CN220397850U - Heat supply structure of heat conduction oil furnace for producing hydrogen by converting methanol with temperature independently regulated - Google Patents
Heat supply structure of heat conduction oil furnace for producing hydrogen by converting methanol with temperature independently regulated Download PDFInfo
- Publication number
- CN220397850U CN220397850U CN202320659243.0U CN202320659243U CN220397850U CN 220397850 U CN220397850 U CN 220397850U CN 202320659243 U CN202320659243 U CN 202320659243U CN 220397850 U CN220397850 U CN 220397850U
- Authority
- CN
- China
- Prior art keywords
- temperature
- conduction oil
- heat conduction
- heat
- supply structure
- 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
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 title claims abstract description 63
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 title claims abstract description 23
- 239000001257 hydrogen Substances 0.000 title claims abstract description 23
- 229910052739 hydrogen Inorganic materials 0.000 title claims abstract description 23
- 230000001105 regulatory effect Effects 0.000 title claims abstract description 9
- 238000006243 chemical reaction Methods 0.000 claims abstract description 51
- 238000009834 vaporization Methods 0.000 claims abstract description 29
- 230000008016 vaporization Effects 0.000 claims abstract description 29
- 230000003197 catalytic effect Effects 0.000 claims abstract description 10
- 230000003044 adaptive effect Effects 0.000 claims abstract 2
- 239000002994 raw material Substances 0.000 claims description 27
- 238000004519 manufacturing process Methods 0.000 claims description 12
- 239000003054 catalyst Substances 0.000 claims description 4
- 238000010438 heat treatment Methods 0.000 claims description 4
- 239000007795 chemical reaction product Substances 0.000 claims description 3
- 239000007789 gas Substances 0.000 claims description 3
- 238000002309 gasification Methods 0.000 claims description 3
- 238000004064 recycling Methods 0.000 claims description 2
- 239000002699 waste material Substances 0.000 description 3
- 230000006978 adaptation Effects 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
Landscapes
- Hydrogen, Water And Hydrids (AREA)
Abstract
The utility model relates to a heat supply structure of a heat conduction oil furnace for producing hydrogen by converting methanol with temperature being independently regulated, which comprises a vaporization superheater and a reactor which are correspondingly arranged, wherein the vaporization superheater and the reactor are used as execution parts of vaporization, catalytic conversion and conversion reaction of external high-temperature heat conduction oil, after part of external high-temperature heat conduction oil passes through the execution parts, low-temperature heat conduction oil after heat supply is formed, and other high-temperature heat conduction oil which does not pass through the execution parts is mixed to form adaptive heat conduction oil suitable for heat supply temperature, and the heat supply structure for producing hydrogen by converting methanol with temperature being independently regulated is formed by combination.
Description
Technical Field
The utility model relates to the technical field of hydrogen production technology and hydrogen production equipment, in particular to a heat-conducting oil furnace heat supply structure for hydrogen production by methanol conversion with independent temperature regulation.
Background
The methanol conversion hydrogen production is an endothermic reaction, and needs to be heated from the outside to reach the vaporization temperature of materials and the reaction temperature of the catalyst, the initial temperature is generally controlled at 250-260 ℃, the final temperature is controlled at 270-280 ℃, the oil temperature is required to be relatively stable in a certain stage, and the oil temperature is independently adjustable, and usually, heat conduction oil is selected as a heat transfer medium and is heated by a special heat conduction oil furnace.
When heat conduction oil is needed to be used as a heat transfer medium in other working occasions, the temperature range of the heat conduction oil is different from that of the heat conduction oil used in the previous working occasion, so that a heat conduction oil furnace is needed to be additionally and correspondingly arranged, and the problems of production resource waste and production field occupation are caused.
Therefore, it is necessary to provide a heat-conducting oil furnace heat supply structure for producing hydrogen by converting methanol with independent temperature regulation to solve the above problems.
Disclosure of Invention
The utility model aims to provide a heat supply structure of a heat conduction oil furnace for producing hydrogen by converting methanol with independent temperature regulation.
The technical proposal is as follows:
the utility model provides a heat conduction oil stove heat supply structure of temperature independent regulation formula methyl alcohol conversion hydrogen manufacturing, including vaporization superheater and the reactor that corresponds the setting, vaporization superheater and reactor are used as the evaporation of extrinsic high temperature conduction oil, catalytic conversion and conversion reaction's executive part, and after the extrinsic high temperature conduction oil of part passed through executive part, form the low temperature conduction oil after the heat supply, mix the other high temperature conduction oil that do not pass through executive part, form the adaptation conduction oil that is fit for heat supply temperature, the combination forms temperature independent regulation formula methyl alcohol conversion hydrogen manufacturing heat supply structure.
