CN113477190A - Method for preparing methane gas from solid waste in two-stage mode - Google Patents
Method for preparing methane gas from solid waste in two-stage mode Download PDFInfo
- Publication number
- CN113477190A CN113477190A CN202110666308.XA CN202110666308A CN113477190A CN 113477190 A CN113477190 A CN 113477190A CN 202110666308 A CN202110666308 A CN 202110666308A CN 113477190 A CN113477190 A CN 113477190A
- Authority
- CN
- China
- Prior art keywords
- methanation
- methane gas
- region
- catalyst
- solid waste
- 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
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
- B01J8/24—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
- B01J8/24—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique
- B01J8/26—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique with two or more fluidised beds, e.g. reactor and regeneration installations
- B01J8/28—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique with two or more fluidised beds, e.g. reactor and regeneration installations the one above the other
-
- 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
-
- 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
- C10L2200/00—Components of fuel compositions
- C10L2200/04—Organic compounds
- C10L2200/0461—Fractions defined by their origin
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E50/00—Technologies for the production of fuel of non-fossil origin
- Y02E50/30—Fuel from waste, e.g. synthetic alcohol or diesel
Abstract
The invention discloses a method for preparing methane gas by solid waste in a two-stage mode, which comprises the following steps: step 10) in a primary methanation region, introducing steam from the bottom, introducing solid waste and a modified calcium-based ore catalyst from the side, mixing the solid waste and the modified calcium-based ore catalyst upwards under the action of the steam, and performing direct methanation reaction with the steam to obtain crude methane gas; step 20) discharging the crude methane gas from the top of the primary methanation region, allowing the crude methane gas to enter a secondary methanation region, allowing the hydrogen gas to uniformly enter the secondary methanation region, and pre-modulating the hydrogen-carbon ratio of the crude methane gas; the catalytic methanation catalyst is used for carrying out catalytic methanation reaction on the methane gas, and the high-quality methane gas is obtained under the fluidization action of the hydrogen and the crude methane gas. The method can realize the effects of high fuel utilization rate, high methane quality and low catalysis cost.
Description
Technical Field
The invention belongs to the technical field of natural gas preparation by utilizing solid wastes as resources, and discloses a method for preparing methane gas by using solid wastes in a two-stage manner.
Background
Methane has received a great deal of attention as a highly efficient clean energy source for its synthesis and utilization. The process route for preparing methane can be divided into two main categories of indirect methanation and direct methanation. In the indirect methanation process, raw materials sequentially pass through a synthesis gas unit, a cleaning and purifying unit and a catalytic methanation synthesis unit to prepare methane; in the direct methanation process, the methanogenic process of the feedstock is integrated into one operational unit, thereby producing a methane-rich gas directly from the feedstock.
In the methanation process, fuels such as coal, biomass and the like are widely adopted, while solid wastes which are solid fuels have wide sources and are rich in hydrogen elements, and can be theoretically used as raw materials of the methanation process, but at present, the fuels are not widely adopted due to complex components.
The complex components and high temperature uniformity of the raw materials of the reactor lead to extremely complex competition and coupling mechanisms among gasification reaction, water-gas shift reaction and methanation reaction in the methanation process. Specifically, the solid waste as the raw material has heterogeneous, multi-component characteristics, so that it is difficult to have a uniform rule in terms of quantification of products (coke, volatiles, tar) at the initial stage of the reaction, thereby causing excessive disproportionated carbon deposition reaction and excessive tar byproduct generation due to the difference of the species and quantity of the reactants during the subsequent reaction, resulting in premature deactivation of the catalyst and reduction of methane yield. Meanwhile, because the temperature difference in the reactor is small, the respective optimal temperature requirements of the gasification reaction, the water-gas shift reaction and the methanation reaction are difficult to meet at the same time, so that the complex competition and coupling relation of the three reactions inevitably exists, and the yield and the quality of methane are further influenced.
