CN107460013B - Process for preparing natural gas through methanation of synthesis gas fluidized bed based on interstage dehydration - Google Patents
Process for preparing natural gas through methanation of synthesis gas fluidized bed based on interstage dehydration Download PDFInfo
- Publication number
- CN107460013B CN107460013B CN201710455223.0A CN201710455223A CN107460013B CN 107460013 B CN107460013 B CN 107460013B CN 201710455223 A CN201710455223 A CN 201710455223A CN 107460013 B CN107460013 B CN 107460013B
- Authority
- CN
- China
- Prior art keywords
- gas
- methanation
- fluidized bed
- heat
- pipe
- 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.)
- Expired - Fee Related
Links
- 239000007789 gas Substances 0.000 title claims abstract description 66
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 title claims abstract description 52
- 238000003786 synthesis reaction Methods 0.000 title claims abstract description 21
- 230000015572 biosynthetic process Effects 0.000 title claims abstract description 20
- 230000018044 dehydration Effects 0.000 title claims abstract description 18
- 238000006297 dehydration reaction Methods 0.000 title claims abstract description 18
- 239000003345 natural gas Substances 0.000 title claims abstract description 12
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 10
- 238000006243 chemical reaction Methods 0.000 claims abstract description 55
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 34
- 239000003054 catalyst Substances 0.000 claims abstract description 32
- 238000000034 method Methods 0.000 claims abstract description 29
- 238000000605 extraction Methods 0.000 claims abstract description 21
- 208000005156 Dehydration Diseases 0.000 claims abstract description 17
- 239000007787 solid Substances 0.000 claims abstract description 16
- 239000007788 liquid Substances 0.000 claims abstract description 10
- 239000000843 powder Substances 0.000 claims abstract description 8
- 238000001816 cooling Methods 0.000 claims abstract description 4
- 229920006395 saturated elastomer Polymers 0.000 claims description 9
- 239000000498 cooling water Substances 0.000 claims description 8
- 230000001105 regulatory effect Effects 0.000 claims description 6
- 239000000463 material Substances 0.000 claims description 4
- 238000000926 separation method Methods 0.000 claims 1
- 239000012495 reaction gas Substances 0.000 abstract description 3
- 239000000047 product Substances 0.000 description 23
- 230000036961 partial effect Effects 0.000 description 4
- 239000002002 slurry Substances 0.000 description 4
- 239000003245 coal Substances 0.000 description 3
- 238000005265 energy consumption Methods 0.000 description 3
- 239000007791 liquid phase Substances 0.000 description 3
- 238000002360 preparation method Methods 0.000 description 3
- 239000002994 raw material Substances 0.000 description 3
- 238000012546 transfer Methods 0.000 description 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 238000012360 testing method Methods 0.000 description 2
- 238000003809 water extraction Methods 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 230000006835 compression Effects 0.000 description 1
- 238000007906 compression Methods 0.000 description 1
- 230000001276 controlling effect Effects 0.000 description 1
- 208000012839 conversion disease Diseases 0.000 description 1
- 238000005336 cracking Methods 0.000 description 1
- 238000005520 cutting process Methods 0.000 description 1
- 230000003247 decreasing effect Effects 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000007865 diluting Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005243 fluidization Methods 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 230000002401 inhibitory effect Effects 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 239000012071 phase Substances 0.000 description 1
- 238000001556 precipitation Methods 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 230000001737 promoting effect Effects 0.000 description 1
- 230000002829 reductive effect Effects 0.000 description 1
- 238000013341 scale-up Methods 0.000 description 1
- 230000009919 sequestration Effects 0.000 description 1
- 238000003860 storage Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 239000002918 waste heat Substances 0.000 description 1
Images
Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
- C10L3/06—Natural gas; Synthetic natural gas obtained by processes not covered by C10G, C10K3/02 or C10K3/04
- C10L3/08—Production of synthetic natural gas
Landscapes
- Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
Abstract
The invention provides a process for preparing natural gas by methanation of a synthetic gas fluidized bed based on interstage dehydration, which is used for converting CO/H2The purified synthesis gas with the ratio of 1:3 enters a first-stage fluidized bed reactor with a heat extraction pipe, and part of CO and/H2With a micro powder methanation catalyst at 240-Performing heat exchange at 500 deg.C and 0.3-6.0Mpa by heat-taking pipe to perform uniform temperature methanation reaction to generate methane and water vapor, removing catalyst from product gas by gas-solid separator, cooling by water cooler, and allowing the product gas to enter into gas-liquid cyclone dehydrator; the dehydrated product gas enters a second-stage fluidized bed reactor with a heat taking pipe, and the process is repeated; after the product gas after secondary dehydration enters a three-stage fluidized bed reactor with a heat extraction pipe again, CO and/H2Performing heat exchange with the micro powder methanation catalyst at 500 ℃ and 0.3-6.0Mpa by a heat-taking pipe to generate a temperature-equalizing methanation reaction, and enabling the product gas to enter a water cooler to regulate and control the temperature after the catalyst is removed by a gas-solid separator; and the third-stage reaction gas directly enters a fixed bed methanation reactor to regulate and control the product quality of the synthetic natural gas.
