CN220238585U - Isothermal adiabatic reactor with wide adaptive temperature - Google Patents

Abstract

The utility model relates to a wide-adaptability temperature isothermal adiabatic reactor, and relates to the technical field of chemical reactors. The utility model discloses a wide-adaptation temperature isothermal adiabatic reactor, which comprises a shell, wherein a first cavity and a second cavity are arranged in the shell, a heat exchange channel is arranged in the second cavity, one end of the heat exchange channel is communicated with the first cavity, the other end of the heat exchange channel penetrates through the second cavity, a first catalyst layer is arranged in the first cavity, a second catalyst is filled in the heat exchange channel, fluid entering the first cavity moves along the heat exchange channel after reacting with the first catalyst layer and reacts with the second catalyst, and a heat exchange medium capable of exchanging heat with the heat exchange channel is filled in the second cavity so as to maintain the heat exchange channel in a preset temperature range. The operating temperature range of the reactor is enlarged, the application range is wide, the structure is simple, and the installation and the operation are convenient.

Description

Isothermal adiabatic reactor with wide adaptive temperature

Technical Field

The utility model relates to the technical field of chemical reactors, in particular to a wide-adaptability temperature isothermal adiabatic reactor.

Background

With the continued development of human society, the demand for energy, particularly clean and efficient liquid fuels, is becoming increasingly urgent. In the prior art, coal, natural gas, coke oven gas and various tail gases are generally used as raw materials to prepare synthetic gas, and then the synthetic gas is used for synthesizing liquid fuel and chemical products. The liquid fuel is synthesized by synthetic gas, such as gasoline, diesel oil and paraffin. The process of preparing low-carbon olefin with synthetic gas includes preparing low-carbon olefin, such as ethylene, propylene, butene, etc. with synthetic gas, methanol and dimethyl ether. The oxygen-containing compound prepared from the synthesis gas refers to a series of products such as low-carbon alcohol, methanol series, formaldehyde series, acetic acid series and the like prepared from the synthesis gas. These synthetic reactions are all produced by reaction under the action of a catalyst, which is a strongly exothermic reaction, and the catalyst requires a specific pressure and temperature range to effectively remove the heat of reaction. The reactors used in the synthesis in the prior art are: a shell-and-tube fixed bed reactor, a fluidized bed reactor and a slurry bed reactor.

In order to obtain high conversion rate and meet the increasingly large-scale requirements, the reactors are connected with heat exchangers in series, the water-cooled reactor is connected with a gas-mixing cold reactor, and the fixed bed reactor, the fluidized bed reactor and the slurry bed reactor are connected with each other in series, so that the process flow is complex, the occupied area is large, the investment is high, the operation difficulty is large, and in the middle and later period of catalyst use, the deactivation reaction of the catalyst is slowed down, the reaction load is transferred to the equipment connected with the catalyst in series, thereby changing the operation condition of the catalyst in the equipment connected with the equipment in series, the activity of the catalyst cannot be effectively exerted, and the service life of the catalyst is shortened.

Therefore, the utility model discloses a wide-adaptability temperature isothermal adiabatic reactor.

Disclosure of Invention

The utility model provides a wide-adaptation temperature isothermal adiabatic reactor, which expands the operation temperature range of the reactor, has wide application range and simple structure, and is convenient to install and operate.

The utility model provides a wide-adaptation temperature isothermal adiabatic reactor, which comprises a shell, wherein a first cavity and a second cavity are arranged in the shell, a heat exchange channel is arranged in the second cavity, one end of the heat exchange channel is mutually communicated with the first cavity, the other end of the heat exchange channel penetrates through the second cavity, a first catalyst layer is arranged in the first cavity, a second catalyst is filled in the heat exchange channel, fluid entering the first cavity reacts with the first catalyst layer, then moves along the heat exchange channel and reacts with the second catalyst, and a heat exchange medium capable of performing heat exchange with the heat exchange channel is filled in the second cavity so as to maintain the heat exchange channel in a preset temperature range.

In one embodiment, the shell is further provided with a third cavity located on one side, away from the first cavity, of the second cavity, a third catalyst layer is arranged in the third cavity, and two ends of the heat exchange channel are communicated with the first cavity and the third cavity. Through this embodiment, be provided with first cavity and third cavity respectively at the both ends of heat exchange tube, can realize multistage reaction to the fluid, carry out adiabatic reaction at first cavity and third cavity, carry out isothermal reaction in the second cavity, improve application scope.

