CN219051258U - Methylamine synthesis adiabatic reactor - Google Patents
Methylamine synthesis adiabatic reactor Download PDFInfo
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- CN219051258U CN219051258U CN202223202320.4U CN202223202320U CN219051258U CN 219051258 U CN219051258 U CN 219051258U CN 202223202320 U CN202223202320 U CN 202223202320U CN 219051258 U CN219051258 U CN 219051258U
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Abstract
The utility model provides a thermal insulation reactor for synthesizing methylamine, and relates to the technical field of methylamine synthesis. The methylamine synthesis adiabatic reactor comprises a tower body, a catalyst layer, a first heat exchanger and a second heat exchanger; the first outer outlet of the first heat exchanger is communicated with the first inner inlet of the second heat exchanger, the first inner outlet of the second heat exchanger is communicated with the upper inlet of the tower body, the lower outlet of the tower body is communicated with the inlet of the second outer tower body of the first heat exchanger, the second inner inlet of the second heat exchanger is communicated with the upper inlet of the tower body, and the second inner outlet of the second heat exchanger is communicated with the lower outlet. The reaction raw materials in the first heat exchanger are heated by recycling the heat of the reactant, and the reaction raw materials in the second heat exchanger are heated by the heat of the reactant in the reaction process, so that the reaction raw materials reach the required temperature, no extra energy source or cost is consumed, and the cost of synthesizing methylamine is reduced.
Description
Technical Field
The utility model relates to the technical field of methylamine synthesis, in particular to a methylamine synthesis adiabatic reactor.
Background
The methylamine synthesis is obtained by taking methanol and ammonia as raw materials, and reacting the raw materials at a certain temperature and under a certain pressure according to a certain proportion under the action of a catalyst.
In the related art, a reactor for synthesizing methylamine is generally an adiabatic reactor. The reaction temperature of methylamine synthesis is generally controlled between 360 ℃ and 420 ℃, and raw materials for methylamine synthesis need to adopt an external heat source at the inlet of a reactor to reach the reaction temperature.
However, the external heat source consumes a large amount of additional energy, and there is a problem in that the cost of methylamine synthesis increases.
Disclosure of Invention
The utility model provides a thermal insulation reactor for synthesizing methylamine, which aims to solve the problem that a great amount of extra energy is consumed by an external heat source, and the cost for synthesizing methylamine is increased.
The utility model provides a methylamine synthesis adiabatic reactor, which comprises a tower body, a catalyst layer, a first heat exchanger and a second heat exchanger;
the first heat exchanger is positioned outside the tower body, and is provided with a first outer inlet, a first outer outlet, a second outer inlet and a second outer outlet, wherein the first outer inlet is communicated with the first outer outlet, and the second outer inlet is communicated with the second outer outlet;
the second heat exchanger is positioned in the tower body, the catalyst layers are distributed on the upper side and the lower side of the second heat exchanger, the second heat exchanger is provided with a first inner inlet, a first inner outlet, a second inner inlet and a second inner outlet, the first inner inlet is communicated with the first inner outlet, and the second inner inlet is communicated with the second inner outlet;
the tower body is provided with an upper inlet and a lower outlet, the first outer outlet of the first heat exchanger is communicated with the first inner inlet of the second heat exchanger, the first inner outlet of the second heat exchanger is communicated with the upper inlet, the lower outlet is communicated with the second outer inlet of the first heat exchanger, the second inner inlet of the second heat exchanger is communicated with the upper inlet, and the second inner outlet of the second heat exchanger is communicated with the lower outlet.
Optionally, the second heat exchanger is located in the middle of the tower body, the tower body includes a first reaction portion and a second reaction portion, the first reaction portion is located above the second heat exchanger, and the second reaction portion is located below the second heat exchanger.
