CN110270277B - Gas material distributor and direct coal liquefaction hydrogenation reactor - Google Patents
Gas material distributor and direct coal liquefaction hydrogenation reactor Download PDFInfo
- Publication number
- CN110270277B CN110270277B CN201910617021.0A CN201910617021A CN110270277B CN 110270277 B CN110270277 B CN 110270277B CN 201910617021 A CN201910617021 A CN 201910617021A CN 110270277 B CN110270277 B CN 110270277B
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- shell
- buffer
- material distributor
- gas
- inner shell
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- 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
- B01J8/008—Details of the reactor or of the particulate material; Processes to increase or to retard the rate of reaction
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
- C10G1/06—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal by destructive hydrogenation
- C10G1/065—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal by destructive hydrogenation in the presence of a solvent
-
- 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
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00796—Details of the reactor or of the particulate material
- B01J2208/00893—Feeding means for the reactants
- B01J2208/00911—Sparger-type feeding elements
Abstract
The invention relates to the technical field of coal direct liquefaction processes, in particular to a gas material distributor and a coal direct liquefaction hydrogenation reactor comprising the same. The utility model provides a gaseous material distributor, has the open-ended casing including honeycomb duct and one side, and the discharge gate of honeycomb duct is located the casing, be provided with the buffer that has the clearance that the gas passes through in the casing, the opening passes through clearance and honeycomb duct discharge gate intercommunication. The buffer enables the materials to be fully dispersed, and the catalyst is arranged in the structure after the materials flow through the buffer, so the catalyst is blocked by the buffer; the buffer prevents a large amount of catalyst from being brought into a circulating pump and a pipeline of the reactor due to the blockage of the guide pipe by the catalyst; so that the material circulation is smooth and the work efficiency is improved.
Description
Technical Field
The invention relates to the technical field of direct coal liquefaction processes, in particular to a gas material distributor and a direct coal liquefaction hydrogenation reactor.
Background
In the direct coal liquefaction technology, the main task of solvent hydrogenation is to provide qualified hydrogen supply solvent meeting the requirements for a coal liquefaction unit, and carry out full-fraction pre-hydrogenation on liquefied oil produced by the coal liquefaction unit to carry out pre-processing treatment for producing naphtha and diesel oil.
The original inlet distributor of the solvent hydrogenation reactor of the device is three flow guide pipes with the check function, so that materials entering the reactor are uniformly distributed, and the phenomenon that a circulating pump of the reactor is blocked and a pipeline is blocked due to backflow of a bed layer catalyst caused by system pressure fluctuation is avoided. However, in the process of multiple operations of the test device, the catalyst bed layer is unevenly distributed, and the catalyst is easily blocked at the position of the one-way valve of the flow guide pipe and then enters a circulating pump and a front pipeline of the reactor, so that the internal circulation of the reactor is poor, the reaction effect is poor, and the device is shut down.
Disclosure of Invention
The invention aims to solve the problems of blockage of a circulating pump of a reactor, pipeline blockage and the like caused by backflow of a catalyst due to system pressure fluctuation in the prior art.
In order to achieve the above object, in one aspect, the present invention provides a gas material distributor, which includes a flow guide pipe and a housing having an opening on one side, wherein a discharge port of the flow guide pipe is located in the housing, a buffer having a gap for gas to pass through is provided in the housing, and the opening is communicated with the discharge port of the flow guide pipe through the gap.
Preferably, the buffer is a plurality of porcelain balls.
Preferably, a fixed cover is arranged at the opening of the shell, and a through hole is formed in the fixed cover; the size of the through hole is smaller than the diameter of the porcelain ball.
Preferably, the honeycomb duct sets up the inside of casing, the honeycomb duct includes the inner shell and around the inner shell arrange and with form radial spaced's outer shell between the inner shell, the one end of inner shell forms the feed inlet, the other end and the radial spaced intercommunication of inner shell, be formed with the discharge gate on the outer shell.
Preferably, a backstop device for preventing the materials from reversely flowing into the inner shell from the outer shell is arranged at the communication position of the inner shell and the outer shell.
Preferably, the non-return means is a one-way valve.