The reaction components involved in the direct methanation process of the solid waste are complex, and meanwhile, the raw materials can also produce sulfur-containing gas, so that more gas-solid heterogeneous catalytic reactions exist in the reactor, the catalyst is easy to inactivate in advance, and the service life of the catalyst is shortened.
Disclosure of Invention
The technical problem is as follows: the invention provides a method for preparing methane gas by solid wastes in a two-stage mode, aims to overcome the challenges of complex coupling of reaction processes and early catalyst deactivation of solid wastes serving as methanation process fuels, provides a new solution for reduction and resource utilization of the solid wastes, and achieves the purposes of high fuel utilization rate, high methane quality and low catalysis cost.
The technical scheme is as follows: in order to solve the technical problem, the embodiment of the invention adopts the following technical scheme:
a method for preparing methane gas by solid waste in a two-stage mode comprises the following steps:
step 10) in a primary methanation region in a two-stage methanation reactor, introducing water vapor serving as a fluidizing medium and a methyl alkylating agent from the bottom of the primary methanation region, introducing solid waste serving as fuel and a modified calcium-based ore catalyst serving as a direct methanation catalyst from the side of the primary methanation region, mixing the solid waste and the modified calcium-based ore catalyst upwards under the action of the water vapor to form bubbling fluidization motion, and performing direct methanation reaction with the water vapor to obtain crude methane gas;
step 20) discharging the crude methane gas from the top of the primary methanation region, allowing the crude methane gas to enter a secondary methanation region, allowing hydrogen gas to uniformly enter the secondary methanation region from one side of the bottom of the secondary methanation region, and pre-modulating the hydrogen-carbon ratio of the crude methane gas; in the secondary methanation region, the catalytic methanation catalyst is used for carrying out catalytic methanation reaction on the methane gas, the catalytic methanation catalyst is in rapid fluidized motion under the fluidization action of the hydrogen and the crude methane gas, and the catalytic methanation reaction is carried out to obtain the high-quality methane gas.
Preferably, the modified calcium-based ore catalyst is: the calcium-based ore is used as a carrier, and any one or more metal components in K, Fe are loaded.
Preferably, the catalytic methanation catalyst is one or more of nickel-based, iron-based and molybdenum-based catalysts with high methane conversion rate.
Preferably, the particle size of the modified calcium-based ore catalyst is larger than that of the solid waste, and the particle size of the solid waste is larger than that of the catalytic methanation catalyst.
Preferably, the two-stage methanation reactor is an integrated device and is divided into a first-stage methanation region and a second-stage methanation region, and the first-stage methanation region is located below the second-stage methanation region.
Preferably, the diameter of the primary methanation region is larger than that of the secondary methanation region, and the primary methanation region is connected with the secondary methanation region through a reducer.
Preferably, a distribution plate is arranged in the reducing pipe to separate the first-stage methanation region from the second-stage methanation region.
Has the advantages that: compared with the traditional solid waste treatment method, the method has the following advantages:
(1) the method couples direct methanation and catalytic methanation, realizes quality improvement and yield increase of the gas produced by the solid fuel, obtains the methane gas with high quality and high yield, and realizes reduction and resource utilization of the solid waste.
(2) According to the invention, the methanation reactor is designed into an integrated two-section type shape and is divided into a primary methanation region and a secondary methanation region, so that the coupling of two methanation processes in the same reactor is realized, and the unification among the high efficiency of reaction, the simplicity of a system and the operation controllability is realized.
(3) The invention provides a novel method for graded catalysis, which realizes stronger adsorption of impurity gas in the reaction process in a primary methanation region, ensures clean reaction atmosphere purification of a secondary methanation region and reduces the inactivation risk of a catalytic methanation catalyst; the deep quality improvement of the crude methane gas is realized in the secondary methanation region, the methane conversion efficiency is obviously improved, the gas production quality is improved, a methanation treatment method aiming at complex components of solid wastes is provided, and the deep methanation utilization of the solid wastes is realized.