Optionally, the catalyst layer includes a first catalytic layer, a second catalytic layer, a third catalytic layer, and a fourth catalytic layer, the first catalytic layer and the second catalytic layer are located above the second heat exchanger, and the third catalytic layer and the fourth catalytic layer are located below the second heat exchanger.
Optionally, the first catalytic layer and the second catalytic layer are arranged at intervals, the second catalytic layer is abutted to the second heat exchanger, the third catalytic layer and the second heat exchanger are arranged at intervals, and the third catalytic layer and the fourth catalytic layer are arranged at intervals.
Optionally, a plurality of thermometers are arranged on the tower body, and the first catalytic layer, the second catalytic layer, the third catalytic layer and the fourth catalytic layer respectively correspond to at least two thermometers.
Optionally, the first catalytic layer, the second catalytic layer, the third catalytic layer and the fourth catalytic layer respectively correspond to three thermometers, and the three thermometers are arranged at equal intervals on the cross section of the tower body.
Optionally, a cold shock tube is disposed between the first catalytic layer and the second catalytic layer and between the third catalytic layer and the fourth catalytic layer.
Optionally, the second heat exchanger is provided with a plurality of the second inner inlets and a plurality of the second inner outlets, and each of the second inner inlets corresponds to one of the second inner outlets.
Optionally, the tower body comprises a first cross section and a second cross section with different heights, a plurality of second inner inlets are arranged on the first cross section at intervals, and a plurality of second inner outlets are arranged on the second cross section at intervals.
Optionally, the upper inlet is located at the top of the tower body, and the lower outlet is located at the bottom or side of the tower body.
The utility model provides an adiabatic reactor for synthesizing methylamine, which can heat the reaction raw materials in a first heat exchanger by recovering the heat of a reactant and heat the reaction raw materials in a second heat exchanger by the heat of the reactant in the reaction process, so that the reaction raw materials can reach the required temperature, and no extra energy and cost are consumed, thereby reducing the cost of synthesizing methylamine.
Drawings
In order to more clearly illustrate the embodiments of the present utility model or the technical solutions of the prior art, the drawings that are needed in the embodiments or the description of the prior art will be briefly described below, it will be obvious that the drawings in the following description are some embodiments of the present utility model, and that other drawings can be obtained according to these drawings without inventive effort to a person skilled in the art.
Fig. 1 is a schematic structural diagram of an adiabatic reactor for methylamine synthesis according to an embodiment of the utility model.
Reference numerals illustrate:
10-tower body;
101-upper inlet;
102-a lower outlet;
103-manhole;
104-a discharge hole;
105-first cross section;
106-a second cross section;
107-a safety valve;
11-a first reaction section;
12-a second reaction section;
201-a first catalytic layer;
202-a second catalytic layer;
203-a third catalytic layer;
204-a fourth catalytic layer;
30-a first heat exchanger;
301-a first outer inlet;
302-a first outer outlet;
303-a second external inlet;
304-a second outer outlet;
40-a second heat exchanger;
401-a first inner inlet;
402-a first inner outlet;
403-a second internal inlet;
404-a second inner outlet;
50-thermometer;
60-a cold shock tube.
Detailed Description
For the purpose of making the objects, technical solutions and advantages of the embodiments of the present utility model more apparent, the technical solutions of the embodiments of the present utility model will be clearly and completely described below with reference to the accompanying drawings in the embodiments of the present utility model, and it is apparent that the described embodiments are some embodiments of the present utility model, but not all embodiments of the present utility model. All other embodiments, which can be made by those skilled in the art based on the embodiments of the utility model without making any inventive effort, are intended to be within the scope of the utility model.
It should be noted that the terms "first," "second," and "second" are used for descriptive purposes only and are not to be construed as indicating or implying a relative importance or implying a number of technical features being indicated. Thus, a feature defining "a first" or "a second" may explicitly or implicitly include at least one such feature. In the description of the present utility model, the meaning of "plurality" means at least two, for example, two, three, etc., unless specifically defined otherwise.