In one embodiment, a first partition plate and a second partition plate are provided inside the housing, and the housing is partitioned into the first cavity, the second cavity, and the third cavity arranged in the same direction by the first partition plate and the second partition plate. Through this embodiment, keep the relative independence of first cavity, second cavity and third cavity, avoid appearing the heat exchange, be convenient for control temperature precision.

In one embodiment, the separator is made of a heat insulating material.

In one embodiment, the third cavity is provided with an air outlet pipe, a gas collector is arranged in the third cavity, the gas collector is covered on the periphery of the air outlet pipe, and the third catalyst layer is located on one side, away from the air outlet pipe, of the gas collector. By the embodiment, the gas in the third cavity can be intensively discharged; the third catalyst layer is isolated, gas and catalyst are separated, and the catalyst is prevented from being discharged from the third cavity along with the gas.

In one embodiment, the gas collector is conical in shape. Through this embodiment, the gas collector can also play the supporting role to the third catalyst layer, through setting up conical, improves the bearing capacity at gas collector middle part, avoids the middle part to take place to collapse, improves the stability to third catalyst layer support.

In one embodiment, the outlet pipe is further connected with a return pipe, and the return pipe is communicated with the first cavity, so that part of the fluid in the third cavity can flow back to the first cavity. According to the embodiment, the high-temperature gas in the third cavity can flow back into the first cavity, so that the gas temperature rising speed in the first cavity is improved.

In one embodiment, the first cavity is provided with an air inlet pipe, and the first cavity is internally provided with a gas distributor communicated with the air inlet pipe. According to the embodiment, the gas entering the first cavity from the gas inlet pipe can be uniformly distributed on the first catalyst layer, and the utilization efficiency of the catalyst is improved.

In one embodiment, the gas distributor can overlie the first catalyst layer for limiting the first catalyst layer. According to the embodiment, the gas distributor has the function of pressing the grid, and plays a limiting role on the first catalyst.

In one embodiment, the heat exchange channel includes a plurality of heat exchange tubes. Through this embodiment, the heat exchange tube is evenly distributed with each other at intervals, guarantees that it can carry out even guide to the gas in the first cavity.

The above-described features may be combined in various suitable ways or replaced by equivalent features as long as the object of the present utility model can be achieved.

Compared with the prior art, the isothermal adiabatic reactor with wide adaptive temperature has at least the following beneficial effects:

the first catalyst layer in the first cavity and the raw material gas generate exothermic synthesis reaction, the released heat causes the gas to be heated to the optimal use temperature range of the catalyst accommodated in the heat exchange channel, the heated gas in the first cavity enters the heat exchange channel and generates exothermic synthesis reaction with the second catalyst in the process of moving along the heat exchange channel, and the released heat is absorbed by the heat exchange medium in the second cavity at the moment, so that the temperature of the heat exchange channel is maintained in the preset temperature direction, the gas in the heat exchange channel is ensured to be always at the optimal reaction temperature, and the reaction efficiency is improved.

Drawings

The utility model will be described in more detail hereinafter on the basis of embodiments and with reference to the accompanying drawings.

Fig. 1 is a schematic structural view of the present utility model.

In the drawings, like parts are designated with like reference numerals. The figures are not to scale.

Reference numerals:

10. a housing; 11. a first cavity; 111. a first catalyst layer; 12. a second cavity; 13. a third cavity; 131. a third catalyst layer; 20. a first separator; 30. a second separator; 40. a heat exchange tube; 50. an air inlet pipe; 51. a gas distributor; 60. an air outlet pipe; 61. a gas collector.

Detailed Description

The utility model will be further described with reference to the accompanying drawings.

As shown in fig. 1, the utility model provides a wide-temperature-adaptation isothermal adiabatic reactor, which comprises a shell 10, wherein a first cavity 11 and a second cavity 12 are arranged in the shell 10, a heat exchange channel is arranged in the second cavity 12, one end of the heat exchange channel is mutually communicated with the first cavity 11, the other end of the heat exchange channel penetrates through the second cavity 12, a first catalyst layer 111 is arranged in the first cavity 11, a second catalyst is filled in the heat exchange channel, fluid entering the first cavity 11 reacts with the first catalyst layer 111 and then moves along the heat exchange channel and reacts with the second catalyst, and a heat exchange medium capable of exchanging heat with the heat exchange channel is filled in the second cavity 12 so as to maintain the heat exchange channel in a preset temperature range.

Specifically, the raw material gas inlet of the first cavity 11 is located above the first catalyst layer 111, and the port of the heat exchange channel communicating with the first cavity 11 is located inside the first catalyst layer 111 or below the first catalyst layer 111, so as to ensure that the raw material gas entering the first cavity 11 is firstly subjected to chemical reaction with the first catalyst layer 111 and then enters the heat exchange channel. The first catalyst layer 111 is in a non-closed plate structure, gas can move from top to bottom along the first catalyst layer 111, the thickness of the first catalyst layer 111 is adjustable, the thickness of the first catalyst layer can be increased or decreased according to actual use requirements or process requirements, and the catalyst in the first cavity 11 and the catalyst in the heat exchange channel can be the same type of catalyst or different types of catalyst. The heat exchange medium is low-temperature medium such as cooling water or cooling oil, the catalyst in the heat exchange channel reacts with gas in an exothermic way, the released heat is absorbed by boiling water outside the heat exchange channel to produce byproduct steam, and the temperature of the catalyst bed in the heat exchange channel is controlled within the optimal use temperature range by adjusting the steam pocket pressure, so that the activity of the catalyst is effectively exerted.

Further, when the raw material gas enters the shell 10, firstly enters the first cavity 11 to perform exothermic synthesis reaction with the catalyst in the first cavity 11, the released heat causes the gas to heat up to the optimal use temperature range of the catalyst in the heat exchange tube 40, the temperature of the gas entering the heat exchange tube 40 is ensured to meet the requirement, and the equipment for heating the gas is not required to be additionally arranged outside the shell 10, so that the reaction temperature of the raw material gas in the heat exchange channel can be ensured under the condition of lower temperature of the raw material gas, namely, the adaptive temperature range of the raw material gas is improved. The tube type fixed bed reactor, the fluidized bed reactor and the slurry bed reactor which are frequently used in engineering have the operating temperature of 180-270 ℃ in the reactor, and heat exchangers or reactors are required to be connected in series to widen the using temperature range, so that the flow is complex, the occupied area is large, the equipment investment is large, and the operating and maintenance difficulties are large. The reactor of the utility model has the operating temperature of 60-500 ℃, the single reactor does not need to be connected with a heat exchanger or a reactor in series, the temperature of inlet and outlet process gas can be adjusted by adjusting the height of the catalyst layer, the flow is simple, the occupied area is small, the equipment investment is small, the operation is simple, the operation is stable, the inspection and maintenance are few, and the structure is simple and is beneficial to large-scale.

In one embodiment, the housing 10 further has a third cavity 13 located on a side of the second cavity 12 away from the first cavity 11, a third catalyst layer 131 is disposed in the third cavity 13, and two ends of the heat exchange channel are communicated with the first cavity 11 and the third cavity 13. By the present embodiment, the first chamber 11 and the third chamber 13 are provided at both ends of the heat exchange tube 40, respectively, so that a multistage reaction can be realized on the fluid, an adiabatic reaction is performed in the first chamber 11 and the third chamber 13, an isothermal reaction is performed in the second chamber 12, and the application range is improved.

Specifically, the gas discharged through the heat exchange channel enters the third cavity 13 and reacts with the catalyst in the third cavity 13 in an exothermic synthesis reaction, and the released heat heats the gas so that the temperature of the gas discharged from the third cavity 13 is increased so as to be matched with the subsequent other reactions. The reaction of the catalyst in the first cavity 11 and the third cavity 13 with the gas is adiabatic reaction, the reaction of the catalyst in the heat exchange channel with the gas is isothermal reaction, the gas temperature of the first cavity 11 is lower than that in the heat exchange channel, the gas temperature in the third cavity 13 is higher than that in the heat exchange channel, different types or the same types of catalysts can be used according to process requirements, at least the catalysts in the heat exchange channel are guaranteed to be in an optimal temperature range, and the first cavity 11 and the third cavity 13 can be provided with the optimal catalysts according to the environmental temperature change range.

Further, the internal operation temperature of the reactor can be controlled by adjusting the heights of the first catalyst layer 111 and the third catalyst layer 131 and the pressure of the steam pocket, or the activity of the catalyst can be effectively exerted by introducing the high-temperature gas part of the third cavity 13 into the gas inlet of the first cavity 11 and maintaining the optimal temperature use range of the catalyst in the heat exchange channel.

In one embodiment, the housing 10 is internally provided with a first partition 20 and a second partition 30, and the housing 10 is internally partitioned into a first chamber 11, a second chamber 12, and a third chamber 13 arranged in the same direction by the first partition 20 and the second partition 30. Through this embodiment, keep the relative independence of first cavity 11, second cavity 12 and third cavity 13, avoid appearing the heat exchange, be convenient for control temperature accuracy.

In one embodiment, the separator is made of a thermally insulating material.

Specifically, the heat insulating material can be made of glass fiber, asbestos, rock wool, a vacuum plate and the like, and the partition plate can also be a heat insulating plate with a metal framework support.

In one embodiment, the third cavity 13 is provided with an air outlet pipe 60, the third cavity 13 is internally provided with a gas collector 61, the gas collector 61 is covered on the periphery of the air outlet pipe 60, and the third catalyst layer 131 is located on one side of the gas collector 61 away from the air outlet pipe 60. By the embodiment, the gas in the third cavity can be intensively discharged; the third catalyst layer 131 is isolated from the catalyst to separate the gas from the catalyst, and prevent the catalyst from being discharged from the third chamber 13 following the gas.

Specifically, the gas collector 61 may adopt a plate structure, the gas collector 61 is provided with a plurality of through holes for gas to pass through but the catalyst cannot pass through, the axis direction of the through holes faces the pipe orifice of the gas outlet pipe to play a role in collecting gas, the gas is prevented from carrying the catalyst through the filtering effect of the gas collector 61, and the gas is directly moved to the gas outlet pipe 60 through the effect of the through holes, so that the gas exhaust efficiency is improved.

In one embodiment, the gas collector 61 is conical in shape. Through this embodiment, the gas collector 61 can also play a supporting role on the third catalyst layer 131, and by providing a conical shape, the bearing capacity of the middle part of the gas collector 61 is improved, collapse of the middle part is avoided, and the stability of supporting the third catalyst layer 131 is improved.

Specifically, the gas collector 61 has a conical shape, and under the condition of consistent thickness, the gas collector 61 is convenient to process through holes for gas to pass through, the direction of the through holes is concentrated towards the middle part, so that the gas can directly enter the gas outlet pipe 60 for discharging, and the condition that turbulence occurs is avoided, so that the gas is concentrated in the third cavity 13 for a long time.

In one embodiment, the outlet pipe 60 is further connected to a return pipe which communicates with the first chamber 11 so that part of the fluid in the third chamber 13 can return to the first chamber 11. In the present embodiment, the high-temperature gas in the third chamber 13 can be returned to the first chamber 11, and the gas temperature rise rate in the first chamber 11 can be increased.

Specifically, the return pipe can introduce a part of the gas heated in the third cavity 13 into the first cavity 11, and recycle the preheating, so that the gas entering the heat exchange channel can be quickly raised to the optimal temperature, and the gas heating efficiency is improved.

In one embodiment, the first chamber 11 is provided with an air inlet pipe 50, and the first chamber 11 is internally provided with a gas distributor 51 communicating with the air inlet pipe 50. With the present embodiment, the gas entering the first chamber 11 from the gas inlet pipe 50 can be uniformly distributed in the first catalyst layer 111, and the catalyst utilization efficiency can be improved.

Specifically, as shown in fig. 1, the outer wall of the gas distributor 51 is provided with a plurality of overflow holes, and the gas entering the first cavity 11 is dispersed through the overflow holes, so that the raw material gas can reach each part on the surface of the first catalyst layer 111 more quickly, the moving time of the raw material gas to the first catalyst layer 111 is shortened, and the reaction efficiency is improved.

In one embodiment, the gas distributor 51 can overlie the first catalyst layer 111 for limiting the first catalyst layer 111. With the present embodiment, the gas distributor 51 plays a role of both the pressure grid and the limit for the first catalyst.

Specifically, the gas distributor 51 may also directly contact the surface of the first catalyst layer 111, and the gas distributor 51 may perform a function of compacting the upper surface of the first catalyst layer 111 while forming a plurality of overflow holes on the gas distributor 51.

In one embodiment, the heat exchange channel includes a plurality of heat exchange tubes 40. By this embodiment, the heat exchange tubes 40 are uniformly distributed at intervals between each other, ensuring that they can uniformly guide the gas in the first chamber 11.

Specifically, a plurality of support plates can be further disposed in the second cavity 12, the support plates are connected with the side walls of the second cavity 12 through the pull rods, the heat exchange tubes 40 penetrate through the support plates, the heat exchange tubes 40 are positioned through the support plates, and structural stability of the heat exchange tubes 40 is improved.

In the description of the present utility model, it should be understood that the terms "upper," "lower," "bottom," "top," "front," "rear," "inner," "outer," "left," "right," and the like indicate or are based on the orientation or positional relationship shown in the drawings, merely to facilitate description of the present utility model and to simplify the description, and do not indicate or imply that the devices or elements referred to must have a particular orientation, be configured and operated in a particular orientation, and thus should not be construed as limiting the present utility model.

While the utility model has been described with reference to a preferred embodiment, various modifications may be made and equivalents may be substituted for elements thereof without departing from the scope of the utility model. In particular, the technical features mentioned in the respective embodiments may be combined in any manner as long as there is no structural conflict. The present utility model is not limited to the specific embodiments disclosed herein, but encompasses all technical solutions falling within the scope of the claims.

Claims (10)

1. The utility model provides a wide adaptation temperature isothermal adiabatic reactor, its characterized in that, includes the casing, the inside of casing has first cavity and second cavity, the second cavity is inside to have the heat transfer passageway, the one end of heat transfer passageway with first cavity intercommunication, the other end runs through the second cavity, set up first catalyst layer in the first cavity, the heat transfer passageway intussuseption is filled with the second catalyst, enters into after the fluid in the first cavity with first catalyst layer reacts, follow the heat transfer passageway removes and reacts with the second catalyst, the second cavity intussuseption be filled with can with the heat transfer medium of heat transfer passageway carries out the heat exchange, in order to maintain the heat transfer passageway is in preset temperature range.

2. The broad temperature isothermal adiabatic reactor according to claim 1, wherein the housing further comprises a third cavity located on one side of the second cavity away from the first cavity, a third catalyst layer is disposed in the third cavity, and two ends of the heat exchange channel are communicated with the first cavity and the third cavity.

3. The broad temperature isothermal adiabatic reactor according to claim 2, wherein a first partition plate and a second partition plate are provided inside the housing, and the inside of the housing is partitioned into the first chamber, the second chamber, and the third chamber arranged in the same direction by the first partition plate and the second partition plate.

4. A wide temperature adaptability isothermal adiabatic reactor according to claim 3, wherein the partition is made of heat insulation material.

5. The broad temperature adaptive isothermal adiabatic reactor according to any of claims 2-4, wherein an outlet pipe is disposed on the third cavity, a gas collector is disposed in the third cavity, the gas collector is covered on the periphery of the outlet pipe, and the third catalyst layer is located on a side of the gas collector away from the outlet pipe.

6. The broad temperature adaptive isothermal adiabatic reactor according to claim 5, wherein the gas collector has a conical shape.

7. The wide temperature band isothermal adiabatic reactor according to claim 5, wherein the outlet pipe is further connected with a return pipe, the return pipe being in communication with the first chamber, so that a portion of the fluid in the third chamber can flow back to the first chamber.

8. The wide temperature adaptability isothermal adiabatic reactor according to any of claims 1-4, wherein an air inlet pipe is arranged on the first cavity, and a gas distributor communicated with the air inlet pipe is arranged inside the first cavity.

9. The broad temperature isothermal adiabatic reactor according to claim 8, wherein the gas distributor is capable of overlying the first catalyst layer for limiting the first catalyst layer.

10. The wide temperature adaptability isothermal adiabatic reactor according to any of claims 1-4, wherein the heat exchange channels comprise a plurality of heat exchange tubes.