(4) The invention provides a new concept of a cheap-efficient binary catalyst system, and a low-cost modification technology is adopted for cheap calcium-based ores to serve as a direct methanation catalyst in a primary methanation region, so that the direct methanation catalyst has moderate direct methanation catalytic activity. Correspondingly, a noble metal is selected as the active component of the catalyst in the secondary methanation region, and the catalyst has good catalytic activity by an advanced loading technology, so that the long service life of the catalyst is ensured, and the balance between the gas production requirement and the economic cost is realized.
Drawings
FIG. 1 is a schematic structural diagram of a two-stage methanation reactor of the present invention.
The figure shows that: the system comprises a primary methanation region 1, a secondary methanation region 2, water vapor A, solid waste particles B, a direct methanation catalyst C, crude methane gas D, hydrogen E, a catalytic methanation catalyst F and high-quality methane gas G.
Detailed Description
The method for preparing methane gas in two stages by using solid waste of the patent is described in detail below with reference to figure 1,
as shown in fig. 1, the method for two-stage preparation of methane gas from solid waste according to the embodiment of the present invention includes the following steps:
step 10) in a primary methanation region 1 in a two-stage methanation reactor, introducing water vapor A serving as a fluidizing medium and a methyl alkylating agent from the bottom of the primary methanation region 1, introducing solid waste B serving as fuel and a modified calcium-based ore catalyst C serving as a direct methanation catalyst from the side edge of the primary methanation region 1, mixing the solid waste B and the modified calcium-based ore catalyst C upwards under the action of the water vapor A to form bubbling fluidization motion, and performing direct methanation reaction with the water vapor A to obtain crude methane gas D.
Step 20, discharging the crude methane gas D from the top of the primary methanation region 1, allowing the crude methane gas D to enter a secondary methanation region 2, uniformly allowing hydrogen gas E to enter the secondary methanation region 2 from one side of the bottom of the secondary methanation region 2, and pre-modulating the hydrogen-carbon ratio of the crude methane gas D; in the secondary methanation region 2, the catalytic methanation catalyst F is used for carrying out catalytic methanation reaction on the methane gas D, and the fine particle catalytic methanation catalyst F is in rapid fluidized motion under the fluidization action of the hydrogen E and the crude methane gas D to carry out catalytic methanation reaction to obtain high-quality methane gas G. The fast fluidized motion means that the particles in the reactor are in a fast moving state under the action of the fluidizing medium, and the specific speed of the particles is related to the particle size, the weight, the wind speed and the like, so the fast fluidized motion can be regarded as a flowing phenomenon of the particles in the reactor.
In the method, the direct methanation reaction occurs in the primary methanation region 1, and the fluidization state of the particles is bubbling fluidization. Catalytic methanation reaction occurs in the secondary methanation region 2, and the fluidization state of particles is fast fluidization.
In the method, in a first-stage methanation region 1 of a two-stage methanation system, water vapor A is used as a fluidizing medium and a methyl alkylating agent, solid waste B is used as a fuel, and modified calcium-based ore serves as a direct methanation catalyst C; when the reaction starts, water vapor A enters from the bottom of the region, solid waste B is added from the side of the region, and under the fluidization action of the water vapor A, the solid waste B and the direct methanation catalyst C perform bubbling fluidization motion and perform direct methanation reaction with the water vapor A to obtain crude methane gas D. In the process, the catalyst C simultaneously plays the role of a sulfur-fixing adsorbent, and the cleaning of the crude methane gas is realized. In the secondary methanation region 2, hydrogen E enters from one side of the bottom of the secondary methanation region 2, so that the hydrogen-carbon ratio (H/C) of crude methane D obtained in the primary methanation region 1 is pre-modulated; the methanation catalyst F takes precious metal as an active component, takes rapid fluidization motion under the fluidization action of the hydrogen E and the methane D, generates catalytic methanation reaction, and deeply improves the quality of the methane D to obtain high-quality methane G. The method is coupled with two-stage methanation reaction, and reduction and resource utilization of the solid waste are realized.