In the present utility model, unless explicitly specified and limited otherwise, the terms "mounted," "connected," "secured," and the like are to be construed broadly and include, for example, either fixedly attached, detachably attached, or integrally formed; may be mechanically connected, may be electrically connected or may be in communication with each other; either directly or indirectly, through intermediaries, or both, may be in communication with each other or in interaction with each other, unless expressly defined otherwise. The specific meaning of the above terms in the present utility model can be understood by those of ordinary skill in the art according to the specific circumstances.
In the present utility model, unless expressly stated or limited otherwise, a first feature "up" or "down" a second feature may be the first and second features in direct contact, or the first and second features in indirect contact via an intervening medium. Moreover, a first feature being "above," "over" and "on" a second feature may be a first feature being directly above or obliquely above the second feature, or simply indicating that the first feature is level higher than the second feature. The first feature being "under", "below" and "beneath" the second feature may be the first feature being directly under or obliquely below the second feature, or simply indicating that the first feature is less level than the second feature.
In the above description, descriptions of the terms "one embodiment," "some embodiments," "examples," "specific examples," or "some examples," etc., mean that a particular feature, structure, material, or characteristic described in connection with the embodiment or example is included in at least one embodiment or example of the utility model. In this specification, schematic representations of the above terms are not necessarily directed to the same embodiment or example. Furthermore, the particular features, structures, materials, or characteristics described may be combined in any suitable manner in any one or more embodiments or examples. Furthermore, the different embodiments or examples described in this specification and the features of the different embodiments or examples may be combined and combined by those skilled in the art without contradiction.
In the related art, a reactor for synthesizing methylamine is generally an adiabatic reactor. The reaction temperature of methylamine synthesis is generally controlled between 360 ℃ and 420 ℃, and raw materials for methylamine synthesis need to adopt an external heat source at the inlet of a reactor to reach the reaction temperature. However, the external heat source consumes a large amount of additional energy, and there is a problem in that the cost of methylamine synthesis increases. In addition, methylamine synthesis is a severe exothermic reaction, and the severe increase of the synthesis temperature is caused by slight improper control in the reaction process, so that the reactor fly temperature, raw material methanol decomposition, catalyst carbon deposition and side reaction increase are caused, and great potential safety hazards are brought.
In order to solve the above problems, the present utility model provides an adiabatic reactor for synthesizing methylamine, which can heat the reaction raw materials in a first heat exchanger by recovering the heat of the reactant and heat the reaction raw materials in a second heat exchanger by the heat of the reactant during the reaction, so that the reaction raw materials reach the required temperature, and no additional energy and cost are consumed, thereby reducing the cost of methylamine synthesis. In addition, the reaction raw materials in the second heat exchanger are heated by the heat of the reactants in the reaction process, and part of the heat is taken away by the reaction raw materials in the second heat exchanger, so that the temperature in the reaction process can be reduced, the generation of the fly temperature of the reactor, the decomposition of raw materials methanol, the carbon deposition of the catalyst and the increase of side reactions can be effectively reduced, and the potential safety hazard can be further reduced.
The methylamine synthesis adiabatic reactor provided in the examples of the present utility model will be described in detail with reference to specific examples.
Fig. 1 is a schematic structural diagram of an adiabatic reactor for methylamine synthesis according to an embodiment of the utility model.
As shown in fig. 1, an embodiment of the present utility model provides a methylamine synthesis adiabatic reactor, which includes a tower body 10, a catalyst layer, a first heat exchanger 30, and a second heat exchanger 40; the first heat exchanger 30 is located outside the tower body 10, the second heat exchanger 40 is located inside the tower body 10, and the catalyst layers are distributed on the upper side and the lower side of the second heat exchanger 40.
Wherein the tower 10 has an upper inlet 101 and a lower outlet 102. The tower 10 extends in the gravity direction, the upper inlet 101 may be located at the top of the tower 10, and the lower outlet 102 may be located at the bottom or side of the tower 10. In some examples, the upper inlet 101 is located at the top of the tower 10 and the lower outlet 102 is located at the side of the tower 10.
The column 10 also has a reaction chamber into which reaction raw materials enter from an upper inlet 101, and reactants in the reaction chamber exit from a lower outlet 102. The reaction raw materials comprise methanol and ammonia gas when the methylamine synthesis adiabatic reactor just starts to work, and monomethylamine, dimethylamine and trimethylamine when the reaction raw materials work subsequently; the reactant comprises monomethylamine, dimethylamine, trimethylamine and unreacted raw materials which are obtained by the reaction of the reaction raw materials under the action of the catalyst layer.
The first heat exchanger 30 has a first outer inlet 301, a first outer outlet 302, a second outer inlet 303, and a second outer outlet 304, the first outer inlet 301 being in communication with the first outer outlet 302, the second outer inlet 303 being in communication with the second outer outlet 304.
The second heat exchanger 40 has a first inner inlet 401, a first inner outlet 402, a second inner inlet 403, and a second inner outlet 404, the first inner inlet 401 and the first inner outlet 402 being in communication, and the second inner inlet 403 and the second inner outlet 404 being in communication.
The first outer outlet 302 of the first heat exchanger 30 is in communication with the first inner inlet 401 of the second heat exchanger 40, the first inner outlet 402 of the second heat exchanger 40 is in communication with the upper inlet 101 of the column 10, the lower outlet 102 of the column 10 is in communication with the second outer inlet 303 of the first heat exchanger 30, the second inner inlet 403 of the second heat exchanger 40 is in communication with the upper inlet 101 of the column 10, and the second inner outlet 404 of the second heat exchanger 40 is in communication with the lower outlet 102 of the column 10.
The reaction raw materials enter the first heat exchanger 30 from the first external inlet 301 of the first heat exchanger 30, the reactants exiting the tower 10 enter the first heat exchanger 30 from the second external inlet 303 of the first heat exchanger 30, and the reactants in the first heat exchanger 30 exit from the second external outlet 304 of the first heat exchanger 30. It should be noted that the reactant exiting the second external outlet 304 of the first heat exchanger 30 enters the rectification system.
The methylamine synthesis adiabatic reactor specifically works: reactant materials enter the first heat exchanger 30 from a first outer inlet 301 of the first heat exchanger 30, reactant materials exiting the tower body 10 enter the first heat exchanger 30 from a second outer inlet 303 of the first heat exchanger 30, reactant materials exiting the tower body 10 serve as heat exchange heat sources of the first heat exchanger 30, and reactant materials in the first heat exchanger 30 heat the reactant materials in the first heat exchanger 30; the reaction raw materials in the first heat exchanger 30 exit from the first outer outlet 302 of the first heat exchanger 30 and enter the second heat exchanger 40 through the first inner inlet 401 of the second heat exchanger 40, methylamine in the tower 10 is synthesized into exothermic reaction, reactants positioned above the second heat exchanger 40 in the tower 10 enter the second heat exchanger 40 from the second inner inlet 403 of the second heat exchanger 40, the reactants positioned above the second heat exchanger 40 in the tower 10 serve as heat exchange heat sources of the second heat exchanger 40, and the reactants in the second heat exchanger 40 heat the reaction raw materials in the second heat exchanger 40; after the reaction raw materials are heated twice by the first heat exchanger 30 and the second heat exchanger 40, the reaction raw materials are discharged from a first inner outlet 402 of the second heat exchanger 40 and enter a reaction cavity of the tower body 10 through an upper inlet 101 of the tower body 10; after the reaction raw materials enter the reaction cavity of the tower body 10 through the upper inlet 101 of the tower body 10, the reaction raw materials pass through the catalyst layer from top to bottom to carry out synthesis reaction.
The reaction raw materials in the first heat exchanger 30 are heated by the heat of the reactants recovered from the tower body 10, and the reaction raw materials in the second heat exchanger 40 are heated by the heat of the reactants in the reaction process in the tower body 10, so that the reaction raw materials reach the required temperature, no additional energy source or cost is consumed, and the cost of synthesizing methylamine can be reduced. In addition, the heat of the reactant in the reaction process in the tower body 10 heats the reaction raw materials in the second heat exchanger 40, and part of the heat is taken away by the reaction raw materials in the second heat exchanger 40, so that the temperature in the reaction process can be reduced, the temperature of the reactor can be effectively reduced, the raw material methanol decomposition, the carbon deposition of the catalyst and the increase of side reactions are generated, the potential safety hazard can be further reduced, and the service life of the catalyst can be prolonged.
Optionally, the second heat exchanger 40 is located in the middle of the tower body 10, the tower body 10 includes a first reaction portion 11 and a second reaction portion 12, the first reaction portion 11 is located above the second heat exchanger 40, and the second reaction portion 12 is located below the second heat exchanger 40.
Wherein the catalyst layer is distributed in the first reaction part 11 and the second reaction part 12. The first reaction part 11 may be understood as a portion of the tower 10 above the second heat exchanger 40, and the second reaction part 12 may be understood as a portion below the second heat exchanger 40.
The catalyst layer may include a plurality of catalyst layers disposed at intervals and having equal thicknesses within the tower body 10.
In an alternative embodiment, the catalyst layer includes a first catalytic layer 201, a second catalytic layer 202, a third catalytic layer 203, and a fourth catalytic layer 204, where the first catalytic layer 201, the second catalytic layer 202, the third catalytic layer 203, and the fourth catalytic layer 204 are sequentially disposed from top to bottom in the tower body 10, the first catalytic layer 201 and the second catalytic layer 202 are located above the second heat exchanger 40, and the third catalytic layer 203 and the fourth catalytic layer 204 are located below the second heat exchanger 40.
The upper inlet 101 of the tower 10 is located above the first catalytic layer 201 and the lower outlet 102 of the tower 10 is located below the fourth catalytic layer 204.
The first catalytic layer 201, the second catalytic layer 202, the third catalytic layer 203 and the fourth catalytic layer 204 are provided with a manhole 103 and a discharge hole 104, and the manhole 103 and the discharge hole 104 are in a closed state during the operation of the methylamine synthesis adiabatic reactor. When the catalyst needs to be added, stopping the operation of the methylamine synthesis adiabatic reactor, and opening the manhole 103 to fill the catalyst; after the catalyst reaches the service cycle, the methylamine synthesis adiabatic reactor stops working, and the discharge hole 104 is opened to remove the catalyst from the tower 10.
Further, the first catalytic layer 201 is disposed at a distance from the second catalytic layer 202, the second catalytic layer 202 is abutted against the second heat exchanger 40, the third catalytic layer 203 is disposed at a distance from the second heat exchanger 40, and the third catalytic layer 203 is disposed at a distance from the fourth catalytic layer 204.
Wherein the reactant passing through the fourth catalytic layer 204 in the tower 10 exits the lower outlet 102 of the tower 10 and enters the first heat exchanger 30 from the second external inlet 303 of the first heat exchanger 30; reactants within the column 10 passing through the second catalytic layer 202 enter the second heat exchanger 40 from the second inner inlet 403 of the second heat exchanger 40.
When the column 10 has a circular cross section in the range where the catalyst layer is located, the catalyst may be packed in the circular cross section.
Optionally, as shown in fig. 1, a plurality of thermometers 50 are disposed on the tower body 10, and the first catalytic layer 201, the second catalytic layer 202, the third catalytic layer 203, and the fourth catalytic layer 204 respectively correspond to at least one thermometer 50. The temperature at which the first catalytic layer 201, the second catalytic layer 202, the third catalytic layer 203, and the fourth catalytic layer 204 perform the synthesis reaction can be detected by the thermometer 50.
Wherein the thicknesses of the first catalytic layer 201, the second catalytic layer 202, the third catalytic layer 203, and the fourth catalytic layer 204 in the up-down direction of the tower body 10 are equal.
The first catalytic layer 201 may correspond to one thermometer 50 or may correspond to a plurality of thermometers 50. When the first catalytic layer 201 corresponds to the plurality of thermometers 50, the plurality of thermometers 50 are arranged at equal intervals on the cross section of the tower body 10, and thus, the plurality of positions of the first catalytic layer 201 can be measured.
The second catalytic layer 202 may correspond to one thermometer 50 or may correspond to a plurality of thermometers 50. When the second catalytic layer 202 corresponds to the plurality of thermometers 50, the plurality of thermometers 50 are arranged at equal intervals on the cross section of the tower body 10, and thus, a plurality of positions of the second catalytic layer 202 can be measured.
The third catalytic layer 203 may correspond to one thermometer 50 or may correspond to a plurality of thermometers 50. When the third catalytic layer 203 corresponds to the plurality of thermometers 50, the plurality of thermometers 50 are arranged at equal intervals on the cross section of the tower body 10, and thus, a plurality of positions of the third catalytic layer 203 can be measured.
The fourth catalytic layer 204 may correspond to one thermometer 50 or may correspond to a plurality of thermometers 50. When the fourth catalytic layer 204 corresponds to the plurality of thermometers 50, the plurality of thermometers 50 are arranged at equal intervals on the cross section of the tower body 10, and thus, a plurality of positions of the fourth catalytic layer 204 can be measured.
In an alternative embodiment, the first catalytic layer 201, the second catalytic layer 202, the third catalytic layer 203 and the fourth catalytic layer 204 correspond to three thermometers 50 respectively, the three thermometers 50 corresponding to the first catalytic layer 201 are arranged at equal intervals on the cross section of the tower body 10, the three thermometers 50 corresponding to the second catalytic layer 202 are arranged at equal intervals on the cross section of the tower body 10, the three thermometers 50 corresponding to the third catalytic layer 203 are arranged at equal intervals on the cross section of the tower body 10, and the three thermometers 50 corresponding to the fourth catalytic layer 204 are arranged at equal intervals on the cross section of the tower body 10.
Further, a cooling pipe 60 is disposed between the first catalytic layer 201 and the second catalytic layer 202 and between the third catalytic layer 203 and the fourth catalytic layer 204, and the temperature of the reactant can be adjusted by the cooling pipe 60.
When the temperature detected by the thermometer 50 on the tower body 10 is not within the required range, the cold shock pipe 60 is opened to adjust the temperature in the tower body 10.
Optionally, the second heat exchanger 40 is provided with a plurality of second inner inlets 403 and a plurality of second inner outlets 404, one second inner outlet 404 for each second inner inlet 403. So configured, the reactants can be caused to rapidly enter and exit the second heat exchanger 40.
The tower 10 includes a first cross section 105 and a second cross section 106 with different heights within the range of the second heat exchanger 40, a plurality of second inner inlets 403 are disposed at intervals on the first cross section 105, and a plurality of second inner outlets 404 are disposed at intervals on the second cross section 106.
Optionally, as shown in fig. 1, a safety valve 107 is provided on the tower 10, and the safety valve 107 is located at the top of the tower 10.
Finally, it should be noted that: the above embodiments are only for illustrating the technical solution of the present utility model, and not for limiting the same; although the utility model has been described in detail with reference to the foregoing embodiments, it will be understood by those of ordinary skill in the art that: the technical scheme described in the foregoing embodiments can be modified or some or all of the technical features thereof can be replaced by equivalents; such modifications and substitutions do not depart from the spirit of the utility model.
