CN216024776U - Pyrolysis reactor of high-temperature fluidized bed - Google Patents
Pyrolysis reactor of high-temperature fluidized bed Download PDFInfo
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- CN216024776U CN216024776U CN202121855445.XU CN202121855445U CN216024776U CN 216024776 U CN216024776 U CN 216024776U CN 202121855445 U CN202121855445 U CN 202121855445U CN 216024776 U CN216024776 U CN 216024776U
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Abstract
The utility model belongs to the technical field of chemical equipment preparation, and particularly relates to a high-temperature fluidized bed cracking reactor. The reactor is of a cylindrical structure, the bottom of the reactor is provided with a process gas inlet, and the top of the reactor is provided with a generated gas outlet; the middle lower part in the reactor is provided with a flue gas heater group, the middle upper part in the reactor is provided with a cyclone separator, the bottom of the cyclone separator is provided with a blanking leg, and the blanking leg is communicated with a reaction bed layer arranged in the middle of the reactor. The process gas enters a gas distributor of the reactor and is uniformly distributed, then enters a reaction bed layer, a flue gas heater group is arranged in the bed layer, after the process gas is heated by a flue gas heat exchanger, the process gas carries out mass transfer and reaction in the bed layer to generate a gas product, the reacted process gas enters a cyclone separator after a gas blocking dust remover breaks large bubbles, and after a catalyst is separated, the reacted process gas flows out from a generated gas outlet at the top of the reactor and enters the next working procedure.
Description
Technical Field
The utility model belongs to the technical field of chemical equipment preparation, and particularly relates to a high-temperature fluidized bed cracking reactor.
Background
The cracking reaction is a high-temperature endothermic reaction, and the temperature range of the general cracking reaction is 450 DEG C
-1200 ℃. The cracking reactor is a necessary device for cracking reaction, and is characterized by high temperature, complex structure, high quality requirement and various used materials. The existing reactor mostly uses molten salt as heating medium, the use temperature of the molten salt is 150-550 ℃, but the sodium nitrite can generate slow decomposition phenomenon above 450 ℃, so the working temperature of the conventional utilization system of the molten salt is within 250-350 ℃. The existing molten salt heating mode cannot be used for a long period.
The fluidized bed catalytic reactor is a device which takes solid as catalyst and utilizes gas or liquid to pass through a solid particle bed layer from bottom to top to make the solid in a suspension state to carry out gas-solid phase or liquid-solid phase catalytic reaction, and is widely applied to the fields of petroleum refining industry, inorganic chemical industry, organic chemical industry and the like.
Disclosure of Invention
The utility model aims to provide a high-temperature fluidized bed cracking reactor aiming at the technical problems of the existing cracking reactor. The reactor is suitable for the endothermic reaction process, and the temperature of a reaction bed layer can be more effectively controlled by utilizing the flue gas heat exchanger; can be better used in the production of cyanamide.
In order to realize the purpose of the utility model, the technical scheme of the utility model is as follows:
a high-temperature fluidized bed cracking reactor is of a cylindrical structure (namely a cylindrical shell is arranged outside the reactor), a process gas inlet is arranged at the bottom of the reactor, and a generated gas outlet is arranged at the top of the reactor; the middle lower part in the reactor is provided with a flue gas heater group, the middle upper part in the reactor is provided with a cyclone separator, the bottom of the cyclone separator is provided with a blanking leg which is communicated with a reaction bed layer arranged in the middle of the reactor, and the reaction bed layer is filled with a catalyst for cracking.
The gas of the process gas inlet at least comprises ammonia gas and/or carbon dioxide gas. The product gas outlet gas comprises at least cyanamide. Ammonia and/or carbon dioxide gas are used as carrier gas of the fluidized bed, wherein substances such as urea, melamine and the like can be added as raw materials, and the ammonia and the carbon dioxide still exist as long as the product of the generated gas is cyanamide.
The pressure in the reactor is 0.2-1.0MPa, the reaction pressure is too high, and the reaction conversion rate is reduced. The reaction pressure is too low, the equipment size is too large, and the manufacturing cost is increased.
As a preferred embodiment in this application, a gas distributor is provided at the process gas inlet.
As a preferred embodiment in the present application, the gas distributor comprises a ring-shaped branch pipe, a nozzle or a jet pipe; the annular branch pipe is provided with a nozzle or a spray pipe; the annular branch pipe is connected with a gas inlet pipe of a process gas inlet through a plurality of straight pipes. The gas enters the annular branch pipe from the gas inlet and is redistributed to the nozzle or the spray pipe, and the nozzle or the spray pipe has certain resistance, so that the aim of uniform gas distribution and further uniform fluidization of the reactor is fulfilled by depending on the resistance.