The main ideas of the invention are as follows: the primary methanation region in the two-stage methanation reactor adopts a modified calcium-based ore catalyst to realize the direct methanation reaction of solid waste to obtain crude methane gas, and the high-efficiency adsorption and capture of the catalyst on impurity gas are mainly ensured. The secondary methanation region utilizes a noble metal catalyst to realize deep catalytic methanation reaction of the crude methane gas, thereby obviously improving the yield and quality of methane.
In the primary methanation region 1, the solid waste B can enter the primary methanation region 1 again after being effectively separated by the particle separator 3. The modified calcium-based ore catalyst C may be separated from the lower end of the particle separator 3 and then introduced into the calcination regeneration reactor 4. The catalytic methanation catalyst F can be efficiently separated by the cyclone.
In the above method, preferably, the modified calcium-based ore catalyst C is: the calcium-based ore is used as a carrier, and any one or more metal components in K, Fe are loaded. The purpose of the modification of the modified calcium-based ore catalyst C is to improve the catalytic capability of the catalyst. The modified calcium-based ore catalyst C has moderate reaction catalytic activity, and simultaneously has strong adsorption performance on impurity gas generated in the reaction process, so that the cleaning of crude methane gas is realized, the clean reaction atmosphere of the secondary methanation region 2 is ensured, and the deactivation risk of the noble metal catalyst used in the secondary methanation region 2 is reduced.
In the above method, preferably, the catalytic methanation catalyst F is one or more of a nickel-based catalyst, an iron-based catalyst and a molybdenum-based catalyst with high methane conversion rate. The catalytic methanation catalyst F has good catalytic activity, realizes deep catalytic methanation of the crude methane gas, and obviously improves the methane conversion efficiency and the gas production quality.
In the method, preferably, the two-stage methanation reactor is an integrated device and is divided into a first-stage methanation region 1 and a second-stage methanation region 2, and the first-stage methanation region 1 is located below the second-stage methanation region 2.
In the above method, preferably, the diameter of the primary methanation region 1 is larger than the diameter of the secondary methanation region 2, and the primary methanation region 1 is connected with the secondary methanation region 2 through a reducer. Preferably, a distribution plate is arranged in the reducing pipe to separate the first-stage methanation region 1 and the second-stage methanation region 2. The distribution plate can block part of fine particles from the primary methanation region, so that fuel particles and catalyst particles are prevented from flowing upwards due to inertia, and the influence on the secondary methanation region is reduced.
The method of the present invention is specifically described below by way of an example.
The catalyst in the first-stage methanation region is taken as an example of modified dolomite, and the catalyst in the second-stage methanation region is Al loaded with Ni-Fe2O3Type catalysts are exemplified. Wherein, in the modified dolomite, the mass content of Ni is 5 percent, and the mass content of Fe is 15 percent.
A method for preparing methane gas by solid waste in two-stage mode comprises the following steps:
the air distribution plate arranged at the bottom of the primary methanation region in the two-stage methanation reactor in the step 1) is a water vapor A inlet, and one side of the bottom of the bed body is a solid waste B inlet. The water vapor heated by the electric heater is taken as a fluidizing medium and a methyl alkylating agent, enters from a water vapor A inlet at the bottom of the primary methanation region 1, carries the solid waste B, the solid waste which is obtained from the separator and is not completely reacted and directly methanates the coarse particle modified dolomite mixture to move upwards. In the process, the direct methanation reaction is carried out among the steam A, the solid waste B and the modified dolomite to generate crude methane gas, and the main components are CO and CO2、H2And CH4. During this process, the CaO component of the catalyst absorbs CO2To CaCO3And simultaneously, by-products such as sulfide, tar and the like generated in the reaction process are adsorbed and fixed, and cleaner crude methane gas is obtained.