Preferably, still include the material buffer tank, the feed inlet of honeycomb duct is connected to the one end of material buffer tank.
In a second aspect, the invention provides a direct coal liquefaction hydrogenation reactor, which comprises the gas material distributor.
Preferably, the gas material distributor is of a cylindrical structure with a hollow interior.
Preferably, the part of the cylinder with the circular cross section at the lower side is a hollow material buffer tank, the part of the cylinder with the circular cross section at the upper side is a shell, and the feed inlet and the discharge outlet of the draft tube are both arranged at the bottom of the shell.
In the technical scheme, the buffer enables the materials to be fully dispersed, and the catalyst is arranged in the structure after the materials flow through the buffer, so that the catalyst is blocked by the buffer; the buffer prevents a large amount of catalyst from being brought into a circulating pump and a pipeline of the reactor due to the blockage of the guide pipe by the catalyst; so that the material circulation is smooth and the work efficiency is improved.
Drawings
FIG. 1 is a top view of a material distributor within a direct coal liquefaction hydrogenation reactor;
fig. 2 is an internal structural view of a material distributor within a direct coal liquefaction hydrogenation reactor.
Description of the reference numerals
1-material buffer tank, 2-honeycomb duct, 3-fixed cover, 4-porcelain ball, 5-shell, 6-discharge hole and 7-through hole.
Detailed Description
The following detailed description of embodiments of the invention refers to the accompanying drawings. It should be understood that the detailed description and specific examples, while indicating the present invention, are given by way of illustration and explanation only, not limitation.
The utility model provides a gaseous material distributor which characterized in that has open-ended casing 5 including honeycomb duct 2 and one side, and the discharge gate 6 of honeycomb duct 2 is located casing 5, be provided with the buffer that has the clearance that supplies gas to pass through in the casing 5, the opening passes through clearance and the discharge gate 6 intercommunication of honeycomb duct 2.
The buffer enables the materials to be fully dispersed, and the catalyst is arranged in the structure after the materials flow through the buffer, so the catalyst is blocked by the buffer; the buffer pair prevents a large amount of catalyst from being brought into a circulating pump and a pipeline of the reactor due to the blockage of the guide pipe by the catalyst; so that the material circulation is smooth and the work efficiency is improved.
Preferably, as shown in fig. 1, the buffer is a plurality of ceramic balls 4.
Compared with other buffers, the ceramic ball has uniform gaps, is easy to fill and take out, and has better process effect.
Preferably, as shown in fig. 2, a fixed cover 3 is arranged at the opening of the housing 5, and a through hole 7 is arranged on the fixed cover 3; the size of the through hole 7 is smaller than the diameter of the porcelain ball 4.
The fixed cover prevents the ceramic balls from being brought into the upper part of the reactor due to material flow or system fluctuation and entering other reaction structures.
Preferably, the draft tube 2 is arranged inside the housing 5, the draft tube 2 includes an inner housing and an outer housing arranged around the inner housing and forming a radial space with the inner housing, one end of the inner housing is formed as a feed inlet, the other end of the inner housing is communicated with the radial space, and a discharge outlet 6 is formed on the outer housing.
The double-layer structure of the flow guide pipe can relatively prolong the flowing process of the materials, so that the materials are uniformly distributed.
Preferably, a backstop device for preventing the materials from reversely flowing into the inner shell from the outer shell is arranged at the communication position of the inner shell and the outer shell.
When the system working pressure is normal, the non-return device on the upper part of the flow guide pipe passes through materials, when the system pressure fluctuates, the pressure of a back path system is higher than the pressure of a front path, the flow guide pipe is in non-return, and the catalyst is prevented from flowing backwards.
Preferably, the non-return means is a one-way valve.
The check valve is a non-return device with higher cost performance, has simple structure and can achieve better effect of preventing reverse flow.
Preferably, the gas material distributor further comprises a material buffer tank 1, and one end of the material buffer tank 1 is connected with the feed inlet of the flow guide pipe 2.
The material buffer tank provides a stopping place for the materials entering the reactor, so that the materials entering the reactor are further uniformly mixed; meanwhile, the buffer function is achieved under the condition of small fluctuation of incoming materials. The material buffer tank can prolong the retention time of the material and avoid impacting the inner structure of the material distributor.