Further, the vaporization superheater comprises a tube side A and a shell side A which are correspondingly arranged, the tube side A is used as a heat conducting oil channel, the shell side A contains reaction raw materials, and the reaction raw materials are heated and gasified by the heat conducting oil in the tube side A, so that a rapid reaction raw material gasification structure is formed.
Further, the reaction raw materials are heated and vaporized by heat conduction oil in a vaporization superheater and superheated to 240-250 ℃ and then enter a reactor.
Further, the reactor comprises a tube side B and a shell side B which are correspondingly arranged, wherein the shell side B is used as a lower channel of the heat conduction oil, and the tube side B accommodates a catalyst.
Further, the reaction raw materials entering the reactor are subjected to catalytic conversion and conversion reaction, and the reaction temperature is 240-250 ℃ to generate a high-temperature conversion gas reaction product.
Further, the heat required for vaporization, catalytic conversion and conversion reactions is provided by the high temperature heat transfer oil.
Further, part of external high-temperature heat conduction oil and low-temperature heat conduction oil after heat supply are mixed to the temperature of 250-260 ℃ required by the system.
Further, pressurizing to 0.4Mpa by a heat conducting oil circulating pump, feeding into a vaporization superheater, providing a heat source for vaporization of the reaction raw materials, and then feeding into a shell side of a reactor to provide heat for the reaction raw materials, thereby forming a continuous heat supply structure of the reaction raw materials.
Further, the low-temperature heat conduction oil with the temperature of 220-230 ℃ discharged from the reactor is recycled after one part of the low-temperature heat conduction oil is mixed with the high-temperature heat conduction oil, and the other part of the low-temperature heat conduction oil is conveyed to an external heat conduction oil furnace system for heating.
Further, the temperature of the heat conduction oil conveyed to the external heat conduction oil furnace system is automatically controlled to 240-250 ℃ mainly through the linkage of a heat conduction oil regulating valve and a temperature transmitter.
Further, the vaporization superheater is a U-tube heat exchanger.
Further, the reactor is a tube-in-tube heat exchanger.
Compared with the prior art, the heat conduction oil for external heat supply is not limited to a specific temperature, the heat conduction oil is mixed with hot oil by mixing with the reflowed cold oil, the supply quantity of the high-temperature heat conduction oil is controlled, the required heat conduction oil temperature is automatically regulated, the universality of heat conduction oil supply is improved, and the resource waste and the production site occupation caused by a plurality of heat conduction oil furnaces are reduced.
Drawings
Fig. 1 is a schematic structural view of the present utility model.
Detailed Description
Examples:
referring to fig. 1, the embodiment shows a heat-conducting oil furnace heat supply structure for producing hydrogen by converting methanol with independent temperature adjustment, which comprises a vaporization superheater 100 and a reactor 200 which are correspondingly arranged, wherein the vaporization superheater 100 and the reactor 200 are used as execution parts of vaporization, catalytic conversion and conversion reactions of external high-temperature heat-conducting oil 10, and after part of external high-temperature heat-conducting oil 10 passes through the execution parts, heat-conducting oil with low temperature after heat supply is formed, and other high-temperature heat-conducting oil which does not pass through the execution parts is mixed to form heat-conducting oil with suitable heat supply temperature, so that the heat-conducting oil heat supply structure for producing hydrogen by converting methanol with independent temperature adjustment is formed.
The vaporization superheater 100 includes a tube side a and a shell side a, which are correspondingly disposed, the tube side a is used as the heat transfer oil channel 300, the shell side a accommodates the reaction raw material 400, and the reaction raw material 400 is heated and gasified by the heat transfer oil in the tube side a, so as to form a rapid reaction raw material gasification structure.
The reaction raw material 400 is heated and vaporized by the heat transfer oil in the vaporization superheater 100 and superheated to 240-250 ℃ and then enters the reactor 200.
The reactor 200 includes a tube side B and a shell side B, which are disposed correspondingly, the shell side B serving as the conduction oil lower channel 500, the tube side B accommodating a catalyst.