Step 2) discharging the crude methane gas D from the top of the primary methanation region 1, then entering the secondary methanation region 2, and loading Ni-Fe Al2O3The catalyst is used for catalyzing methanation reaction. And hydrogen E uniformly enters from one side of the bottom of the secondary methanation region, and the H/C ratio of the crude methane gas is adjusted to promote the catalytic methanation reaction. The gas after the reaction is high-quality methane gas.
And 3) feeding the solid particles (deactivated catalyst particles and ash containing solid wastes) subjected to direct methanation reaction into a particle separator, calcining the separated solid particles to generate decomposition reaction, and then feeding the solid particles into the primary methanation region 1 to participate in the reaction, wherein the ash containing the solid wastes and a small amount of deactivated catalyst particles are returned into the primary methanation region 1 through the particle separator.
And 4) after the deactivated catalytic methanation catalyst F in the step 4) is reduced and regenerated, the catalyst F enters the secondary methanation region 2 to continuously participate in the reaction.
Claims (7)
1. A method for preparing methane gas by solid waste in a two-stage mode is characterized by comprising the following steps:
step 10) in a primary methanation region (1) in a two-stage methanation reactor, introducing water vapor (A) serving as a fluidizing medium and a methyl alkylating agent from the bottom of the primary methanation region (1), introducing solid waste (B) serving as fuel and a modified calcium-based ore catalyst (C) serving as a direct methanation catalyst from the side edge of the primary methanation region (1), mixing the solid waste (B) and the modified calcium-based ore catalyst (C) upwards under the action of the water vapor (A) to form fluidization motion, and carrying out direct methanation reaction with the water vapor (A) to obtain crude methane gas (D);
step 20), discharging the crude methane gas (D) from the top of the primary methanation region (1), allowing the crude methane gas (D) to enter the secondary methanation region (2), uniformly allowing hydrogen (E) to enter the secondary methanation region (2) from one side of the bottom of the secondary methanation region (2), and pre-modulating the hydrogen-carbon ratio of the crude methane gas (D); in the secondary methanation region (2), the catalytic methanation catalyst (F) is used for carrying out catalytic methanation reaction on the methane gas (D), the catalytic methanation catalyst (F) is in rapid fluidization motion under the fluidization action of the hydrogen gas (E) and the crude methane gas (D), and the catalytic methanation reaction is carried out to obtain the high-quality methane gas (G).
2. The method for two-stage preparation of methane gas from solid waste according to claim 1, wherein the modified calcium-based ore catalyst (C) is: the calcium-based ore is used as a carrier, and any one or more metal components in K, Fe are loaded.
3. The method for two-stage preparation of methane gas from solid waste according to claim 1, wherein the catalytic methanation catalyst (F) is one or more of nickel-based, iron-based, molybdenum-based catalysts with high methane conversion rate.
4. The two-stage method for preparing methane gas from solid waste according to claim 1, wherein the particle size of the modified calcium-based ore catalyst (C) is larger than that of the solid waste (B), and the particle size of the solid waste (B) is larger than that of the catalytic methanation catalyst (F).
5. The two-stage type method for preparing methane gas from solid wastes according to claim 1, wherein the two-stage type methanation reactor is an integrated device and is divided into a primary methanation region (1) and a secondary methanation region (2), and the primary methanation region (1) is located below the secondary methanation region (2).
6. The two-stage method for preparing methane gas from solid waste according to claim 1, wherein the diameter of the primary methanation region (1) is larger than that of the secondary methanation region (2), and the primary methanation region (1) is connected with the secondary methanation region (2) through a reducer.
7. The two-stage method for preparing methane gas from solid waste according to claim 6, wherein a distribution plate is disposed in the reducer to separate the primary methanation region (1) and the secondary methanation region (2).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202110666308.XA CN113477190B (en) | 2021-06-16 | 2021-06-16 | Method for preparing methane gas from solid waste in two-stage mode |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202110666308.XA CN113477190B (en) | 2021-06-16 | 2021-06-16 | Method for preparing methane gas from solid waste in two-stage mode |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN113477190A true CN113477190A (en) | 2021-10-08 |
| CN113477190B CN113477190B (en) | 2023-03-17 |
Family
ID=77935142
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202110666308.XA Active CN113477190B (en) | 2021-06-16 | 2021-06-16 | Method for preparing methane gas from solid waste in two-stage mode |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN113477190B (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US11339970B1 (en) | 2020-12-07 | 2022-05-24 | Rolls-Royce Plc | Combustor with improved aerodynamics |
| US11353215B1 (en) | 2020-12-07 | 2022-06-07 | Rolls-Royce Plc | Lean burn combustor |
Citations (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101041136A (en) * | 2007-03-20 | 2007-09-26 | 华东理工大学 | Modification dolomite and the preparing method and the application |
| CN104399472A (en) * | 2014-11-26 | 2015-03-11 | 新奥科技发展有限公司 | Calcium-based compound catalyst and loading method thereof |
| CN104673414A (en) * | 2015-02-01 | 2015-06-03 | 太原理工大学 | Device and method for carrying out catalysis, gasification and methanation enrichment on coal |
| CN105222129A (en) * | 2015-11-05 | 2016-01-06 | 东南大学 | A kind of coal-fired burning chemistry chains separation of C O of the pure oxygen gasification that is coupled 2method |
| CN105312056A (en) * | 2014-06-26 | 2016-02-10 | Sk新技术株式会社 | Catalysts based on natural minerals and process for gasification using the same |
| CN107715887A (en) * | 2017-10-24 | 2018-02-23 | 江门绿润环保科技有限公司 | A kind of preparation method and applications of the nickel-base catalyst of modification dolomite load |
| US10435637B1 (en) * | 2018-12-18 | 2019-10-08 | Greatpoint Energy, Inc. | Hydromethanation of a carbonaceous feedstock with improved carbon utilization and power generation |
| CN110951508A (en) * | 2019-12-16 | 2020-04-03 | 中国科学院山西煤炭化学研究所 | Device and process for preparing methane by coal chemical-looping catalytic gasification based on calcium oxide |
| CN111978991A (en) * | 2020-07-07 | 2020-11-24 | 重庆恒瀚能途环保科技有限公司 | High-efficient innoxious rubbish schizolysis processing apparatus |
-
2021
- 2021-06-16 CN CN202110666308.XA patent/CN113477190B/en active Active
Patent Citations (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101041136A (en) * | 2007-03-20 | 2007-09-26 | 华东理工大学 | Modification dolomite and the preparing method and the application |
| CN105312056A (en) * | 2014-06-26 | 2016-02-10 | Sk新技术株式会社 | Catalysts based on natural minerals and process for gasification using the same |
| CN104399472A (en) * | 2014-11-26 | 2015-03-11 | 新奥科技发展有限公司 | Calcium-based compound catalyst and loading method thereof |
| CN104673414A (en) * | 2015-02-01 | 2015-06-03 | 太原理工大学 | Device and method for carrying out catalysis, gasification and methanation enrichment on coal |
| CN105222129A (en) * | 2015-11-05 | 2016-01-06 | 东南大学 | A kind of coal-fired burning chemistry chains separation of C O of the pure oxygen gasification that is coupled 2method |
| CN107715887A (en) * | 2017-10-24 | 2018-02-23 | 江门绿润环保科技有限公司 | A kind of preparation method and applications of the nickel-base catalyst of modification dolomite load |