The invention provides in another aspect a direct coal liquefaction hydrogenation reactor comprising any one of the gas feed distributors described above.
By using the gas material distributor, the hydrogenation reactor for direct coal liquefaction can improve the hydrogen supply performance of the solvent and reduce the viscosity of aromatic carbon and the solvent in the circulating hydrogen supply solvent; and meanwhile, the content of S, N, O in the coal liquefaction oil is reduced.
Preferably, the gas material distributor is of a cylindrical structure with a hollow interior.
The cylindrical structure can better adapt to the material circulation of the hydrogenation reactor for direct coal liquefaction.
Preferably, the part of the cylinder with the circular cross section at the lower side is a hollow material buffer tank 1, the part of the cylinder with the circular cross section at the upper side is a shell 5, and the feed inlet and the discharge outlet 6 of the draft tube 2 are both arranged at the bottom of the shell 5.
The cylindrical gas material distributor has the advantages that the structure of the distributor is simplified while corresponding functions are realized, the integrally arranged structure is firm, and complicated installation is omitted; meanwhile, the material buffer tank 1 and the shell 5 can be provided with a partition board to separate the space, the guide pipe 2 is arranged at the bottom of the shell 5, and the feed inlet of the inner shell is just communicated with the partition board of the part connected with the material buffer tank; and the discharge gate 6 of honeycomb duct 2 also sets up in the bottom of casing 5, and the material mixes through filling the porcelain ball around honeycomb duct 2, and then overflows at the through-hole 7 at casing 5 top. The device skillfully saves space and simultaneously realizes the corresponding function of the gas material distributor.
The preferred embodiments of the present invention have been described in detail above with reference to the accompanying drawings, but the present invention is not limited thereto. Within the scope of the technical idea of the invention, many simple modifications can be made to the technical solution of the invention. Including each of the specific features, are combined in any suitable manner. The invention is not described in detail in order to avoid unnecessary repetition. Such simple modifications and combinations should be considered within the scope of the present disclosure as well.
Claims (8)
1. A gas material distributor is characterized by comprising a flow guide pipe (2) and a shell (5) with an opening on one side, wherein a discharge hole (6) of the flow guide pipe (2) is positioned in the shell (5), a buffer with a gap for gas to pass through is arranged in the shell (5), and the opening is communicated with the discharge hole (6) of the flow guide pipe (2) through the gap;
the draft tube (2) is arranged inside the shell (5), the draft tube (2) comprises an inner shell and an outer shell which is arranged around the inner shell and forms a radial interval with the inner shell, one end of the inner shell is formed as a feed inlet, the other end of the inner shell is communicated with the radial interval, and a discharge outlet (6) is formed on the outer shell;
and a backstop device for preventing the materials from reversely flowing into the inner shell from the outer shell is arranged at the communicated position of the inner shell and the outer shell.
2. The gas material distributor according to claim 1, wherein the buffer is a plurality of ceramic balls (4).
3. The gas material distributor according to claim 2, wherein a fixed cover (3) is arranged at the opening of the shell (5), and a through hole (7) is arranged on the fixed cover (3); the size of the through hole (7) is smaller than the diameter of the porcelain ball (4).
4. The gaseous material distributor of claim 1, wherein said non-return means is a one-way valve.
5. The gas material distributor according to claim 1, further comprising a material buffer tank (1), wherein one end of the material buffer tank (1) is connected with the feed inlet of the draft tube (2).
6. A coal direct liquefaction hydrogenation reactor characterized by comprising a gas mass distributor according to claims 1-5.
7. The direct coal liquefaction hydrogenation reactor of claim 6, wherein the gas material distributor is of a cylindrical structure with a hollow interior.