Description
1. Field of the invention
The invention provides a process for preparing natural gas by methanation of a synthetic gas fluidized bed based on interstage dehydration, and belongs to the field of coal chemical industry.
2. Background of the invention
The synthesis gas is obtained by gasifying the coal, the preparation of the natural gas by methanation of the synthesis gas is an important way for clean conversion of the coal, is an important means for optimizing an energy structure and guaranteeing energy safety in China, is an effective means for relieving local atmospheric pollution, and has certain competitiveness, which promotes the vigorous development of the coal-to-natural gas industry.
The raw material gas for methanation reaction of synthetic gas mainly contains H2、CO、CO2、CH4、H2O、N2And Ar and the like, and 11 chemical reactions possibly occur in the methanation process, wherein the main reactions are CO methanation reaction and CO2Methanation reaction, CO shift reaction, etc.
Methanation of CO to CO +3H2＝CH4+H2O，CO2Methanation to CO2+4H2＝CH4+2H2CO + H shift reaction site of O, CO2O＝H2+CO2Methanation of CO, CO2The methanation reaction is the positive reaction for promoting the generation of methane, and the CO shift reaction site is CO + H2O＝H2+CO2The method is a negative reaction for inhibiting the generation of methane, and the removal of generated water in the methanation reaction process of the synthesis gas is beneficial to improving the methanation conversion rate and the selectivity. In addition, methanation of CO and CO2Methanation reactions are strongly exothermic, typically with a 74 ℃ temperature rise for every 1% conversion of CO and 1% conversion of CO2An exotherm of 60 ℃ can be produced and the higher the reaction temperature, the lower the CO conversion and the higher the demand on the methanation catalyst.
Since the discovery of methanation of CO, methanation is widely used in the ammonia synthesis industry, in the removal of trace amounts of CO, in fuel cells, in the methanation of part of gas and in the production of synthetic natural gas. Since the 40 s in the 20 th century, people developed various methanation processes in turn, which can be divided into adiabatic fixed bed, isothermal fixed bed, fluidized bed and liquid phase methanation processes according to the type of a reactor.
In the methanation process of the adiabatic fixed bed, the adiabatic temperature rise of the methanation reaction of the synthesis gas directly occurs, the temperature of the outlet of the reactor exceeds 900 ℃, which puts high requirements on the materials of the reactor, a waste heat boiler, a steam superheater and a pipeline and the high temperature resistance of the catalyst, and the methane is easy to generate cracking reaction for carbon precipitation at high temperature, thereby increasing the bed pressure drop and reducing the service life of the catalyst. In order to effectively control the temperature rise of the reactor, the temperature rise of the reactor is generally realized by diluting the raw material gas, and the alternative modes comprise partial high-proportion circulation of process gas, partial circulation of process gas, addition of a small amount of steam, addition of partial steam and the like, so that the methanation reaction balance under the descending temperature is realized, and finally the synthetic natural gas is obtained through multistage methanation reactions. The high proportion of the process gas recycle increases the compression energy consumption and investment.
The fixed bed indirect heat exchange isothermal methanation reactor has heat transferring cold pipe embedded into the catalyst bed layer, and isothermal fixed bed methanation process is developed based on the isothermal methanation reactor. The isothermal fixed bed methanation reactor can generate byproduct steam by virtue of heat released by methanation reaction. However, the size of the apparatus is limited due to structural limitations.
Compared with a fixed bed reactor, the fluidized bed reactor has the advantages of great mass transfer and heat transfer, is more suitable for large-scale strong heat release process, particularly is easy to remove, add and recycle the fluidized bed catalyst, has the advantages of good reaction effect, simple operation, lower operation cost and the like, and is the best reactor for complete methanation of the synthesis gas. But also face problems, especially engineering scale-up problems, such as severe catalyst entrainment and loss, difficult control of reaction temperature, low unit operating pressure, relatively low reaction conversion, large catalyst replacement, and the like, which results in the need for inexpensive catalysts.
The slurry bed methanation process is characterized in that a catalyst and a liquid phase component carried in mixed gas generated in a slurry bed reactor are separated by a gas-liquid separator, a gas phase product is condensed and separated to produce synthetic natural gas, and the liquid phase product and a fresh catalyst in a storage tank are mixed and added into the slurry bed methanation reactor to preheat the fresh catalyst. The slurry bed methanation process has good heat transfer performance, is easy to realize low-temperature operation and has higher CH4Selectivity and better flexibility, but lower CO conversion and greater catalyst loss due to process liquid sequestration.
The key point of improving the competitiveness of the synthesis gas methanation process is how to control the reaction temperature within a reasonable range, fully utilize the methanation reaction heat, improve the methanation conversion rate and selectivity and reduce the process energy consumption by selecting a proper reactor.
3. Summary of the invention
The invention aims to overcome the defects of the existing synthesis gas methanation technology, provide the synthesis gas fluidized bed methanation natural gas preparation process based on interstage dehydration, reduce the heat extraction load of a fluidized bed heat extraction pipe through a staged reaction, and improve the effective reaction sectional area of the fluidized bed; interstage dehydration inhibits the negative reaction of methanation reaction, and greatly improves the methanation conversion rate and selectivity; finally, residual CO and H are solved through a fixed bed methanation reactor2The high-efficiency reaction of the method can regulate and control the product quality.
The technical scheme of the invention is as follows:
the invention aims to reduce the energy consumption and investment of methane preparation from synthesis gas by integrating the technologies of synthesis gas fluidized bed methanation, staged reaction regulation and control of heat extraction, interstage dehydration regulation and control of conversion rate and selectivity, independent disconnection of heat extraction pipes and the like, and ensure stable, long, full and excellent operation of a methanation device. It is characterized in that the CO/H after conversion2The purified synthesis gas with the ratio of 1:3 enters a first-stage fluidized bed reactor with a heat extraction pipe, and part of CO and/H2Performing heat exchange with the micro powder methanation catalyst at 500 ℃ and 0.3-6.0Mpa by a heat-taking pipe to perform temperature-equalizing methanation reaction to generate methane and water vapor, removing the catalyst from the product gas by a gas-solid separator, cooling by a water cooler, and introducing into a gas-liquid cyclone dehydrator; the dehydrated product gas enters a second-stage fluidized bed reactor with a heat taking pipe, and the process is repeated; after the product gas after secondary dehydration enters a three-stage fluidized bed reactor with a heat extraction pipe again, CO and/H2Performing heat exchange with the micro powder methanation catalyst at 500 ℃ and 0.3-6.0Mpa by a heat taking pipe to generate a temperature equalizing methanation reaction, and regulating the temperature of the product gas by a water cooler after the catalyst is removed by a gas-solid separator; in the methanation process of each stage of fluidized bed, cooling water firstly exchanges heat through a water cooler and then enters a heat extraction pipe for heat exchange to generate medium-high pressure saturated steam; and the third-stage reaction gas directly enters a fixed bed methanation reactor, the product quality of the synthetic natural gas is regulated and controlled, and the generated product gas is dehydrated and then sent into a pipe network.
A gas-solid separator is arranged at the upper part in the fluidized bed reactor with the heat taking pipe, a solid dipleg with a wing valve extends into the middle part of the catalyst material layer, and a gas outlet extends out of the fluidized bed reactor; the top of the fluidized bed reactor is provided with heat extraction pipes which are uniformly distributed along the circumference, and a cooling water inlet and a high-temperature saturated water outlet of each heat extraction pipe are respectively and independently connected with a cold water extraction pipe and a steam drum through valves.
The heat taking pipe is of a sleeve structure with the bottom of the inner pipe communicated and the top sealed, cooling water enters the top of the central pipe, and high-temperature saturated water exits from the top of the ring pipe.
The outlet at the lower part of the gas-liquid cyclone dehydrator is provided with two stages of lock hoppers, and the lower ends of the lock hoppers are respectively provided with a lock hopper valve.
The temperature of the product gas after passing through the first and second water coolers is 30-150 ℃, and the temperature of the product gas after passing through the water cooler of the temperature-regulating cross-line valve at the third stage is 250-400 ℃.
The present invention will be described in detail with reference to examples.
4. Description of the drawings
FIG. 1 is a schematic process diagram of the present invention.
The drawing of FIG. 1 is set forth below:
1. a fluidized bed reactor 2 with a first-stage heat taking pipe, a gas distributor 3, a gas-solid separator 4, a water cooler 5, a gas-liquid cyclone dehydrator 6, a lock hopper 7, a lock hopper valve 8, a heat taking pipe 9, a fluidized bed reactor with a second-stage heat taking pipe, a fluidized bed reactor 10 with a third-stage heat taking pipe, a fixed bed reactor 12, a stop valve 13, a saturated steam water bag 14, a temperature-adjusting crossover valve 15, a product gas outlet
The process features of the present invention are described in detail below with reference to the accompanying drawings and examples.
5. Detailed description of the preferred embodiments
Example, post-shift CO/H2The purified synthesis gas with the ratio of 1:3 is sent into a first-stage fluidized bed reactor (1) with a heat extraction pipe through a gas distributor (2), and part of CO and/or H2The product gas and the micro powder methanation catalyst are subjected to heat exchange at the temperature of 240 ℃ and 500 ℃ and under 0.3-6.0Mpa by a heat taking pipe (8) to generate a temperature equalizing methanation reaction to generate methane and water vapor, and the product gas is cooled by a water cooler (4) after the catalyst is removed by a gas-solid separator (3) and enters a gas-liquid cyclone dehydrator (5); the dehydrated product gas enters a second-stage fluidized bed reactor (9) with a heat extraction pipe, and the process is repeated; the product gas after secondary dehydration enters a three-stage fluidized bed reactor (10) with a heat extraction pipe again, and then CO and/H2The catalyst and the micro powder methanation catalyst are subjected to heat exchange at the temperature of 240 ℃ and 500 ℃ and under the pressure of 0.3-6.0Mpa through a heat taking pipe (8) to generate a temperature equalizing methanation reaction, and the temperature of the product gas is regulated and controlled through a temperature regulating cross-line valve (14) of a water cooler (4) after the catalyst of the product gas is removed through a gas-solid separator (3); in the methanation process of each stage of fluidized bed, cooling water firstly exchanges heat through a water cooler (4) and then enters a heat extraction pipe (8) for heat exchange to generate medium-high pressure saturated steam; the third-stage reaction gas directly enters a methanation fixed bed reactor (11), the product quality of the synthetic natural gas is regulated, and the generated product gas is dehydrated through a product gas outlet (15) and then sent to a pipe network.
A gas-solid separator (3) is arranged at the upper part in the fluidized bed reactor with the heat taking pipe (8), a solid dipleg with a wing valve extends into the middle part of the catalyst material layer, and a gas outlet extends out of the fluidized bed reactor; the top of the fluidized bed reactor is provided with heat extraction pipes (8) which are uniformly distributed along the circumference, and a cooling water inlet and a high-temperature saturated water outlet of each heat extraction pipe (8) are respectively and independently connected with a cold water extraction pipe and a steam pocket through valves through stop valves (12).
The heat taking pipe (8) is of a sleeve structure with the bottom of the inner pipe communicated and the top sealed, cooling water enters the top of the central pipe, and high-temperature saturated water exits from the top of the ring pipe.
The outlet at the lower part of the gas-liquid cyclone dehydrator (5) is provided with two stages of lock hoppers (6), and the lower ends of the lock hoppers are respectively provided with a lock hopper valve (7).
The temperature of the product gas after the first and second water coolers (4) is 30-150 ℃, and the temperature of the product gas after the third stage passes through the water cooler (4) of the temperature-regulating cross-line valve (14) is 250-400 ℃.
In addition, the process can adapt to the change of the raw material composition of different syntheses by increasing or decreasing the number of reaction stages, mainly the number of dehydration stages.
According to the process for preparing the natural gas through methanation of the synthetic gas fluidized bed based on interstage dehydration, the heat taking load of the heat taking pipes of the fluidized bed is reduced through the staged reaction, the total sectional area of the heat taking pipes is less than 13% of the sectional area of the fluidized bed, the fluidization quality is ensured, and the effective reaction area of the fluidized bed is improved; interstage dehydration inhibits the negative reaction of methanation reaction, the CO conversion rate is more than 99%, and the methanation selectivity is more than 99%; finally, residual CO and H are solved through a fixed bed methanation reactor2The methane content of the natural gas is more than 99.6 percent; compared with the existing fixed bed partial circulation methanation industrialization process, the method saves energy by 35 percent and saves investment by 30 percent; compared with a fluidized bed methanation test or a pilot plant test process, the conversion rate is improved by 15%, the selectivity is improved by 10%, the design and the processing of the fluidized bed reactor are simplified by extracting and controlling the heat intensity through the grading reaction, and the stable, long, full and excellent operation of the production is not influenced by only cutting off a top stop valve when a single heat extraction pipe fails.
Claims (3)
1. The process for preparing natural gas by methanation of synthetic gas in fluidized bed based on interstage dehydration is technically characterized by converting CO/H2The purified synthesis gas with the ratio of 1:3 enters a first-stage fluidized bed reactor with a heat extraction pipe, and part of CO and H2 and the micro powder methanation catalyst are heated at the temperature of 240-500 ℃ and the pressure of 0.3-6.0MPaPerforming heat exchange in the pipe to generate a temperature-equalizing methanation reaction to generate methane and water vapor, and cooling the product gas by a water cooler after removing the catalyst by a gas-solid separator to enter a gas-liquid cyclone dehydrator; the dehydrated product gas enters a second-stage fluidized bed reactor with a heat taking pipe, and the processes of the fluidized bed methane synthesis, the gas-solid separation and the cooling dehydration are repeated; after the product gas after secondary dehydration enters a three-stage fluidized bed reactor with a heat extraction pipe again, CO, H2 and the micro powder methanation catalyst are subjected to heat exchange at 500 ℃ and 0.3-6.0MPa through the heat extraction pipe to generate a temperature equalization methanation reaction, and the product gas is subjected to catalyst removal through a gas-solid separator and then is subjected to temperature regulation and control through a water cooler; the top of the fluidized bed reactor is provided with heat taking pipes which are uniformly distributed along the circumference, the heat taking pipes are of a sleeve structure with communicated inner pipe bottoms and closed top, cooling water enters the top of the central pipe, high-temperature saturated water exits from the top of the ring pipe, and the water inlet and outlet of each heat taking pipe are independently controlled by a valve; in the methanation process of each stage of fluidized bed, cooling water firstly exchanges heat through a water cooler and then enters a heat taking pipe for heat exchange, and medium-high pressure saturated steam is generated through a steam drum; the temperature of the product gas after the first-stage water cooler and the second-stage water cooler is 30-150 ℃, the product gas at the temperature of 250-400 ℃ after passing through the third-stage water cooler of the temperature-regulating cross-line valve directly enters a fixed bed methanation reactor, the product quality of the synthetic natural gas is regulated, and the generated product gas is dehydrated and then sent to a pipe network.
2. The process for preparing natural gas through methanation of the synthesis gas fluidized bed based on interstage dehydration as claimed in claim 1, wherein a gas-solid separator is arranged at the upper part in the fluidized bed reactor with the heat taking pipe, a solid dipleg with a wing valve extends into the middle of the catalyst material layer, and a gas outlet extends out of the fluidized bed reactor.
3. The process for preparing natural gas through methanation of the synthesis gas fluidized bed based on interstage dehydration as claimed in claim 1, wherein the lower outlet of the gas-liquid cyclone dehydrator is provided with two-stage lock hoppers, and the lower ends of the lock hoppers are respectively provided with a lock hopper valve.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201710455223.0A CN107460013B (en) | 2017-06-16 | 2017-06-16 | Process for preparing natural gas through methanation of synthesis gas fluidized bed based on interstage dehydration |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201710455223.0A CN107460013B (en) | 2017-06-16 | 2017-06-16 | Process for preparing natural gas through methanation of synthesis gas fluidized bed based on interstage dehydration |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN107460013A CN107460013A (en) | 2017-12-12 |
| CN107460013B true CN107460013B (en) | 2020-09-15 |
Family
ID=60546369
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201710455223.0A Expired - Fee Related CN107460013B (en) | 2017-06-16 | 2017-06-16 | Process for preparing natural gas through methanation of synthesis gas fluidized bed based on interstage dehydration |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN107460013B (en) |
Families Citing this family (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110283205B (en) * | 2018-03-19 | 2021-03-23 | 浙江新安化工集团股份有限公司 | System and method for preparing methylphosphonite |
| CN110283202B (en) * | 2018-03-19 | 2021-03-23 | 浙江新安化工集团股份有限公司 | System and method for preparing methylphosphonite from aluminum methylchloride |
Family Cites Families (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| FR2875237B1 (en) * | 2004-09-10 | 2007-07-27 | Total Sa | PROCESS AND INSTALLATION FOR EXTRACTING MERCAPTANS FROM A GASEOUS MIXTURE OF HYDROCARBONS |
| CN101817716B (en) * | 2009-02-27 | 2013-05-01 | 中国科学院过程工程研究所 | Method and device for catalyzing methanation of synthesis gas |
| CN103242921B (en) * | 2012-02-09 | 2014-12-10 | 中国科学院大连化学物理研究所 | Technology for preparing natural gas from synthetic gas |
| CN103695058B (en) * | 2013-12-19 | 2015-05-20 | 中国海洋石油总公司 | Novel methanation reaction process for preparing synthetic natural gas |
| CN105255532B (en) * | 2015-11-06 | 2018-04-06 | 中国海洋石油总公司 | The methanation process that a kind of fluid bed is combined with fixed bed |
-
2017
- 2017-06-16 CN CN201710455223.0A patent/CN107460013B/en not_active Expired - Fee Related
Also Published As
| Publication number | Publication date |
|---|---|
| CN107460013A (en) | 2017-12-12 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| RU2583785C1 (en) | Method and system for efficient combined-cycle cogeneration based on gasification and methanation of biomass | |
| CN101704513B (en) | Shunting-type isothermal sulfur-tolerant conversion process and equipment thereof | |
| CN105385473B (en) | A kind of technique of coal hydrogen and methane based on chemical chain gasification | |
| CN110550601B (en) | Transformation process for high-concentration CO raw material gas | |
| CN101649233A (en) | Isothermal methanation process and device for the preparation of synthetic natural gas | |
| CN107460013B (en) | Process for preparing natural gas through methanation of synthesis gas fluidized bed based on interstage dehydration | |
| CN104192798A (en) | Adiabatic-isothermal shift technique for high-concentration CO raw gas | |
| CN111234876A (en) | Material grading preheating and overtemperature protection system and method for supercritical water gasification hydrogen production | |
| CN207672007U (en) | Based on the synthesis gas fluid bed preparing natural gas by methanation device being dehydrated between grade | |
| CN105255532B (en) | The methanation process that a kind of fluid bed is combined with fixed bed | |
| CN107129844B (en) | Process for preparing natural gas by methanation of synthesis gas fluidized bed | |
| CN105132056A (en) | Process and system for producing natural gas through lignite steam hydrogasification | |
| CN104645898A (en) | Trickle-bed reaction device and process for synthetic gas methanation | |
| CN109054908B (en) | Isothermal transformation process matched with pulverized coal gasification | |
| CN109279573B (en) | Isothermal transformation process matched with coal water slurry gasification | |
| CN201436296U (en) | Isothermal methanation device for preparing synthesized natural gas | |
| CN107090320B (en) | Device for preparing natural gas by methanation of synthetic gas fluidized bed based on interstage dehydration | |
| CN108018088A (en) | A kind of method of catalytic coal gasifaction | |
| CN107090319B (en) | Device for preparing natural gas by methanation of synthetic gas fluidized bed | |
| CN111621340B (en) | High-efficiency catalytic gasification system and method for coal | |
| CN109665492A (en) | High water-gas ratio raw gas combined transformation technique | |
| CN111718760B (en) | Sulfur-tolerant methanation system and method for coal-based natural gas | |
| CN109280568B (en) | Isothermal transformation process matched with pulverized coal gasification | |
| CN107164007A (en) | A kind of method of non-stoichiometric isothermal synthetic natural gas | |
| CN205011719U (en) | Trickle bed reaction unit of synthetic gas methanation |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20200915 |