As a preferred embodiment in the present application, the flue gas heater group comprises a flue gas inlet ring pipe, a flue gas outlet ring pipe, a branch pipe and a flue gas heat exchange pipe; the flue gas heat exchange tube is vertically arranged inside the reactor, the flue gas inlet ring tube and the flue gas outlet ring tube are arranged outside the reactor, and the branch tube penetrates through the reactor shell to be communicated with the flue gas heat exchange tube in the reactor. The medium in the flue gas heater group is high-temperature flue gas which can come from a gas boiler or a coal-fired boiler, and the temperature range of the flue gas is 450-1200 ℃. The heating requirements of the cleavage reactor can be over-met.
As a better embodiment in the present application, the flue gas heat exchange tubes are circumferentially and uniformly distributed, and a plurality of turns, for example, 3 turns, are provided on different diameters; 28 flue gas heat exchange tubes are uniformly distributed in the first circle (outermost circle), 16 flue gas heat exchange tubes are distributed in the second circle (middle circle), and 6 flue gas heat exchange tubes are distributed in the third circle (innermost circle).
As a preferred embodiment in this application, a urea inlet is provided in the reaction bed at the upper end of the gas distributor.
Another proposal of the cyclone of the high temperature fluidized bed cracking reactor is that the cyclone is arranged outside the reactor.
As a preferred embodiment in this application, the cyclone is a multi-stage cyclone, for example a 2-stage cyclone. The single-stage cyclone can play a good role in separating large-particle catalysts, but the separation efficiency of small particles such as 10-100 micron particles can only reach about 90%, and the multistage cyclone can further improve the separation efficiency and further separate fine particles.
The reaction principle of the device is as follows:
the process gas enters a gas distributor of the reactor through a process gas inlet and is uniformly distributed, then enters a reaction bed layer, a flue gas heater group is arranged in the bed layer, after the process gas is heated by a flue gas heat exchanger, the process gas carries out mass transfer and reaction in the bed layer to generate a gas product, the reacted process gas enters a cyclone separator after a gas blocking dust remover breaks large bubbles, and after a catalyst is separated, the reacted process gas flows out from a generated gas outlet at the top of the reactor and enters the next working procedure.
Compared with the prior art, the utility model has the beneficial effects that:
the reactor is suitable for endothermic reaction process, and the temperature of the reaction bed can be more effectively controlled by using the flue gas heat exchanger.
The reactor can be used for heating under high temperature conditions, and the reaction temperature can easily reach more than 500 ℃. The structure of the flue gas heat exchanger can achieve self-balance of thermal stress under high-temperature transformation. The temperature difference between the inlet and the outlet can reach 100-300 ℃, and the reactor and the heat exchanger cannot be damaged by thermal stress.
And (III) the arrangement mode of the annular gas inlet and the flue gas pipe in the reactor enables the flue gas to be uniform in the heat exchange pipe, and the heat exchange efficiency of the heat exchange flue gas pipe is improved.
And (IV) the arrangement mode of the flue gas heat exchange tubes is adopted, so that the most heat exchange tubes are arranged in the limited space, and the space utilization rate is improved.
And (V) the smoke heat exchange tubes are arranged, and welding points of the heat exchange tubes are connected to the lower part and the top of the equipment and have overhaul spaces. The manufacture, the installation and the maintenance are convenient.
Description of the drawings:
FIG. 1 is a schematic view of the structure of a pyrolysis fluidized bed cracking reactor according to the present invention.
FIG. 2 is a schematic view of the structure of the gas distributor according to the present invention.
Fig. 3 is a schematic structural diagram of the flue gas heat exchanger of the present invention.
Wherein, 1: cylindrical housing, 2: process gas inlet, 3: inlet gas distributor, 3-1: distributor header, 3-2: distributor branch pipe, 3-3: nozzle, 4: flue gas heat exchanger group, 4-1: a flue gas inlet ring pipe, 4-2: flue gas outlet ring pipe, 4-3: branch pipe, 4-4: flue gas heat exchange tube, 5: cyclone separator, 6: blanking legs, 7: reaction bed, 8: and a generated gas outlet.
Detailed Description
A high-temperature fluidized bed cracking reactor is of a cylindrical structure (namely a cylindrical shell is arranged outside the reactor), a process gas inlet is arranged at the bottom of the reactor, and a generated gas outlet is arranged at the top of the reactor; the middle lower part in the reactor is provided with a flue gas heater group, the middle upper part in the reactor is provided with a cyclone separator, the bottom of the cyclone separator is provided with a blanking leg which is communicated with a reaction bed layer arranged in the middle of the reactor, and the reaction bed layer is filled with a catalyst for cracking.
A gas distributor is arranged at the process gas inlet. The gas distributor comprises an annular branch pipe, a nozzle or a spray pipe; the annular branch pipe is provided with a nozzle or a spray pipe; the annular branch pipe is connected with a gas inlet pipe of a process gas inlet through a plurality of straight pipes. The gas enters the annular branch pipe from the gas inlet and is redistributed to the nozzle or the spray pipe, and the nozzle or the spray pipe has certain resistance, so that the aim of uniform gas distribution and further uniform fluidization of the reactor is fulfilled by depending on the resistance.
The flue gas heater group comprises a flue gas inlet ring pipe, a flue gas outlet ring pipe, a branch pipe and a flue gas heat exchange pipe; the flue gas heat exchange tube is vertically arranged inside the reactor, the flue gas inlet ring tube and the flue gas outlet ring tube are arranged outside the reactor, and the branch tube penetrates through the reactor shell to be communicated with the flue gas heat exchange tube in the reactor.
The flue gas heat exchange tubes are circumferentially and uniformly distributed, a plurality of circles, such as 3 circles, are arranged on different diameters, and each circle is provided with a plurality of flue gas heat exchange tubes.
The reaction bed layer at the upper end of the gas distributor is provided with a urea inlet.
The cyclone of the reactor may be arranged outside the reactor. The cyclone may be located inside the reactor.
The cyclone separator is a multi-stage cyclone separator, such as a 2-stage cyclone separator.
In order to facilitate an understanding of the inventive content of the present invention, the process described in the present invention will be further elucidated with reference to the drawings and the detailed description. It should not be understood that the scope of the above-described subject matter of the present invention is limited to the following examples.
In the description of the present invention, it should be noted that the terms "center", "upper", "lower", "left", "right", "vertical", "horizontal", "inner", "outer", and the like indicate orientations or positional relationships based on the orientations or positional relationships shown in the drawings or orientations or positional relationships that the products of the present invention are conventionally placed in use, and are only for convenience of describing the present invention and simplifying the description, but do not indicate or imply that the device or element to which the description refers must have a specific orientation, be constructed in a specific orientation, and be operated, and thus should not be construed as limiting the present invention. Furthermore, the terms "first," "second," "third," and the like are used solely to distinguish one from another and are not to be construed as indicating or implying relative importance.
Furthermore, the terms "horizontal", "vertical", "overhang" and the like do not imply that the components are required to be absolutely horizontal or overhang, but may be slightly inclined. For example, "horizontal" merely means that the direction is more horizontal than "vertical" and does not mean that the structure must be perfectly horizontal, but may be slightly inclined.
In the description of the present invention, it should also be noted that, unless otherwise explicitly specified or limited, the terms "disposed," "mounted," "connected," and "connected" are to be construed broadly and may, for example, be fixedly connected, detachably connected, or integrally connected; can be mechanically or electrically connected; they may be connected directly or indirectly through intervening media, or they may be interconnected between two elements. The specific meanings of the above terms in the present invention can be understood in specific cases to those skilled in the art.
In addition, it should be noted that, in the present invention, if the specific structures, connection relationships, position relationships, power source relationships, and the like are not written in particular, the structures, connection relationships, position relationships, power source relationships, and the like related to the present invention can be known by those skilled in the art without creative work on the basis of the prior art.
EXAMPLE 1 application of the reactor in the production of cyanamide
As shown in fig. 1, cyanamide substances include cyanamide, dicyandiamide, melamine, etc., melamine can be further cracked into cyanamide by high temperature, in this example, the fluidized bed cracking reactor of the present invention is used for cracking melamine to produce cyanamide.
A pyrolysis reactor of a high-temperature fluidized bed mainly comprises a cylindrical shell 1, a process gas inlet 2, an inlet gas distributor 3 and a flue gas heater group 4, wherein a cyclone separator 5 is arranged above the high-temperature fluidized bed, a blanking leg 6 is arranged at the bottom of the cyclone separator, and the blanking leg is introduced into a reaction bed layer 7. The top of the reactor is provided with a generated gas outlet 8, and the reactor is filled with a cracking catalyst.
The medium in the flue gas heater group 4 is high-temperature flue gas which is provided by natural gas combusted by a hot blast stove, and the temperature range of the flue gas is 800 ℃. The heating requirements of the cleavage reactor can be over-met.
The gas at the process gas inlet is ammonia gas and CO2And (4) mixing the gases. The generated gas outlet gas mainly comprises cyanamide, ammonia gas and CO2. The pressure in the reactor is 0.2-1.0 MPa.
The gas distributor comprises a ring-shaped branch pipe and a spray pipe. The cyclone separator may be provided as a 2-stage cyclone separator. The cyclone may be located inside the reactor.
The flue gas heater group is provided with a flue gas inlet ring pipe and a flue gas outlet ring pipe outside the equipment, and a plurality of branch pipes respectively penetrate through the reactor shell and are connected with the flue gas heat exchange pipe in the reactor. The flue gas heat exchange tubes of the flue gas heater group are circumferentially and uniformly distributed, 3 circles are arranged on different diameters, 28 are uniformly distributed in the first circle (the outermost circle), 16 are distributed in the second circle (the middle circle) and 6 are distributed in the third circle (the innermost circle) from outside to inside.
The method for producing cyanamide by using the reactor comprises the steps of heating the fluidized bed cracking reactor by using the flue gas for producing cyanamide, wherein the reaction temperature is 400-2The process gas, which is the main gas, is uniformly distributed in the gas distributor 3 entering the reactor from the process gas inlet 2 and then enters the reaction bed 7. A flue gas heater group 4 is arranged in the bed layer to provide heat for the cracking reaction, the process gas is used as fluidization carrier gas in the bed layer 7, the reaction raw material is melamine or urea, mass transfer and reaction are carried out in the bed layer, the melamine and the urea are cracked into cyanamide, the reacted process gas enters a cyclone separator, and after a catalyst is separated, the main components of the process gas are ammonia gas and CO2And cyanamide, and then the resultant gas flows out of a product gas outlet 7 at the top of the reactor and enters a post-treatment step.
The production method of cyanamide by using the reactorCase 1: the production process of cyanamide includes heating the cracking reactor in a fluidized bed at 450 deg.c with the said fume. The pressure in the reactor was 0.3MPa and the temperature in the flue gas heater tube was 700 ℃. By using a gas mixture containing ammonia and CO2The process gas is uniformly distributed in a gas distributor 3 which enters the reactor from a process gas inlet 2 and then enters a reaction bed layer 7. A flue gas heater group 4 is arranged in the bed layer to provide heat for the cracking reaction, and the process gas is used as fluidization carrier gas in the bed layer 7. The height of the bed layer is provided with a urea inlet, urea is used as a reaction raw material and is sprayed into the bed layer of the reactor, mass transfer and reaction are carried out in the bed layer to generate a gas product, and the urea reacts to generate cyanamide, ammonia and CO2In the form of a gas phase in the reactor, and together with the carrier, forms a reaction gas whose main constituents are still cyanamide, ammonia and CO2. And the reacted generated gas enters a cyclone separator, after the catalyst is separated, the reacted generated gas flows out from a generated gas outlet 7 at the top of the reactor and enters the next post-treatment process. The conversion rate of the reaction is more than 60 percent, and the yield of the cyanamide is more than 50 percent.
Case 2: the production method of cyanamide comprises heating fluidized bed cracking reactor with the above flue gas at 500 deg.C. The pressure in the reactor was 0.4MPa and the temperature in the flue gas heater tube was 750 ℃. By using a gas mixture containing ammonia and CO2The process gas is uniformly distributed in a gas distributor 3 which enters the reactor from a process gas inlet 2 and then enters a reaction bed layer 7. A flue gas heater group 4 is arranged in the bed layer to provide heat for the cracking reaction, and the process gas is used as fluidization carrier gas in the bed layer 7. The height of the bed layer is provided with a urea inlet, urea is used as a reaction raw material and is sprayed into the bed layer of the reactor, mass transfer and reaction are carried out in the bed layer to generate a gas product, and the urea reacts to generate cyanamide, ammonia and CO2In the form of a gas phase in the reactor, and together with the carrier, forms a reaction gas whose main constituents are still cyanamide, ammonia and CO2. The generated gas after the reaction enters a cyclone separator, after the catalyst is separated, the generated gas flows out from a generated gas outlet 7 at the top of the reactor and enters the next post-treatmentAnd (5) working procedures. The conversion rate of the reaction is more than 70 percent, and the yield of the cyanamide is more than 60 percent.
Case 3: the production method of cyanamide comprises heating fluidized bed cracking reactor with the above flue gas at 600 deg.C. The pressure in the reactor was 0.4MPa and the temperature in the flue gas heater tube was 800 ℃. By using a gas mixture containing ammonia and CO2The process gas is uniformly distributed in a gas distributor 3 which enters the reactor from a process gas inlet 2 and then enters a reaction bed layer 7. A flue gas heater group 4 is arranged in the bed layer to provide heat for the cracking reaction, and the process gas is used as fluidization carrier gas in the bed layer 7. The height of the bed layer is provided with a urea inlet, urea is used as a reaction raw material and is sprayed into the bed layer of the reactor, mass transfer and reaction are carried out in the bed layer to generate a gas product, and the urea reacts to generate cyanamide, ammonia and CO2In the form of a gas phase in the reactor, and together with the carrier, forms a reaction gas whose main constituents are still cyanamide, ammonia and CO2. And the reacted generated gas enters a cyclone separator, after the catalyst is separated, the reacted generated gas flows out from a generated gas outlet 7 at the top of the reactor and enters the next post-treatment process. The conversion rate of the reaction is more than 90 percent, and the yield of the cyanamide is more than 80 percent.
The foregoing basic embodiments of the utility model and their various further alternatives can be freely combined to form multiple embodiments, all of which are contemplated and claimed herein. In the scheme of the utility model, each selection example can be combined with any other basic example and selection example at will. Numerous combinations will be known to those skilled in the art.
Although the present invention has been described in detail with respect to specific embodiments thereof, it will be understood by those skilled in the art that various changes in form and details may be made therein without departing from the scope of the utility model encompassed by the appended claims.
Claims (8)
1. The utility model provides a high temperature fluidized bed cracking reactor, this reactor is cylinder structure, its characterized in that: a process gas inlet (2) is arranged at the bottom of the reactor, and a generated gas outlet (8) is arranged at the top of the reactor; a smoke heater group (4) is arranged at the middle lower part in the reactor, a cyclone separator (5) is arranged at the middle upper part in the reactor, a blanking leg (6) is arranged at the bottom of the cyclone separator, and the blanking leg (6) is communicated with a reaction bed layer (7) arranged at the middle part of the reactor.
2. The high temperature fluidized bed cracking reactor of claim 1, wherein: a gas distributor (3) is arranged at the process gas inlet (2).
3. The high temperature fluidized bed cracking reactor of claim 2, wherein: the gas distributor (3) comprises a distributor main pipe (3-1), distributor branch pipes (3-2) and nozzles or spray pipes (3-3); a nozzle or a spray pipe (3-3) is arranged on the distributor branch pipe (3-2); the distributor main pipe (3-1) is connected with a gas inlet pipe of the process gas inlet (2) through a plurality of distributor branch pipes (3-2).
4. A pyrolysis fluidized bed cracking reactor according to claim 1 or 2, characterized in that: the flue gas heater group (4) comprises a flue gas inlet ring pipe (4-1), a flue gas outlet ring pipe (4-2), branch pipes (4-3) and flue gas heat exchange pipes (4-4); the flue gas heat exchange tubes (4-4) are vertically arranged inside the reactor, the flue gas inlet ring tube (4-1) and the flue gas outlet ring tube (4-2) are arranged outside the reactor, and the branch tubes (4-3) penetrate through the shell of the reactor and are communicated with the flue gas heat exchange tubes (4-4) in the reactor.
5. The high temperature fluidized bed cracking reactor of claim 4, wherein: the flue gas heat exchange tubes (4-4) are circumferentially and uniformly distributed and are arranged in a plurality of circles on different diameters.
6. The high temperature fluidized bed cracking reactor of claim 2, wherein: a urea inlet (9) is arranged on a reaction bed layer (7) at the upper end of the gas distributor (3).
7. The high temperature fluidized bed cracking reactor of claim 1, wherein: the cyclone of the reactor is arranged outside the reactor.
8. The high temperature fluidized bed cracking reactor of claim 1, wherein: the cyclone separator (5) is a multi-stage cyclone separator.
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| Application Number | Priority Date | Filing Date | Title |
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| CN202121855445.XU CN216024776U (en) | 2021-08-10 | 2021-08-10 | Pyrolysis reactor of high-temperature fluidized bed |
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| Application Number | Priority Date | Filing Date | Title |
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| CN202121855445.XU CN216024776U (en) | 2021-08-10 | 2021-08-10 | Pyrolysis reactor of high-temperature fluidized bed |
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