CN216654570U - Novel multi-process multi-section coupling reactor - Google Patents

Novel multi-process multi-section coupling reactor Download PDF

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CN216654570U
CN216654570U CN202123032747.XU CN202123032747U CN216654570U CN 216654570 U CN216654570 U CN 216654570U CN 202123032747 U CN202123032747 U CN 202123032747U CN 216654570 U CN216654570 U CN 216654570U
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catalytic reaction
reactor
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郑长勇
任志恒
袁亚飞
张伟
刘星
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Shaanxi Yanchang Petroleum Group Co Ltd
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Abstract

The utility model relates to a novel multi-process multi-section coupling reactor. A multi-process multi-section coupling novel reactor comprises a reactor; a preparation area, an activation area and a catalytic reaction area are sequentially arranged in the reactor, and an inlet of the preparation area is connected with a feeding device and a preparation area gas inlet end; the activation area is connected with an air outlet end of the activation area; the inlet of the catalytic reaction zone is connected with the gas inlet end of the catalytic reaction zone, and the outlet of the catalytic reaction zone is connected with the outlet end; the preparation zone is isolated from the activation zone through a first buffer zone, and the activation zone is isolated from the catalytic reaction zone through a second buffer zone; outside the reactor, a first communicating device is arranged between the preparation area and the activation area, and a second communicating device is arranged between the activation area and the catalytic reaction area. The utility model greatly shortens the production period from the preparation of the catalyst to the production of the product.

Description

Novel multi-process multi-section coupling reactor
Technical Field
The utility model relates to a novel multi-process multi-section coupling reactor.
Background
The solid catalyst is widely applied to multiphase reactors such as fixed beds, fluidized beds, slurry beds and the like, but the preparation, activation and reaction of the solid catalyst are different in required atmosphere, pressure and temperature, so that the three links of the preparation, activation and reaction of the catalyst are generally required to be respectively and independently carried out, and the problems of complicated flow and great waste of resources are caused.
Disclosure of Invention
The utility model designs a novel three-section coupling reactor suitable for in-situ generation, activation and reaction of a catalyst aiming at the condition that the temperature difference required by preparation, activation and reaction is large, tail gas generated in one link can be just used as an active atmosphere or a multiphase reaction system of reaction raw materials in the next link, the catalyst in the system is sequentially subjected to in-situ generation, in-situ activation and reaction in different temperature areas of the reactor, the rings are buckled, and simultaneously generated heat and gas can be supplemented with each other.
The technical scheme of the utility model is as follows:
a multi-process multi-section coupling novel reactor comprises a reactor; a preparation area, an activation area and a catalytic reaction area are sequentially arranged in the reactor, and an inlet of the preparation area is connected with a feeding device and a preparation area gas inlet end; the activation area is connected with an air outlet end of the activation area; the inlet of the catalytic reaction zone is connected with the gas inlet end of the catalytic reaction zone, and the outlet of the catalytic reaction zone is connected with the outlet end; the preparation zone is isolated from the activation zone through a first buffer zone, and the activation zone is isolated from the catalytic reaction zone through a second buffer zone; outside the reactor, a first communicating device is arranged between the preparation area and the activation area, and a second communicating device is arranged between the activation area and the catalytic reaction area.
Preferably, inside the reactor, the preparation zone, the first buffer zone, the activation zone, the second buffer zone and the catalytic reaction zone are arranged from bottom to top in sequence; a first lifting pipe is arranged outside the reactor between the preparation zone and the activation zone, and a second lifting pipe is arranged between the activation zone and the catalytic reaction zone.
Outside the reactor, the activation zone and the catalytic reaction zone are also provided with a communicating pipe with a slide valve, one end of the communicating pipe with the slide valve is connected to the catalytic reaction zone, and the other end of the communicating pipe with the slide valve is connected to the first lifting pipe.
And the second buffer zone is also provided with a partition plate for further preventing the gas in the catalytic reaction zone from flowing into the activation zone.
The preparation area air inlet end and the catalytic reaction area air inlet end are both provided with air distributors, and the outlet of the catalytic reaction area is also provided with a cyclone separator for assisting in separating most of catalysts.
(II) or preferably, the preparation zone, the first buffer zone, the activation zone, the second buffer zone and the catalytic reaction zone are sequentially arranged from top to bottom in the reactor; outside the reactor, a first slide valve is arranged between the preparation area and the activation area, and a second slide valve is arranged between the activation area and the catalytic reaction area.
And a third riser is arranged outside the reactor, in the activation zone and the catalytic reaction zone.
And a gas distributor is arranged at the gas inlet end of the catalytic reaction zone, and a cyclone separator is arranged in the second buffer zone.
The feeding device is a hopper, and the hopper is connected with the preparation area through a slide valve.
The utility model has the technical effects that:
1. the preparation, activation and catalytic reaction of the catalyst can be synchronously realized in the multi-process multi-section coupling novel reactor, and the three processes are finished in respective functional areas, are relatively independent and are mutually coupled; compared with the traditional catalyst production and use separation mode, the production period from the preparation of the catalyst to the output of the product can be greatly shortened;
2. the activation zone has the dual functions of continuous activation and continuous regeneration: not only can activate the catalyst from the preparation area, but also has the function of burning carbon. The catalyst in the catalytic reaction zone is gradually reduced in activity due to carbon deposition or coking and the like, and can be returned to the activation zone for regeneration. The existence of the activation zone is beneficial to realizing long-period continuous operation of catalytic reaction, improving the productivity and saving the investment of catalyst regeneration equipment;
3. the temperatures required for preparation, activation and catalytic reactions generally have large differences, and energy complementation in different temperature regions can be realized by utilizing the difference. For example: the catalyst activation temperature and reaction temperature are maintained by the heat of the catalyst solids from the production zone, the heat conducted from the reactor walls, and the heat removed from the exothermic reaction. This further reduces the thermal load on the reactor.
Drawings
Fig. 1 is a schematic structural diagram of embodiment 2 of the present invention.
Fig. 2 is a schematic structural diagram of embodiment 3 of the present invention.
Fig. 3 is a schematic structural diagram of embodiment 4 of the present invention.
Fig. 4 is a schematic structural diagram of embodiment 5 of the present invention.
Reference numerals: 1. a preparation area; 2. an activation zone; 3. a catalytic reaction zone; 4. a first riser; 5. a second riser; 6. a storage bin; 7. a gas distributor; 8. a gas separator; 9. a communicating pipe with a slide valve; 10. a first spool valve; 11. a second spool valve; 12. a third riser.
Detailed Description
Example 1
A multi-process multi-section coupling novel reactor comprises a reactor; a preparation area 1, an activation area 2 and a catalytic reaction area 3 are sequentially arranged in the reactor, and an inlet of the preparation area 1 is connected with a feeding device and a gas inlet end of the preparation area 1; the activation region 2 is connected with an air outlet end of the activation region 2; the inlet of the catalytic reaction zone 3 is connected with the gas inlet end of the catalytic reaction zone 3, and the outlet is connected with the outlet end; wherein, the preparation area 1 is isolated from the activation area 2 by a first buffer area, and the activation area 2 is isolated from the catalytic reaction area 3 by a second buffer area; outside the reactor, a first communication device is arranged between the preparation area 1 and the activation area 2, and a second communication device is arranged between the activation area 2 and the catalytic reaction area 3.
Example 2
On the basis of the embodiment 1, the method further comprises the following steps:
inside the reactor, a preparation zone 1, a first buffer zone, an activation zone 2, a second buffer zone and a catalytic reaction zone 3 are sequentially arranged from bottom to top; outside the reactor, a first lifting pipe 4 is arranged between the preparation area 1 and the activation area 2, and a second lifting pipe 5 is arranged between the activation area 2 and the catalytic reaction area 3. As shown in fig. 1.
Example 3
On the basis of embodiment 2, the method further comprises the following steps: outside the reactor, the activation zone 2 and the catalytic reaction zone 3 are also provided with a communicating pipe 9 with a slide valve, one end of the communicating pipe 9 with the slide valve is connected to the catalytic reaction zone 3, and the other end is connected to the first lifting pipe 4. As shown in fig. 2. The solid particles in the catalytic reaction zone 3 are brought back to the activation zone 2 to realize the regeneration of the catalyst. The second buffer zone is also provided with a partition plate for further preventing the gas in the catalytic reaction zone 3 from entering the activation zone 2.
The gas distributor 7 is arranged at the gas inlet end of the preparation area 1 and the gas inlet end of the catalytic reaction area 3, and the cyclone separator is arranged at the outlet of the catalytic reaction area 3 to assist in separating most of the catalyst.
Specific application example- -in situ preparation of Fe-CNTs and application of Fe-CNTs in catalyzing F-T reaction to prepare synthetic oil
The catalyst raw material is loaded with FexOySolid microspheres P with a suitable particle size distribution: fexOyP, solid microspheres P: fexOythe/P enters the preparation zone 1 from the hopper and is mixed with the carbon source CH in the preparation zone 14Gas (namely Gas-1) meets, under the high temperature environment of 600-800 ℃, the iron compound catalyzes the cracking of the carbon source and generates the Carbon Nano Tubes (CNTs) and H in situ2. Unreacted carbon source CH4Gas and in situ generated H2As a first mixed gas, passes upward through the activation zone2, with Fe elevated theretoxOyCNTs/P, at 250-350 ℃ in the first gas mixture2Mixing FexOyReducing the CNTs/P to Fe-CNTs/P, wherein the residence time of the catalyst raw material is 0.5-20 h. The Gas from the activation zone 2 is a second mixed Gas Gas-2 containing methane, hydrogen and water vapor, and after dehumidification by a dryer and pressurization by a circulating compressor, the residual Gas is taken as a circulating Gas and divided into two parts according to the proportion of 5:1 to 1:5, and the two parts are respectively merged into feed Gas Gas-1 and Gas-3. And the Fe-CNTs/P which is the iron-based catalyst after reduction and activation in the activation zone 2 is lifted to the catalytic reaction zone 3 again, the raw material synthesis Gas (Gas-3) is catalyzed by the Fe-CNTs/P to generate low-molecular-weight straight-chain alkane at the low temperature of 150-250 ℃, the product and the unreacted raw material synthesis Gas are fourth mixed Gas and come out from the upper part of the reactor to form Gas-4. After reacting for a period of time, the catalyst with gradually reduced activity in the catalytic reaction zone 3 due to carbon deposition or coking and the like can return the solid particles in the catalytic reaction zone 3 to the activation zone 2 for regeneration through the communication device with the slide valve, and then enter the next use cycle. The composition of the mixed gas referred to in this example is detailed in the attached table 1.
Table 1 attached gas composition table 1
Figure DEST_PATH_IMAGE002
。
Example 4
On the basis of embodiment 1, the method further comprises the following steps:
inside the reactor, a preparation zone 1, a first buffer zone, an activation zone 2, a second buffer zone and a catalytic reaction zone 3 are sequentially arranged from top to bottom; outside the reactor, a first slide valve 10 is arranged between the preparation area 1 and the activation area 2, and a second slide valve 11 is arranged between the activation area 2 and the catalytic reaction area 3. As shown in fig. 3.
Example 5
On the basis of embodiment 4, the method further comprises the following steps:
and a third riser 12 is arranged outside the reactor, in the activation zone 2 and the catalytic reaction zone 3, and solid particles in the catalytic reaction zone 3 are brought back to the activation zone 2, so that the regeneration of the catalyst is realized. And a gas distributor 7 is arranged at the gas inlet end of the catalytic reaction zone 3, and a cyclone separator is arranged in the second buffer zone. The feeding device is a hopper, and the hopper is connected with the preparation area 1 through a slide valve. As shown in fig. 4.
Specific application example- -in situ preparation of NiCNTs and for catalysis of C4Selective hydrogenation of butadiene to 1-butene
The catalyst raw material is solid microsphere N with proper particle size distributioniO/SiO2Solid microspheres NiO/SiO2From the hopper into the preparation zone 1, where it is mixed with a carbon source C4Gas (Gas-1) meets each other, and under the high temperature environment of 600-2. Unreacted carbon source C4Gas (Gas-1) and in situ generated H2(first mixture) passes down through activation zone 2 and N moves down to this point via slide valveiO-CNTs/SiO2Meet the H content in the first mixed gas at the temperature of 250-450 DEG C2Will NiO-CNTs/SiO2Reduction to Ni-CNTs/SiO2The residence time of the catalyst feed at this point is from 0.5 to 20 hours. The Gas from the activation zone 2 is a second mixed Gas Gas-2 containing C1-C4Low carbon hydrocarbon, hydrogen and water vapor are dehumidified by a dryer and pressurized by a circulating compressor, and the rest Gas is divided into two parts according to the proportion of 10:1 to 1:10 and respectively merged into feed Gas Gas-1 and Gas-3. The nickel-based catalyst which is subjected to reduction activation in the activation zone 2 moves downwards to the catalytic reaction zone 3 through a slide valve, and the carbon source C is at a low temperature of 150-260 DEG C4Butadiene in the Gas (Gas-3) is catalyzed by Fe-CNTs/Ps to generate 1-butene, and the product and unreacted raw material synthesis Gas are fourth mixed Gas and come out from the upper part of the catalytic reaction zone 3 to be Gas-4. The composition of the mixed gas referred to in this example is detailed in the attached table 2.
TABLE 2 attached gas composition TABLE 2
Figure DEST_PATH_IMAGE003
。

Claims (9)

1. A multi-process multi-section coupling novel reactor comprises a reactor; the method is characterized in that: a preparation area (1), an activation area (2) and a catalytic reaction area (3) are sequentially arranged in the reactor, and an inlet of the preparation area (1) is connected with a feeding device and an air inlet end of the preparation area (1); the activation area (2) is connected with an air outlet end of the activation area (2); the inlet of the catalytic reaction zone (3) is connected with the gas inlet end of the catalytic reaction zone (3), and the outlet is connected with the outlet end; wherein the preparation zone (1) is isolated from the activation zone (2) by a first buffer zone, and the activation zone (2) is isolated from the catalytic reaction zone (3) by a second buffer zone; outside the reactor, a first communication device is arranged between the preparation area (1) and the activation area (2), and a second communication device is arranged between the activation area (2) and the catalytic reaction area (3).
2. The multi-process multi-section coupled novel reactor according to claim 1, characterized in that: inside the reactor, a preparation zone (1), a first buffer zone, an activation zone (2), a second buffer zone and a catalytic reaction zone (3) are sequentially arranged from bottom to top; outside the reactor, a first lifting pipe (4) is arranged between the preparation area (1) and the activation area (2), and a second lifting pipe (5) is arranged between the activation area (2) and the catalytic reaction area (3).
3. The multi-process multi-section coupled novel reactor according to claim 2, characterized in that: outside the reactor, the activation zone (2) and the catalytic reaction zone (3) are also provided with a communicating pipe (9) with a slide valve, one end of the communicating pipe (9) with the slide valve is connected to the catalytic reaction zone (3), and the other end is connected to the first lifting pipe (4).
4. The multi-process multi-section coupled novel reactor according to claim 3, wherein: the second buffer area is also provided with a clapboard.
5. The novel multi-process multi-section coupled reactor of claim 4, wherein: the preparation area (1) inlet end and catalytic reaction area (3) inlet end all are equipped with gas distributor (7), and the export in catalytic reaction area (3) still is equipped with cyclone.
6. The multi-process multi-section coupled novel reactor according to claim 1, characterized in that: inside the reactor, a preparation zone (1), a first buffer zone, an activation zone (2), a second buffer zone and a catalytic reaction zone (3) are sequentially arranged from top to bottom; outside the reactor, a first slide valve (10) is arranged between the preparation area (1) and the activation area (2), and a second slide valve (11) is arranged between the activation area (2) and the catalytic reaction area (3).
7. The multi-process multi-section coupled novel reactor according to claim 6, wherein: and a third riser (12) is arranged outside the reactor, in the activation zone (2) and the catalytic reaction zone (3).
8. The multi-process multi-section coupled novel reactor according to claim 7, wherein: and a gas distributor (7) is arranged at the gas inlet end of the catalytic reaction zone (3), and a cyclone separator is arranged in the second buffer zone.
9. The multi-process multi-section coupled novel reactor according to claim 5 or claim 8, characterized in that: the feeding device is a hopper, and the hopper is connected with the preparation area (1) through a slide valve.
CN202123032747.XU 2021-12-06 2021-12-06 Novel multi-process multi-section coupling reactor Active CN216654570U (en)

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Application Number Priority Date Filing Date Title
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