8. The coal direct liquefaction hydrogenation reactor according to claim 7, characterized in that the part of the cylinder with the circular cross section at the lower side is a hollow material buffer tank (1), the part with the circular cross section at the upper side is a shell (5), and the feed inlet and the discharge outlet (6) of the draft tube (2) are both arranged at the bottom of the shell (5).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201910617021.0A CN110270277B (en) | 2019-07-09 | 2019-07-09 | Gas material distributor and direct coal liquefaction hydrogenation reactor |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201910617021.0A CN110270277B (en) | 2019-07-09 | 2019-07-09 | Gas material distributor and direct coal liquefaction hydrogenation reactor |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN110270277A CN110270277A (en) | 2019-09-24 |
| CN110270277B true CN110270277B (en) | 2021-10-12 |
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| Application Number | Title | Priority Date | Filing Date |
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| CN201910617021.0A Active CN110270277B (en) | 2019-07-09 | 2019-07-09 | Gas material distributor and direct coal liquefaction hydrogenation reactor |
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Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101396647A (en) * | 2007-09-29 | 2009-04-01 | 中科合成油技术有限公司 | Gas-liquid-solid three-phase suspended bed reactor for f-t synthesis and use thereof |
| CN204251564U (en) * | 2014-11-27 | 2015-04-08 | 兰州寰球工程公司 | A kind of carbon four hydroaromatization reactor |
| CN204583143U (en) * | 2015-03-20 | 2015-08-26 | 河北中海石化股份有限公司 | A kind of up flow type hydrogenation reactor |
| CN106179132A (en) * | 2016-08-30 | 2016-12-07 | 凯瑞环保科技股份有限公司 | A kind of mixing carbon four selectivity for high concentration alkynes and alkadienes is hydrogenated with calandria type fixed bed reactor altogether |
| CN106902712A (en) * | 2017-03-30 | 2017-06-30 | 中国神华能源股份有限公司 | Reactor |
| CN107661735A (en) * | 2017-09-30 | 2018-02-06 | 北京中科诚毅科技发展有限公司 | A kind of hydrogenation reactor feed distributor and its feeding process, design method and purposes |
| CN208098031U (en) * | 2018-05-29 | 2018-11-16 | 成都升力科技有限责任公司 | A kind of hydrogen from methyl alcohol reactor |
| CN208406520U (en) * | 2018-05-25 | 2019-01-22 | 杭州天利空分设备制造有限公司 | A kind of air flow method diffusion structure |
Family Cites Families (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US9849434B2 (en) * | 2010-09-22 | 2017-12-26 | Grupo Petrotemex, S.A. De C.V. | Methods and apparatus for enhanced gas distribution |
| CN202666816U (en) * | 2012-07-30 | 2013-01-16 | 中国石油化工集团公司 | Gas distributor for triphase slurry bed reactor |
-
2019
- 2019-07-09 CN CN201910617021.0A patent/CN110270277B/en active Active
Patent Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101396647A (en) * | 2007-09-29 | 2009-04-01 | 中科合成油技术有限公司 | Gas-liquid-solid three-phase suspended bed reactor for f-t synthesis and use thereof |
| CN204251564U (en) * | 2014-11-27 | 2015-04-08 | 兰州寰球工程公司 | A kind of carbon four hydroaromatization reactor |
| CN204583143U (en) * | 2015-03-20 | 2015-08-26 | 河北中海石化股份有限公司 | A kind of up flow type hydrogenation reactor |
| CN106179132A (en) * | 2016-08-30 | 2016-12-07 | 凯瑞环保科技股份有限公司 | A kind of mixing carbon four selectivity for high concentration alkynes and alkadienes is hydrogenated with calandria type fixed bed reactor altogether |
| CN106902712A (en) * | 2017-03-30 | 2017-06-30 | 中国神华能源股份有限公司 | Reactor |
| CN107661735A (en) * | 2017-09-30 | 2018-02-06 | 北京中科诚毅科技发展有限公司 | A kind of hydrogenation reactor feed distributor and its feeding process, design method and purposes |
| CN208406520U (en) * | 2018-05-25 | 2019-01-22 | 杭州天利空分设备制造有限公司 | A kind of air flow method diffusion structure |
| CN208098031U (en) * | 2018-05-29 | 2018-11-16 | 成都升力科技有限责任公司 | A kind of hydrogen from methyl alcohol reactor |
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| Publication number | Publication date |
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| CN110270277A (en) | 2019-09-24 |
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