The reaction raw materials 400 entering the reactor 200 are subjected to catalytic conversion and conversion reactions at a reaction temperature of 240-250 ℃ to generate a high-temperature conversion gas reaction product 600.
The heat required for vaporization, catalytic conversion and conversion reactions is provided by high temperature heat transfer oil.
Mixing part of external high-temperature heat conduction oil and low-temperature heat conduction oil after heat supply to the temperature of 250-260 ℃ required by the system.
Then the reaction raw material 400 is pressurized to 0.4Mpa by a heat conducting oil circulating pump 1 and then is sent into a vaporization superheater 100, and after a heat source is provided for vaporization of the reaction raw material 400, the reaction raw material 400 is provided with heat by entering a shell side of the reactor 200, so that a continuous heat supply structure of the reaction raw material is formed.
And (3) mixing one part of the low-temperature heat conduction oil with the temperature of 220-230 ℃ and the high-temperature heat conduction oil which is discharged from the reactor 200, and then continuously recycling the mixed oil, and conveying the other part of the mixed oil to an external heat conduction oil furnace system for heating.
The temperature of the conduction oil 500 conveyed to the outside-boundary conduction oil furnace system is automatically controlled to 240-250 ℃ mainly through the linkage of a conduction oil regulating valve and a temperature transmitter.
The vaporization superheater 100 is a U-tube heat exchanger.
Reactor 200 is a tube-in-tube heat exchanger.
Compared with the prior art, the heat conduction oil for external heat supply is not limited to a specific temperature, the heat conduction oil is mixed with hot oil by mixing with the reflowed cold oil, the supply quantity of the high-temperature heat conduction oil is controlled, the required heat conduction oil temperature is automatically regulated, the universality of heat conduction oil supply is improved, and the resource waste and the production site occupation caused by a plurality of heat conduction oil furnaces are reduced.
What has been described above is merely some embodiments of the present utility model. It will be apparent to those skilled in the art that various modifications and improvements can be made without departing from the spirit of the utility model.
Claims (8)
1. A heat conduction oil furnace heat supply structure of independent temperature regulation formula methyl alcohol conversion hydrogen manufacturing, its characterized in that: the device comprises a vaporization superheater and a reactor which are correspondingly arranged, wherein the vaporization superheater and the reactor are used as execution parts of vaporization, catalytic conversion and conversion reaction of external high-temperature heat conduction oil, after part of external high-temperature heat conduction oil passes through the execution parts, low-temperature heat conduction oil after heat supply is formed, and the rest high-temperature heat conduction oil which does not pass through the execution parts is mixed to form adaptive heat conduction oil suitable for heat supply temperature, so that a temperature independent regulation type methanol conversion hydrogen production heat supply structure is formed;
the vaporization superheater comprises a tube side A and a shell side A which are correspondingly arranged, wherein the tube side A is used as a heat conducting oil channel, the shell side A contains reaction raw materials, and the reaction raw materials are heated and gasified by the heat conducting oil in the tube side A to form a rapid reaction raw material gasification structure;
the reactor comprises a tube side B and a shell side B which are correspondingly arranged, wherein the shell side B is used as a lower channel of heat conduction oil, and the tube side B accommodates a catalyst.
2. The heat conduction oil furnace heat supply structure for producing hydrogen by converting methanol with independent temperature regulation as claimed in claim 1, wherein: the reaction raw materials are heated and vaporized by heat conduction oil in a vaporization superheater and are overheated to 240-250 ℃ and then enter a reactor.
3. The heat conduction oil furnace heat supply structure for producing hydrogen by independently adjusting temperature and converting methanol according to claim 2, wherein the heat conduction oil furnace heat supply structure is characterized in that: the reaction raw materials entering the reactor are subjected to catalytic conversion and conversion reaction, and the reaction temperature is 240-250 ℃ to generate a high-temperature conversion gas reaction product.
4. A heat transfer oil furnace heating structure for producing hydrogen by converting methanol with independent temperature regulation as claimed in claim 3, wherein: the heat required for vaporization, catalytic conversion and conversion reactions is provided by high temperature heat transfer oil.
5. The heat conduction oil furnace heat supply structure for producing hydrogen by independently adjusting temperature and converting methanol as claimed in claim 4, wherein: mixing part of external high-temperature heat conduction oil and low-temperature heat conduction oil after heat supply to the temperature of 250-260 ℃ required by the system.
