temperature of reaction can realize the stable isothermal operation continued, pure oxygen is not needed to prepare, do not need to drive the larger energy consumption needed for granules of catalyst circulation, extend the work-ing life of reactor wall, avoid methane and directly contact with gas phase oxygen the danger that may blast, solve the energy consumption existed in current fluidized-bed reactor preferably large, easy to wear, fluctuation of service, the problem that the fluctuation of temperature each point is larger, as substituted air with water during oxygen carrier regeneration in reactor, also can obtain comparatively pure hydrogen, can be used for fuel cell.
Gas radiation formula pre-distributor 2 is connected with gas reactor entrance 1.Gas for entering gas reactor entrance 1 distributes again, makes gas uniform stably enter cellular oxygen carrier duct.
Reactor shell 5 and atmosphere storage district 3 removably connect; reactor shell 5 and atmosphere storage district 3 are by bolt or Flange joint; or connected all within protection domain of the present utility model by the mode of connection that it may occur to persons skilled in the art that, reactor shell 5 is connected by the first flange 4 with atmosphere storage district 3 in the present embodiment.
Reactor shell 5 and plenum zone 9 removably connect; reactor shell 5 and plenum zone 9 are by bolt or Flange joint; or connected all within protection domain of the present utility model by the mode of connection that it may occur to persons skilled in the art that, reactor shell 5 is connected by the second flange 8 with plenum zone 9 in the present embodiment.Reactor shell 5 operates with other with the maintenance can be convenient in production process that removably connects of plenum zone 8 with atmosphere storage district 3 and reactor shell 5.
Reactor shell 5 is outside equipped with heating unit, and reactor shell outer wall is made up of high temperature resistant stainless steel material (904L), reactor shell outer wall by the heat supply of hearth-type heating system, to maintain the temperature needed for reaction.
Cellular oxygen carrier is selected from La
0.7sr
0.3mnO
3, La
0.7sr
0.3niO
3and LaFeO
3in one, cellular oxygen carrier is formed by composite transition metal oxide compacting sintering.Cellular oxygen carrier is made up of composite transition metal oxide, structure has a large amount of Lacking oxygen and there is larger specific surface area, by center to the isometrical evenly distributed cylindrical bore of periphery, duct is with axially parallel, the reversible absorption of energy and transmission oxygen when high temperature, to fuel such as methane, there is higher catalytic activity, there is good thermodynamic stability and suitable physical strength, negatively charged ion, electronics, room are demonstrated to the transport properties of mixed type, therefore, be suitable for carrying out chemical chain reformation in oxygen carrier reactor.Existing experiment shows, composition metal compound can be reformed for the chemical chain of methane and be provided enough lattice oxygen, and has outstanding structural stability and good oxidation reduction cycle reactive behavior.
Principle of work of the present utility model is: open reactor cylinder external heating device, controls temperature of reactor 850 DEG C-900 DEG C, fuel (CH
4), air, rare gas element (N
2) alternately enter reactor through the gas reactor entrance 1 of reactor bottom.First N in gas reactor entrance 1 is opened
2purge 5 minutes, closes N afterwards
2, open the fuel inlet in gas reactor entrance 1, from the CH of reactor bottom
4enter radiant gas pre-distributor 2, enter after radiant gas pre-distributor 2 is uniformly dispersed, flow from bottom to top along cellular oxygen carrier passage 7 under the pressure of self, CH during high temperature
4react with cellular oxygen carrier 6, use lattice oxygen in cellular oxygen carrier to carry out partial oxidative steam reforming CH
4, generate CO and H
2for the synthetic gas of main ingredient, synthetic gas is discharged by offgas outlet 10 after plenum zone 9, and obtain after heat through waste heat boiler, after isolation of purified system purification, obtain purer synthetic gas, methane conversion is more than 90%, CO and H
2close to 1:2, store after pressurization or enter synthesizing section, react after 30 minutes, close fuel air, open N
2gas entrance, purge remaining unreacting gas 5 minutes, tail gas is discharged through top offgas outlet 10, and the gas after discharge enters air after waste heat boiler or interchanger reclaim heat, after purging completes, close inert gas entrance, open the gas inlet in gas reactor entrance 1, air enters reactor through radiant gas pre-distributor 2, flow from bottom to top along cellular oxygen carrier road 7 under the pressure of self, gaseous oxygen during high temperature in air and cellular oxygen carrier 6 react, lattice oxygen in cellular oxygen carrier 6 is recovered, and carry out thermal exchange with cellular oxygen carrier 6, what promotion was reacted continues to carry out, tail gas is through exporting 10 discharges, air is entered again after waste heat boiler or interchanger reclaim heat, so alternately pass into fuel, rare gas element, air, reaction persistent loop carries out.
Embodiment 2
Reaction unit is identical with embodiment 1, chooses LaFeO
3for cellular oxygen carrier material, open reactor cylinder external heating device, control temperature of reactor 850 DEG C, fuel (CH
4), air, rare gas element (N
2) alternately enter reactor through the gas reactor entrance 1 of reactor bottom.First N in gas reactor entrance 1 is opened
2purge 5 minutes, gas flow 80L/h, closes N afterwards
2, open the fuel inlet in gas reactor entrance 1, from the CH of reactor bottom
4enter radiant gas pre-distributor 2, gas flow 120L/h, enter after radiant gas pre-distributor 2 is uniformly dispersed, flow from bottom to top along cellular oxygen carrier passage 7 under the pressure of self, CH during high temperature
4react with cellular oxygen carrier 6, use lattice oxygen in cellular oxygen carrier to carry out partial oxidative steam reforming CH
4, generate CO and H
2for the synthetic gas of main ingredient, synthetic gas is discharged by offgas outlet 10 after plenum zone 9, obtains after heat, obtain purer synthetic gas, store or enter synthesizing section after pressurization after isolation of purified system purification through waste heat boiler, react after 30 minutes, close fuel air, open N
2gas entrance, purge remaining unreacting gas 5 minutes, tail gas is discharged through top offgas outlet 10, and the gas after discharge enters air after waste heat boiler or interchanger reclaim heat, after purging completes, close inert gas entrance, open the gas inlet in gas reactor entrance 1, air enters reactor through radiant gas pre-distributor 2, flow from bottom to top along cellular oxygen carrier road 7 under the pressure of self, flow is 180L/h, gaseous oxygen during high temperature in air and cellular oxygen carrier 6 react, lattice oxygen in cellular oxygen carrier 6 is recovered, and carry out thermal exchange with cellular oxygen carrier 6, what promotion was reacted continues to carry out, tail gas is through exporting 10 discharges, air is entered again after waste heat boiler or interchanger reclaim heat, so alternately pass into fuel, rare gas element, air, reaction persistent loop carries out.
The implementation condition of embodiment 2 and embodiment result, as shown in table 1.
Table 1
Embodiment 3
Identical with embodiment 2, difference is:
The implementation condition of embodiment 3 and embodiment result, as shown in table 2.
Table 2
Embodiment 4
Identical with embodiment 2, difference is:
The implementation condition of embodiment 4 and embodiment result, as shown in table 3.
Table 3
As can be seen from table 1, table 2 and table 3, methane conversion is more than 90%, CO and H
2close to 1:2.
Methane chemical chain reforming reaction device and traditional water vapor or CO
2reformation is compared, and eliminates water vapour and link prepared by pure oxygen, and cost significantly reduces; Be easy to the isothermal operation of realization response, but also avoid methane and directly contact with gas phase oxygen the danger that may blast; Do not need to drive granules of catalyst to circulate in the reactor, energy waste is low, and service life of equipment is long; During oxygen carrier regeneration, as used water vapour to replace air, steam cracking can generate comparatively pure hydrogen, can be used for fuel cell; Cellular oxygen carrier has heat accumulation function in the reaction, reactor can be helped to maintain temperature of reaction, alleviate the thermal load of external heat equipment, is conducive to the stable of reaction and carries out.
The foregoing is only preferred embodiment of the present utility model, be not limited to the utility model, for a person skilled in the art, the utility model can have various modifications and variations.All within spirit of the present utility model and principle, any amendment done, equivalent replacement, improvement etc., all should be included within protection domain of the present utility model.
Claims (8)
1. a methane chemical chain reformation synthetic reaction device processed, comprise reactor shell, it is characterized in that: be provided with cellular oxygen carrier in described reactor shell and several run through the cellular oxygen carrier duct of described reactor shell, described reactor shell one end is provided with atmosphere storage district, described atmosphere storage district is provided with gas reactor entrance, the other end is provided with plenum zone, and described plenum zone is provided with offgas outlet.
2. methane chemical chain reformation according to claim 1 synthetic reaction device processed, it is characterized in that: described atmosphere storage district is also provided with gas radiation formula pre-distributor, described gas radiation formula pre-distributor is connected with described gas reactor entrance.
3. methane chemical chain reformation according to claim 1 synthetic reaction device processed, is characterized in that: described reactor shell and described atmosphere storage district removably connect.
4. methane chemical chain reformation according to claim 3 synthetic reaction device processed, is characterized in that: reactor shell and described atmosphere storage district pass through Flange joint.
5. methane chemical chain reformation according to claim 1 synthetic reaction device processed, is characterized in that: described reactor shell and described plenum zone removably connect.
6. methane chemical chain reformation according to claim 5 synthetic reaction device processed, is characterized in that: described reactor shell and described plenum zone pass through Flange joint.
7. methane chemical chain reformation according to claim 1 synthetic reaction device processed, is characterized in that: described reactor shell is outside equipped with heating unit.
8. methane chemical chain reformation according to claim 1 synthetic reaction device processed, is characterized in that: described cellular oxygen carrier is selected from La
0.7sr
0.3mnO
3, La
0.7sr
0.3niO
3and LaFeO
3in one.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201520880921.1U CN205115038U (en) | 2015-11-05 | 2015-11-05 | Synthetic reaction unit of methane chemistry chain system of reforming |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201520880921.1U CN205115038U (en) | 2015-11-05 | 2015-11-05 | Synthetic reaction unit of methane chemistry chain system of reforming |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN205115038U true CN205115038U (en) | 2016-03-30 |
Family
ID=55570663
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201520880921.1U Active CN205115038U (en) | 2015-11-05 | 2015-11-05 | Synthetic reaction unit of methane chemistry chain system of reforming |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN205115038U (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108855109A (en) * | 2018-07-02 | 2018-11-23 | 西北大学 | A kind of chemical chain partial oxidation methane preparing synthetic gas carrier of oxygen and its preparation method and application |
| CN113880047A (en) * | 2021-11-08 | 2022-01-04 | 深圳市英策科技有限公司 | Hydrogen production device and method for methane-containing raw material |
| CN114408865A (en) * | 2022-03-01 | 2022-04-29 | 浙江浙能技术研究院有限公司 | Chemical chain methane reforming hydrogen production device |
-
2015
- 2015-11-05 CN CN201520880921.1U patent/CN205115038U/en active Active
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108855109A (en) * | 2018-07-02 | 2018-11-23 | 西北大学 | A kind of chemical chain partial oxidation methane preparing synthetic gas carrier of oxygen and its preparation method and application |
| CN108855109B (en) * | 2018-07-02 | 2020-12-15 | 西北大学 | Synthetic gas oxygen carrier prepared by oxidizing methane with chemical chain part and preparation method and application thereof |
| CN113880047A (en) * | 2021-11-08 | 2022-01-04 | 深圳市英策科技有限公司 | Hydrogen production device and method for methane-containing raw material |
| CN113880047B (en) * | 2021-11-08 | 2024-04-09 | 深圳市英策科技有限公司 | Hydrogen production device and method for methane-containing raw material |
| CN114408865A (en) * | 2022-03-01 | 2022-04-29 | 浙江浙能技术研究院有限公司 | Chemical chain methane reforming hydrogen production device |
| CN114408865B (en) * | 2022-03-01 | 2023-01-17 | 浙江浙能技术研究院有限公司 | Chemical chain methane reforming hydrogen production device |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| KR102290845B1 (en) | Method and equipment for the production of nitric acid | |
| CN103373706B (en) | A kind of methane reforming hydrogen production process and device | |
| CN103204464A (en) | Cellular oxygen carrier chemical-looping reforming reactor | |
| CN100491235C (en) | Circulation fluid bed hydrogen preparation reaction technology and reaction device by reforming methane and water steam | |
| CN102408097A (en) | Process and apparatus for thermally integrated hydrogen generation system | |
| CN205115038U (en) | Synthetic reaction unit of methane chemistry chain system of reforming | |
| CN113461027B (en) | Low-pressure synthetic ammonia tower and renewable energy source low-pressure synthetic ammonia system | |
| CN211998798U (en) | Skid-mounted mobile on-site hydrogen production all-in-one machine | |
| CN112569739B (en) | System and method for capturing carbon dioxide at high temperature and converting carbon dioxide into synthesis gas in situ | |
| CN103086325A (en) | Natural gas hydrogen production reactor and hydrogen production process thereof | |
| CN110156047A (en) | A kind of synthesis ammonia method of solid oxide electrolyte/fossil fuel synthesis ammonia coupling | |
| CN100553020C (en) | A kind of solid-oxide fuel cell stack biogas systemic circulatory system and method | |
| CN113005475B (en) | System and process for solar high-temperature water electrolysis coupling hydrogen production based on amino thermochemical energy storage | |
| CN105314596A (en) | Method and device for preparing synthesis gas through methane and carbon dioxide auto-thermal reforming | |
| CN102921355B (en) | A kind of calandria type fixed bed reactor and coal bed gas deoxidation method | |
| CN204848257U (en) | Device of methane catalytic cracking production hydrogen | |
| CN109095438B (en) | Biomass multistage conversion combined hydrogen production device and working method thereof | |
| CN101745350B (en) | Device for by-product steam catalytic reaction | |
| CN102452641B (en) | Method for recovering Fischer-Tropsch synthesis technology purge gas | |
| CN105542889A (en) | Quenching type methanation process with heat removing internally | |
| CN113479905B (en) | Self-deoxidization ammonia synthesis tower and renewable energy source ammonia synthesis system | |
| CN106946637B (en) | A kind of device and technique of skid-mounted type lower carbon number hydrocarbons production methane | |
| CN105561739A (en) | Apparatus and method for enriching and converting CO2 in closed space | |
| CN201501787U (en) | Device utilizing lattice oxygen to partially oxidize natural gas to prepare synthetic gas | |
| CN102952596B (en) | Process and device for synthesizing natural gas through methanation based on slurry bed |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant |