CN220149491U - Catalytic pyrolysis reaction system - Google Patents
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- CN220149491U CN220149491U CN202322924940.7U CN202322924940U CN220149491U CN 220149491 U CN220149491 U CN 220149491U CN 202322924940 U CN202322924940 U CN 202322924940U CN 220149491 U CN220149491 U CN 220149491U
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- 238000006243 chemical reaction Methods 0.000 title claims abstract description 82
- 238000007233 catalytic pyrolysis Methods 0.000 title claims abstract description 28
- 238000000197 pyrolysis Methods 0.000 claims abstract description 56
- 239000003054 catalyst Substances 0.000 claims abstract description 26
- 238000010438 heat treatment Methods 0.000 claims abstract description 23
- 238000001833 catalytic reforming Methods 0.000 claims abstract description 21
- 239000000376 reactant Substances 0.000 claims abstract description 21
- 230000003197 catalytic effect Effects 0.000 claims abstract description 13
- 230000004048 modification Effects 0.000 claims abstract description 10
- 238000012986 modification Methods 0.000 claims abstract description 10
- 239000007789 gas Substances 0.000 claims description 56
- 238000009833 condensation Methods 0.000 claims description 21
- 230000005494 condensation Effects 0.000 claims description 21
- 230000009471 action Effects 0.000 claims description 11
- 239000002826 coolant Substances 0.000 claims description 6
- 238000001816 cooling Methods 0.000 claims description 6
- 125000003158 alcohol group Chemical group 0.000 claims description 2
- 239000003245 coal Substances 0.000 description 17
- 238000000034 method Methods 0.000 description 6
- 230000008569 process Effects 0.000 description 5
- 238000000926 separation method Methods 0.000 description 5
- XKRFYHLGVUSROY-UHFFFAOYSA-N Argon Chemical compound [Ar] XKRFYHLGVUSROY-UHFFFAOYSA-N 0.000 description 4
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 4
- 230000008901 benefit Effects 0.000 description 4
- 239000002817 coal dust Substances 0.000 description 3
- 239000000463 material Substances 0.000 description 3
- 238000012546 transfer Methods 0.000 description 3
- 239000004215 Carbon black (E152) Substances 0.000 description 2
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 2
- 229910052786 argon Inorganic materials 0.000 description 2
- 239000011280 coal tar Substances 0.000 description 2
- 238000002485 combustion reaction Methods 0.000 description 2
- 238000011161 development Methods 0.000 description 2
- 238000002309 gasification Methods 0.000 description 2
- 229930195733 hydrocarbon Natural products 0.000 description 2
- 239000001257 hydrogen Substances 0.000 description 2
- 229910052739 hydrogen Inorganic materials 0.000 description 2
- 125000004435 hydrogen atom Chemical class [H]* 0.000 description 2
- 238000009434 installation Methods 0.000 description 2
- 229910052757 nitrogen Inorganic materials 0.000 description 2
- 238000010248 power generation Methods 0.000 description 2
- 239000011269 tar Substances 0.000 description 2
- 239000002028 Biomass Substances 0.000 description 1
- 229910003310 Ni-Al Inorganic materials 0.000 description 1
- -1 Small molecule hydrocarbon Chemical class 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 238000003763 carbonization Methods 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 239000003034 coal gas Substances 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000000428 dust Substances 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005485 electric heating Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000001307 helium Substances 0.000 description 1
- 229910052734 helium Inorganic materials 0.000 description 1
- SWQJXJOGLNCZEY-UHFFFAOYSA-N helium atom Chemical compound [He] SWQJXJOGLNCZEY-UHFFFAOYSA-N 0.000 description 1
- 230000003993 interaction Effects 0.000 description 1
- 239000004058 oil shale Substances 0.000 description 1
- 239000004033 plastic Substances 0.000 description 1
- 229920003023 plastic Polymers 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 230000004083 survival effect Effects 0.000 description 1
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- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
Abstract
The utility model provides a catalytic pyrolysis reaction system. The device comprises a pyrolysis furnace, a catalytic reforming furnace and a condensing tank, wherein the pyrolysis furnace comprises a first heater, a first reaction tube and a crucible, the first reaction tube comprises a first high-temperature region, the first heater is used for heating the first reaction tube, the crucible is used for holding reactants to be pyrolyzed, and the crucible can move in the first reaction tube; the catalytic reforming furnace comprises a second heater and a second reaction tube, the catalytic reforming furnace is connected with the pyrolysis furnace through a first valve, the second heater is used for heating the second reaction tube, and a catalyst is loaded in the second reaction tube; the condensing tank comprises a condensing pipe, and is connected with the catalytic reforming furnace and the pyrolysis furnace through a second valve. According to the utility model, the arrangement of the pyrolysis furnace and the catalytic modification furnace is adjusted, and the movable crucible for containing the reactant to be pyrolyzed is arranged in the catalytic furnace, so that the rapid pyrolysis of the reactant to be pyrolyzed can be realized, and the problem of difficulty in separating the reactant from the catalyst is solved.
Description
Technical Field
The utility model relates to the field of catalytic pyrolysis, in particular to a catalytic pyrolysis reaction system.
Background
Energy is an important material basis for survival and development of human society, and is closely related to economic development. Worldwide, the energy demand of emerging countries is growing rapidly. At present, the energy structure of China belongs to fossil energy, and in the future, the energy supply of China will be diversified, but the fossil energy still occupies the main place, and the proportion of renewable energy is increased. Efficient, low-carbon and clean utilization of coal has become common knowledge.
The utilization modes of coal include combustion, gasification, liquefaction, pyrolysis and the like. Coal is mostly used for power generation and has low utilization rate, and is a main pollution source. Pyrolysis is not only a basic process of coal utilization, but also an important way for realizing classification, quality separation and efficient clean utilization of coal. Pyrolysis tar, coal gas and semicoke can be obtained through mild pyrolysis. Compared with combustion and gasification, the method has the advantages of less energy consumption, environmental protection and economy, can change a single coal power generation mode, increase oil gas and improve energy safety.
The structure of the reactor has important influence on coal pyrolysis, and mainly has different mass transfer, heat transfer and other aspects. From the aspect of heating, it can be largely classified into external heating type and internal heating type. Wherein the external heating is not uniform for heating the coal, and the semicoke quality is not uniform, mainly due to poor heat conductivity of the coal. The internal heating type has higher heat transfer efficiency. At present, the middle-low temperature pyrolysis in the northern Shaanxi region generally adopts an internal heating pyrolysis furnace process, is suitable for the characteristics of coal types, and has remarkable economic benefit; but also has the following drawbacks: the raw materials are only limited by lump coal, the generation scale is small, the gas is less, the heat value is low, and the like. The biggest constraint is that only lump coal can be used, which makes about 80% of the pulverized coal inefficient. In addition, the problem of oil-dust separation in pulverized coal pyrolysis is also a technical and engineering problem.
At present, most of laboratory researches are performed by electric heating equipment, and a thermogravimetric analyzer, a grid Jin Diwen carbonization tester, a fixed bed, a fluidized bed, a cracker and the like are common. In the above-mentioned apparatus, there are problems in that rapid pyrolysis/cooling of the sample cannot be performed, separation of the reactant from the catalyst is difficult, and the like.
Disclosure of Invention
Aiming at the problems that rapid pyrolysis/cooling cannot be performed, separation of reactants and catalysts is difficult and the like in the prior art, the utility model provides a catalytic pyrolysis reaction system, which comprises:
the pyrolysis furnace comprises a first heater, a first reaction tube and a crucible, wherein the first reaction tube comprises a first high-temperature zone, the first heater is used for heating the first reaction tube, the crucible is used for containing reactants to be pyrolyzed, and the crucible can move in the first reaction tube;
the catalytic reforming furnace comprises a second heater and a second reaction tube, and is connected with the pyrolysis furnace through a first valve, wherein the second heater is used for heating the second reaction tube, and the second reaction tube is loaded with a catalyst;
the condensing tank comprises a condensing pipe, is connected with the catalytic reforming furnace and is connected with the pyrolysis furnace through a second valve;
when the first heater heats the first high-temperature region to a preset pyrolysis temperature, the crucible can enter the first high-temperature region and leave the first high-temperature region within a preset time, and the reactant to be pyrolyzed generates volatile gas; when the first valve is opened, the second valve is closed, and the second heater is heated to a preset catalytic modification temperature, the volatile gas can enter the catalytic modification furnace and is catalytically modified under the action of the catalyst to generate modified products, and the modified products can enter the condensation tank and are condensed and collected under the action of the condensation pipe; when the first valve is closed and the second valve is opened, the volatile gas can enter the condensation tank and is condensed and collected under the action of the condensation pipe.
In some embodiments of the utility model, the pyrolysis furnace further comprises a moving rack, the crucible is mounted on the moving rack, and the moving rack can move in the first reaction tube, so that the crucible is driven to move in the first reaction tube.
In some embodiments of the utility model, the first reaction tube further comprises a first low temperature zone and a second low temperature zone, the first high temperature zone being located between the first low temperature zone and the second low temperature zone;
wherein the crucible is located in the first low temperature zone when the first high temperature zone is not heated to the predetermined pyrolysis temperature; after the reactant to be pyrolyzed is pyrolyzed for the predetermined time, the crucible exits the first high temperature zone and enters the second low temperature zone.
In some embodiments of the utility model, the second reaction tube comprises a second high temperature zone, the catalyst being loaded in the second high temperature zone;
wherein when the second high temperature region is heated to the predetermined catalytic reforming temperature, the volatile gas can be catalytically reformed in the second high temperature region under the action of the catalyst to generate the reformed product.
In some embodiments of the utility model, the second reaction tube further comprises a third low temperature zone and a fourth low temperature zone, the second high temperature zone being located between the third low temperature zone and the fourth low temperature zone;
the third low-temperature zone is used for preheating the volatile gas, and the fourth low-temperature zone is used for cooling the modified product.
In some embodiments of the utility model, the cooling medium of the condenser tube is alcohol.
In some embodiments of the utility model, the central axis of the second reaction tube is parallel to the direction of flow of the volatile gas.
In some embodiments of the utility model, the pyrolysis furnace further comprises a first temperature controller coupled to the first heater, the first temperature controller for controlling the heating temperature of the first reaction tube;
the catalytic reforming furnace further comprises a second temperature controller connected with the second heater, and the second temperature controller is used for controlling the heating temperature of the second reaction tube.
In some embodiments of the utility model, the catalytic pyrolysis reaction system further comprises a gas chromatograph connected to the condensation tank, wherein the gas chromatograph is configured to detect non-condensable gases in the upgraded product or the volatile gas that cannot be condensed and collected.
In some embodiments of the utility model, the catalytic pyrolysis reaction system further comprises a gas supply unit coupled to the pyrolysis furnace, the gas supply unit comprising a flow meter.
According to the utility model, the arrangement of the pyrolysis furnace and the catalytic modification furnace is adjusted, and the movable crucible for containing the reactant to be pyrolyzed is arranged in the catalytic furnace, so that the rapid pyrolysis of the reactant to be pyrolyzed can be realized, and the problem of difficulty in separating the reactant from the catalyst is solved. In addition, the catalytic pyrolysis reaction system provided by the utility model can achieve effective catalytic effect under the condition of a small amount of catalyst, so that the catalytic cost is reduced, and the catalytic pyrolysis reaction system is very suitable for industrial popularization and application.
Additional aspects and advantages of the utility model will be set forth in part in the description which follows, and in part will be obvious from the description, or may be learned by practice of the utility model.
Drawings
Fig. 1 shows a schematic structural diagram of a catalytic pyrolysis reaction system according to an embodiment of the utility model.
Reference numerals illustrate:
100. the device comprises a pyrolysis furnace, 200, a catalytic reforming furnace, 300, a condensing tank, 400, a gas supply unit, 500, a gas chromatograph, 101, a first heater, 102, a first reaction tube, 103, a crucible, 104, a movable frame, 105, a first temperature controller, 201, a second heater, 202, a second reaction tube, 203, a second temperature controller, 301, a condensing tube, 401, a flowmeter, 106, a first low temperature region, 107, a first high temperature region, 108, a second low temperature region, 204, a third low temperature region, 205, a second high temperature region, 206, a fourth low temperature region, 207, a catalyst, 601, a first valve, 602, a second valve, 402 and a third valve.
Detailed Description
Hereinafter, only certain exemplary embodiments are briefly described. As will be recognized by those of skill in the pertinent art, the described embodiments may be modified in various different ways without departing from the spirit or scope of the present utility model. Accordingly, the drawings and description are to be regarded as illustrative in nature and not as restrictive.
The following disclosure provides many different embodiments, or examples, for implementing different features of the utility model. In order to simplify the present disclosure, components and installations of specific examples are described below. They are, of course, merely examples and are not intended to limit the utility model. Furthermore, the present utility model may repeat reference numerals and/or letters in the various examples, which are for the purpose of brevity and clarity, and which do not in themselves indicate the relationship between the various embodiments and/or installations in question. In addition, the present utility model provides examples of various specific processes and materials, but one of ordinary skill in the art will recognize the application of other processes and/or the use of other materials.
In the present disclosure, the terms "first," "second," and the like are used for descriptive purposes only and are not to be construed as indicating or implying a relative importance or implicitly indicating the number of technical features indicated. Thus, a feature defining "a first" or "a second" may explicitly or implicitly include one or more of the described features. In the description of the present utility model, the meaning of "a plurality" is two or more, unless explicitly defined otherwise.
It should be noted that, unless explicitly stated or limited otherwise, the terms "connected," "connected," and "connected" are to be construed broadly, and may be, for example, fixedly connected, detachably connected, or integrally connected: can be mechanically connected, electrically connected or can be communicated with each other; can be directly connected or indirectly connected through an intermediate medium, and can be communicated with the inside of two elements or the interaction relationship of the two elements. The specific meaning of the terms in this disclosure will be understood by those of ordinary skill in the art as the case may be. In addition, in the drawings, the thickness, proportion, and size of the parts are exaggerated or reduced for the purpose of effectively describing the technical contents.
The following detailed description of specific embodiments of the utility model is provided in connection with the accompanying drawings and examples in order to provide a better understanding of the aspects of the utility model and advantages thereof. However, the following description of specific embodiments and examples is for illustrative purposes only and is not intended to be limiting of the utility model.
Fig. 1 illustrates a catalytic pyrolysis reaction system provided by the present utility model, which includes a pyrolysis furnace 100, a catalytic reforming furnace 200, a condensation tank 300, a gas supply unit 400, and a gas chromatograph 500.
Wherein the pyrolysis furnace 100 includes a first heater 101, a first reaction tube 102, and a crucible 103. The first heater 101 is used to heat the first reaction tube 102. In the embodiment shown in fig. 1, the first reaction tube 102 includes a first low temperature zone 106, a first high temperature zone 107, and a second low temperature zone 108, the first high temperature zone 107 being located between the first low temperature zone 106 and the second low temperature zone 108. The first heater 101 is mainly used to heat the first high temperature region 107.
Crucible 103 is used to hold the reactants to be pyrolyzed. In the utility model, the reactant to be pyrolyzed can be one or more of coal, biomass, oil shale, plastics, residual oil and the like.
In the embodiment shown in fig. 1, the heating furnace 100 further includes a moving frame 104, and the crucible 103 is mounted on the moving frame 104, and the moving frame 104 is capable of moving within the first reaction tube 102 (i.e., is capable of moving within the range of the first low temperature region 106, the first high temperature region 107, and the second low temperature region 108), thereby moving the crucible 103 within the first reaction tube 102.
Before the first heater 101 heats the first high temperature region 107 to a predetermined pyrolysis temperature, the crucible 103 containing the reactants to be pyrolyzed is located in the first low temperature region 106, and is preheated in the first low temperature region 106. When the first high temperature zone 107 is heated to a predetermined pyrolysis temperature, the crucible 103 enters the first high temperature zone 107 under the action of the moving frame 104, the reactant to be pyrolyzed is pyrolyzed in the first high temperature zone 107 to generate volatile gas, and then the crucible 103 leaves the first high temperature zone 107 for a predetermined time and enters the second low temperature zone 108 to complete the fast pyrolysis. In the second low temperature zone 108, pyrolysis products (e.g., semicoke) and volatile gases may be cooled and then vented.
The pyrolysis furnace 100 provided by the utility model can realize the rapid pyrolysis of reactants to be pyrolyzed and the rapid cooling of pyrolysis products obtained after pyrolysis, so that the yield of volatile gases and the quality of pyrolysis products can be greatly improved.
In the embodiment shown in fig. 1, the pyrolysis furnace 100 further comprises a first temperature controller 105 connected to the first heater 101, the first temperature controller 105 being adapted to control the heating temperature of the first reaction tube 101.
The catalytic reforming furnace 200 includes a second heater 201 and a second reaction tube 202. Wherein the catalytic reforming furnace 200 is connected to the second low temperature zone of the pyrolysis furnace 100. A first valve 601 is installed on a connection line between the catalytic reforming furnace 200 and the pyrolysis furnace 100. The second heater 201 is used for heating the second reaction tube 202, and the second reaction tube 202 is loaded with a catalyst 207 for catalytically modifying the volatile gas.
In the embodiment shown in fig. 1, the second reaction tube 202 includes a third low temperature zone 204, a second high temperature zone 205, and a fourth low temperature zone 206, with the second high temperature zone 205 being located between the third low temperature zone 204 and the fourth low temperature zone 206. Wherein the catalyst 207 is loaded in the second high temperature zone 205. The second heater 201 is mainly used to heat the second high temperature region 205.
When the first valve 601 is opened and the second high temperature zone 205 is heated to a predetermined catalytic reforming temperature, the volatile gas can first enter the third low temperature zone 204 to be preheated and then enter the second high temperature zone 205 to be catalytically reformed under the action of the catalyst 207 to generate a reformed product. The upgraded product can then enter the fourth low temperature zone 206 to be cooled.
The separation of the catalyst from the reactant can be achieved by separating the catalyst from the catalyst in the catalytic reforming step. Moreover, effective catalytic effect can be achieved with a small amount of catalyst. The inventor finds that compared with the existing fluidized bed rapid pyrolysis reactor, the pyrolysis and catalytic modification of 5g of coal dust needs 30g of catalyst, and the catalytic pyrolysis reaction system provided by the utility model only needs 0.2g of catalyst for pyrolysis and catalytic modification of 5g of coal dust.
In the embodiment shown in fig. 1, the catalytic reforming furnace 200 further includes a second temperature controller 203 connected to the second heater 201, and the second temperature controller 203 is configured to control the heating temperature of the second reaction tube 201.
Optionally, the central axis of the second reaction tube 202 is parallel to the direction of flow of the volatile gas, facilitating contact of the volatile gas with the catalyst 207. In the embodiment shown in fig. 1, the central axis of the second reaction tube 202 is perpendicular to the ground, which facilitates the flow of the volatile gas and the contact of the volatile gas with the catalyst 207, thereby improving the catalytic reforming effect and efficiency.
A condensation duct 301 is provided in the condensation tank 300. In this embodiment, the cooling medium in the condensation duct 301 is alcohol. The cooling temperature of the alcohol can reach-80 ℃, and the gas to be condensed can be rapidly cooled.
The condensation tank 300 is connected to the fourth low temperature zone 206 of the second reaction tube 202 and to the second low temperature zone 108 of the first reaction tube 102. A second valve 602 is provided in the connection line between the condensation tank 300 and the second low temperature zone 108.
When the catalytic pyrolysis reaction system provided by the utility model is used, generally, when the first valve 601 is opened, the second valve 602 is closed; when the first valve 601 is closed, the second valve 602 is opened. When the first valve 601 is opened and the second valve 602 is closed, the upgraded product can enter the condensation tank 300 from the fourth low temperature zone 206, and be condensed and collected by the cooling medium in the condensation duct 301. When the first valve 601 is closed and the second valve 602 is opened, volatile gas can enter the condensation tank 300 from the second low temperature region 108 and be condensed and collected by the cooling medium in the condensation duct 301.
In the embodiment shown in fig. 1, the catalytic pyrolysis reaction system further comprises a gas supply unit 400 connected to the pyrolysis furnace 100. The gas supply unit 400 is used to supply various gases, such as nitrogen, argon, hydrogen, etc. In the embodiment shown in fig. 1, the gas supply unit 400 comprises a flow meter 401 and further comprises a third valve 402.
In the embodiment shown in fig. 1, the catalytic pyrolysis reaction system further includes a gas chromatograph 500 connected to the condensation tank 300, where the gas chromatograph 500 is used to detect non-condensable gases in the upgraded product or volatile gas that cannot be condensed and collected.
Alternatively, when the catalytic pyrolysis reaction system shown in fig. 1 is used for catalytic pyrolysis of coal dust, the following process is adopted:
filling pulverized coal into a crucible 103, opening a third valve 402, supplying one or more of nitrogen, helium, argon and hydrogen, heating a first high-temperature region 107 of a first reaction tube 102 to about 600-800 ℃ by adopting a first heater 101, and then operating a movable frame 104 to drive the crucible 103 to move from a first low-temperature region 106 to the first high-temperature region 107, wherein the pulverized coal is pyrolyzed to generate volatile gases (the volatile gases in the embodiment mainly comprise coal tar, CO and CO) 2 、H 2 、CH 4 、C 2 -C 3 Small molecule hydrocarbon gases). After pyrolysis for about 2-3 min, the moving frame 104 is operated to drive the crucible 103 to move from the first high temperature region 107 to the second low temperature region 108. Semicoke and volatile gas generated by pyrolysis can be cooled in the second low temperature region 108, and the semicoke is discharged. Heating the second high temperature region 205 of the second reaction tube 202 to about 550-700 ℃ by adopting a second heater 201, opening a first valve 601, closing a second valve 602, preheating volatile gas in the third low temperature region 204 of the pyrolysis furnace 100, and then in the second high temperature region 205, wherein in Ga-ZSM-5 or Ni-Al 2 O 3 Is catalytically modified into a modified product by the action of an isocatalyst (in this example, the main packageIncluding light coal tar). The upgraded product then enters fourth low temperature zone 206 to be cooled, then enters condensate tank 300, and is condensed and collected (i.e., tar) by the cooling medium in condenser 301. Detecting non-condensable gases (CO, CO) which cannot be condensed and collected by using a gas chromatograph 500 2 、CH 4 、C 2-3 Small molecule hydrocarbon gases).
It is apparent that the above examples are only illustrative of the present utility model and are not limiting of the embodiments. Other variations or modifications of the above teachings will be apparent to those of ordinary skill in the art. It is not necessary here nor is it exhaustive of all embodiments. And obvious variations or modifications thereof are contemplated as falling within the scope of the present utility model.
Claims (10)
1. A catalytic pyrolysis reaction system, comprising:
the pyrolysis furnace comprises a first heater, a first reaction tube and a crucible, wherein the first reaction tube comprises a first high-temperature zone, the first heater is used for heating the first reaction tube, the crucible is used for containing reactants to be pyrolyzed, and the crucible can move in the first reaction tube;
the catalytic reforming furnace comprises a second heater and a second reaction tube, and is connected with the pyrolysis furnace through a first valve, wherein the second heater is used for heating the second reaction tube, and the second reaction tube is loaded with a catalyst;
the condensing tank comprises a condensing pipe, is connected with the catalytic reforming furnace and is connected with the pyrolysis furnace through a second valve;
when the first heater heats the first high-temperature region to a preset pyrolysis temperature, the crucible can enter the first high-temperature region and leave the first high-temperature region within a preset time, and the reactant to be pyrolyzed generates volatile gas;
when the first valve is opened, the second valve is closed, and the second heater is heated to a preset catalytic modification temperature, the volatile gas can enter the catalytic modification furnace and is catalytically modified under the action of the catalyst to generate modified products, and the modified products can enter the condensation tank and are condensed and collected under the action of the condensation pipe;
when the first valve is closed and the second valve is opened, the volatile gas can enter the condensation tank and is condensed and collected under the action of the condensation pipe.
2. The catalytic pyrolysis reaction system of claim 1 wherein the pyrolysis furnace further comprises a moving frame on which the crucible is mounted, the moving frame being movable within the first reaction tube to move the crucible within the first reaction tube.
3. The catalytic pyrolysis reaction system of claim 1 wherein the first reaction tube further comprises a first low temperature zone and a second low temperature zone, the first high temperature zone being located between the first low temperature zone and the second low temperature zone;
wherein the crucible is located in the first low temperature zone when the first high temperature zone is not heated to the predetermined pyrolysis temperature; after the reactant to be pyrolyzed is pyrolyzed for the predetermined time, the crucible exits the first high temperature zone and enters the second low temperature zone.
4. The catalytic pyrolysis reaction system of claim 1 wherein the second reaction tube comprises a second high temperature zone, the catalyst being loaded in the second high temperature zone;
wherein when the second high temperature region is heated to the predetermined catalytic reforming temperature, the volatile gas can be catalytically reformed in the second high temperature region under the action of the catalyst to generate the reformed product.
5. The catalytic pyrolysis reaction system of claim 4 wherein the second reaction tube further comprises a third low temperature zone and a fourth low temperature zone, the second high temperature zone being located between the third low temperature zone and the fourth low temperature zone;
the third low-temperature zone is used for preheating the volatile gas, and the fourth low-temperature zone is used for cooling the modified product.
6. The catalytic pyrolysis reaction system of claim 1 wherein the cooling medium of the condenser tube is alcohol.
7. The catalytic pyrolysis reaction system of claim 1 wherein the central axis of the second reaction tube is parallel to the direction of flow of the volatile gas.
8. The catalytic pyrolysis reaction system of claim 1 wherein the pyrolysis furnace further comprises a first temperature controller coupled to the first heater for controlling the heating temperature of the first reaction tube;
the catalytic reforming furnace further comprises a second temperature controller connected with the second heater, and the second temperature controller is used for controlling the heating temperature of the second reaction tube.
9. The catalytic pyrolysis reaction system of claim 1 further comprising a gas chromatograph coupled to the condensation tank for detecting non-condensable gases in the upgraded product or the volatile gases that cannot be condensed and collected.
10. The catalytic pyrolysis reaction system of claim 1 further comprising a gas supply unit connected to the pyrolysis furnace, the gas supply unit comprising a flow meter.
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| CN202322924940.7U CN220149491U (en) | 2023-10-31 | 2023-10-31 | Catalytic pyrolysis reaction system |
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| CN202322924940.7U CN220149491U (en) | 2023-10-31 | 2023-10-31 | Catalytic pyrolysis reaction system |
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