Claims (10)
1. The methylamine synthesis adiabatic reactor is characterized by comprising a tower body, a catalyst layer, a first heat exchanger and a second heat exchanger;
the first heat exchanger is positioned outside the tower body, and is provided with a first outer inlet, a first outer outlet, a second outer inlet and a second outer outlet, wherein the first outer inlet is communicated with the first outer outlet, and the second outer inlet is communicated with the second outer outlet;
the second heat exchanger is positioned in the tower body, the catalyst layers are distributed on the upper side and the lower side of the second heat exchanger, the second heat exchanger is provided with a first inner inlet, a first inner outlet, a second inner inlet and a second inner outlet, the first inner inlet is communicated with the first inner outlet, and the second inner inlet is communicated with the second inner outlet;
the tower body is provided with an upper inlet and a lower outlet, the first outer outlet of the first heat exchanger is communicated with the first inner inlet of the second heat exchanger, the first inner outlet of the second heat exchanger is communicated with the upper inlet, the lower outlet is communicated with the second outer inlet of the first heat exchanger, the second inner inlet of the second heat exchanger is communicated with the upper inlet, and the second inner outlet of the second heat exchanger is communicated with the lower outlet.
2. The adiabatic methylamine synthesis reactor as claimed in claim 1, wherein the second heat exchanger is located in the middle of the column, the column comprises a first reaction part and a second reaction part, the first reaction part is located above the second heat exchanger, and the second reaction part is located below the second heat exchanger.
3. The methylamine synthesis adiabatic reactor of claim 2, wherein the catalyst layer comprises a first catalytic layer, a second catalytic layer, a third catalytic layer, and a fourth catalytic layer, the first catalytic layer and the second catalytic layer being located above the second heat exchanger, the third catalytic layer and the fourth catalytic layer being located below the second heat exchanger.
4. A methylamine synthesis adiabatic reactor as claimed in claim 3, characterised in that the first catalytic layer is spaced from the second catalytic layer, the second catalytic layer is in abutment with the second heat exchanger, the third catalytic layer is spaced from the second heat exchanger, and the third catalytic layer is spaced from the fourth catalytic layer.
5. The adiabatic reactor for methylamine synthesis as claimed in claim 4, wherein a plurality of thermometers are provided on the column body, and the first catalytic layer, the second catalytic layer, the third catalytic layer and the fourth catalytic layer correspond to at least two of the thermometers, respectively.
6. The adiabatic reactor for methylamine synthesis as claimed in claim 5, wherein the first catalytic layer, the second catalytic layer, the third catalytic layer and the fourth catalytic layer correspond to three thermometers respectively, and the three thermometers are disposed at equal intervals on the cross section of the tower body.
7. The adiabatic reactor for methylamine synthesis as claimed in claim 5, wherein a cold shock tube is provided between the first catalytic layer and the second catalytic layer and between the third catalytic layer and the fourth catalytic layer.
8. The adiabatic reactor for methylamine synthesis as claimed in any one of claims 1 to 7, wherein the second heat exchanger is provided with a plurality of the second inner inlets and a plurality of the second inner outlets, one for each of the second inner inlets.
9. The adiabatic methylamine synthesis reactor as claimed in claim 8, wherein the column comprises a first cross section and a second cross section of different heights, the plurality of second inner inlets being spaced apart on the first cross section and the plurality of second inner outlets being spaced apart on the second cross section.
10. The adiabatic reactor for methylamine synthesis as claimed in any one of claims 1 to 6, wherein the upper inlet is located at the top of the column and the lower outlet is located at the bottom or side of the column.
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| CN116395636A (en) * | 2023-03-23 | 2023-07-07 | 上海工程技术大学 | Spiral heating tube type dimethyl ether reforming hydrogen production reactor and application thereof |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN116395636A (en) * | 2023-03-23 | 2023-07-07 | 上海工程技术大学 | Spiral heating tube type dimethyl ether reforming hydrogen production reactor and application thereof |
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