| US10435637B1 (en) * | 2018-12-18 | 2019-10-08 | Greatpoint Energy, Inc. | Hydromethanation of a carbonaceous feedstock with improved carbon utilization and power generation |
| CN110951508A (en) * | 2019-12-16 | 2020-04-03 | 中国科学院山西煤炭化学研究所 | Device and process for preparing methane by coal chemical-looping catalytic gasification based on calcium oxide |
| CN111978991A (en) * | 2020-07-07 | 2020-11-24 | 重庆恒瀚能途环保科技有限公司 | High-efficient innoxious rubbish schizolysis processing apparatus |
Non-Patent Citations (1)
| Title |
|---|
| 赵丽霞著: "《生物质甘油共气化制氢基础研究》", 31 October 2019 * |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US11339970B1 (en) | 2020-12-07 | 2022-05-24 | Rolls-Royce Plc | Combustor with improved aerodynamics |
| US11353215B1 (en) | 2020-12-07 | 2022-06-07 | Rolls-Royce Plc | Lean burn combustor |
| US11402099B2 (en) * | 2020-12-07 | 2022-08-02 | Rolls-Royce Plc | Combustor with improved aerodynamics |
| US11603993B2 (en) | 2020-12-07 | 2023-03-14 | Rolls-Royce Plc | Combustor with improved aerodynamics |
Also Published As
| Publication number | Publication date |
|---|---|
| CN113477190B (en) | 2023-03-17 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| Valizadeh et al. | Valorization of biomass through gasification for green hydrogen generation: A comprehensive review | |
| Zeng et al. | Continuous hydrogen production from non-aqueous phase bio-oil via chemical looping redox cycles | |
| CN113477190B (en) | Method for preparing methane gas from solid waste in two-stage mode | |
| JP4259777B2 (en) | Biomass gasification method | |
| CA2900192C (en) | Methods for fuel conversion into syngas with composite metal oxides | |
| CN101774542B (en) | Biomass gasification hydrogen-producing system and method | |
| CN108424791B (en) | Process and apparatus for synthesis gas preparation | |
| CN102465047A (en) | Method for preparing methane by catalyzing and gasifying coal | |
| CN111363570B (en) | Method for preparing methane-rich gas by using waste | |
| CN102021037A (en) | Method and apparatus for preparing methane by catalytic gasification of coal | |
| CN106629600B (en) | Crude synthesis gas adsoption catalysis process for making hydrogen and its equipment | |
| CN1608972A (en) | Biomass-gasifying hydrogen generating serial fluid bed apparatus and method | |
| CN108504394B (en) | Catalytic pyrolysis-gasification integrated reaction device and method | |
| CN111777035A (en) | Self-heating type brown coal chemical chain gasification method based on copper-iron-based composite oxygen carrier | |
| Hu et al. | Application of calcium oxide/ferric oxide composite oxygen carrier for corn straw chemical looping gasification | |
| CN111378512A (en) | Method and system for preparing synthesis gas by biomass pyrolysis and gasification | |
| CN1482056A (en) | Process of catalyzing and gasifying fresh substance by solid thermophore for preparing hydrogen-rich gas | |
| CN114574250B (en) | Method and device for preparing clean synthetic gas by biomass chemical chain gasification | |
| CN104910969A (en) | Novel brown coal gasification system and method | |
| CN114275736A (en) | Chemical-looping CO (carbon monoxide) method taking red mud as oxygen carrier2Graded regeneration process and system | |
| CN101891147B (en) | Solid fuel fluidized bed near-zero emission hydrogen generating device | |
| CN201770472U (en) | Solid fuel fluidized bed near-zero emission hydrogen production device | |
| SHI et al. | Preparation and characterization of Ni/TPC catalyst and applied in straw pyrolysis gas reforming | |
| Luo et al. | Conversion and syngas production of toluene as a biomass tar model compound in chemical looping reforming | |
| CN108219816A (en) | A kind of low-order coal and the method for methyl hydride catalyzed common refining production lighting tar |
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 |