6. The heat conduction oil furnace heat supply structure for producing hydrogen by independently adjusting temperature and converting methanol as claimed in claim 5, wherein: and then the reaction raw materials are pressurized to 0.4Mpa by a heat conducting oil circulating pump and then are sent into a vaporization superheater, after a heat source is provided for vaporization of the reaction raw materials, the reaction raw materials enter a shell side of a reactor to provide heat for the reaction raw materials, and a continuous heat supply structure of the reaction raw materials is formed.
7. The heat conduction oil furnace heat supply structure for producing hydrogen by independently adjusting temperature and converting methanol as claimed in claim 6, wherein: and (3) mixing one part of the 220-230 ℃ low-temperature heat conduction oil discharged from the reactor with the high-temperature heat conduction oil, then continuously recycling the mixed oil, and conveying the other part of the mixed oil to an external heat conduction oil furnace system for heating.
8. The heat conduction oil furnace heat supply structure for producing hydrogen by independently adjusting temperature and converting methanol as claimed in claim 7, wherein: the temperature of the heat conduction oil conveyed to the outside-boundary heat conduction oil furnace system is automatically controlled to 240-250 ℃ mainly through the linkage of a heat conduction oil regulating valve and a temperature transmitter.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202320659243.0U CN220397850U (en) | 2023-03-29 | 2023-03-29 | Heat supply structure of heat conduction oil furnace for producing hydrogen by converting methanol with temperature independently regulated |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202320659243.0U CN220397850U (en) | 2023-03-29 | 2023-03-29 | Heat supply structure of heat conduction oil furnace for producing hydrogen by converting methanol with temperature independently regulated |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN220397850U true CN220397850U (en) | 2024-01-26 |
Family
ID=89611597
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202320659243.0U Active CN220397850U (en) | 2023-03-29 | 2023-03-29 | Heat supply structure of heat conduction oil furnace for producing hydrogen by converting methanol with temperature independently regulated |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN220397850U (en) |
-
2023
- 2023-03-29 CN CN202320659243.0U patent/CN220397850U/en active Active
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101191084B (en) | Multi-coproduction energy method and system by using coal gasification heat with methane reforming manner | |
| US5048284A (en) | Method of operating gas turbines with reformed fuel | |
| CN101704513B (en) | Shunting-type isothermal sulfur-tolerant conversion process and equipment thereof | |
| US9011562B2 (en) | Method for operating a reformer furnace and reforming plant | |
| CN102660339A (en) | Gas-steam efficient cogeneration process and system based on biomass gasification and methanation | |
| CN110616077B (en) | Method and device for preparing high-yield coke by combined baking-carbonization | |
| CN220397850U (en) | Heat supply structure of heat conduction oil furnace for producing hydrogen by converting methanol with temperature independently regulated | |
| CN106966361A (en) | A kind of hydrogen manufacturing conversion furnace | |
| EP0351094B1 (en) | Gas turbines | |
| CN104355966A (en) | Optimized reaction technology producing ethylene-glycol by adding hydrogen in oxalate | |
| CN107032300B (en) | A kind of hydrogen production by methanol system that reactor feed temperature is stable | |
| CN202688235U (en) | Device for producing formaldehyde by methanol | |
| CN205690385U (en) | Coal-burning boiler preposition biomass ultrahigh speed self-balancing gasification mixed combustion device | |
| CN212962863U (en) | Energy-saving carbon black production system | |
| CN208716846U (en) | A kind of lighter hydrocarbons producing synthesis gas reforming unit converting the conversion of gas pre-heating heat-exchanging formula using one section of high temperature | |
| CN108264937B (en) | Double fluidized bed reaction system | |
| CN216337460U (en) | Waste pot type hydrogenation gasification furnace | |
| CN112624045A (en) | Self-heat-transfer CO conversion process | |
| CN217398454U (en) | Needle coke hydrogen production unit vaporization reaction device | |
| CN201439492U (en) | Shunting isothermal sulphur-resisting conversion device | |
| CN217677349U (en) | Heat balance thioether synthesis system | |
| CN115466631B (en) | Method and device for biomass baking coupling sludge hydro-thermal synergistic co-gasification | |
| CN102502656A (en) | Method for converting silicon tetrachloride into trichlorosilane | |
| CN217498680U (en) | System for utilize low-pressure steam low level heat energy to carry out methyl alcohol hydrogen manufacturing | |
| CN220485617U (en) | Energy-saving biomass pyrolysis, carbon activation and gas reforming system |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant |