CN214468739U - SCR (Selective catalytic reduction) comprehensive reactor - Google Patents
SCR (Selective catalytic reduction) comprehensive reactor Download PDFInfo
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- CN214468739U CN214468739U CN202022471939.XU CN202022471939U CN214468739U CN 214468739 U CN214468739 U CN 214468739U CN 202022471939 U CN202022471939 U CN 202022471939U CN 214468739 U CN214468739 U CN 214468739U
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Abstract
The utility model relates to a SCR integrated reactor, including SCR reaction section and heat transfer section, wherein, the exit linkage of SCR reaction section the tube side entry of heat transfer section, the tube side export of heat exchange tube is then connected and is provided with the exhanst gas outlet pipeline, the shell side entry linkage flue gas inlet pipeline of heat transfer section, the shell side export of heat transfer section is then connected the raw materials entry of SCR reaction section. Compared with the prior art, the utility model discloses can reduce the energy resource consumption of reactor for system's heat energy can obtain recycle, simultaneously, saves the cost, simplifies and sets up the structure etc..
Description
Technical Field
The utility model belongs to the technical field of flue gas denitration treatment, a SCR synthesizes reactor is related to.
Background
In recent years, the emission of pollutants, nitrogen oxides, has been rapidly increased under the drive of rapid economic development. The ecological environment is seriously polluted, and the reduction and control of the emission of nitrogen oxides in thermal power plants and waste incineration power plants are urgent. The method for reducing the emission of nitrogen oxides mainly comprises 2 methods of combustion control and flue gas denitration. The flue gas denitration method includes a non-selective catalytic reduction method (SNCR), a selective catalytic reduction method (SCR), an adsorption method, a plasma method and the like. The Selective Catalytic Reduction (SCR) flue gas denitration technology is applied to the denitration of the flue gas of the incinerator. Due to the characteristics of mature denitration technology, high-efficiency denitration efficiency and the like, the denitration catalyst is widely applied in the world and is known as the mainstream technology of flue gas denitration.
But because the denitration system has short domestic application time and little accumulated experience, a system operation standard which can be popularized is not formed yet. The mainstream flue gas denitration system at present comprises the processes of deacidification, dust removal, flue gas preheating (GGH), Selective Catalytic Reduction (SCR) reaction and the like, so that the discharged flue gas meets the emission standard, and the pollution to the atmosphere is reduced, wherein the Selective Catalytic Reduction (SCR) is the core unit of the denitration system.
In the traditional flue gas denitration process flow, all monomer devices are mutually independent, and pipelines are used as media for linking up the whole process. Each single device is fixedly supported by the frame structure. The flue gas after deacidification and dust removal is heated by an air preheater and enters an SCR reactor for reaction after reaching the catalytic reaction temperature, and the flue gas after denitration is directly discharged to the atmosphere through a chimney. The flue gas denitration system has a huge overall structure, a frame type supporting structure of the equipment has a large occupied area, is complex to manufacture and large in material loss, structurally influences the pipeline arrangement of the system, and increases the pipeline loss. In order to ensure the catalytic reaction efficiency, the flue gas needs to be heated to the optimal action temperature of the catalyst, the energy consumption of the flue gas preheater is large, the high-temperature gas after the temperature rise through the reaction of the SCR reactor is directly discharged into a chimney, and the heat energy loss is serious.
SUMMERY OF THE UTILITY MODEL
The utility model aims at providing a SCR synthesizes reactor to reduce the energy resource consumption of reactor, make system's heat energy can obtain recycle, save the cost.
The purpose of the utility model can be realized through the following technical scheme:
the SCR comprehensive reactor comprises an SCR reaction section and a heat exchange section, wherein an outlet of the SCR reaction section is connected with a tube side inlet of the heat exchange section, a tube side outlet of a heat exchange tube is connected with a flue gas outlet pipeline, a shell side inlet of the heat exchange section is connected with a flue gas inlet pipeline, and a shell side outlet of the heat exchange section is connected with a raw material inlet of the SCR reaction section.
Furthermore, a shell side outlet of the heat exchange section is connected with a raw material inlet of the SCR reaction section through a flue gas circulation pipeline.
Furthermore, the heat exchange section comprises a heat exchange shell fixedly connected with the SCR reaction section and a heat exchange tube bundle arranged in the heat exchange shell, and two ends of the heat exchange tube bundle are respectively connected with an outlet of the SCR reaction section and a flue gas outlet pipeline.
Further, the heat exchange tube bundle is arranged along the longitudinal direction.
Furthermore, a plurality of baffle plates perpendicular to the heat exchange tube bundle are arranged in the heat exchange shell, and the baffle plates are arranged in a staggered mode along the direction of the heat exchange tube bundle.
Preferably, one side of the baffle plate is hermetically connected with the inner wall of the heat exchange shell, the other side of the baffle plate is spaced from the inner wall of the heat exchange shell, and the baffle plate is fixedly connected with part of the heat exchange tube bundle. More preferably, the area of the baffle plate is 2/3-3/4 of the cross section area of the heat exchange shell.
Furthermore, heat exchange fins are arranged on the heat exchange tube bundle.
Furthermore, the bottom of the heat exchange section is also provided with a skirt type support.
Furthermore, a shell pass inlet of the heat exchange section is positioned below the heat exchange section, and a shell pass outlet of the heat exchanger is positioned above the heat exchange section, so that fluid in the shell pass of the heat exchange section is in countercurrent contact with fluid in the tube pass of the heat exchange section.
Compared with the prior art, the utility model has the advantages of it is following:
(1) energy conservation: a reaction/heat exchange integrated structure is adopted, a flue gas heat exchange circulating system is arranged, the energy consumption of the flue gas preheater is reduced, and the heat energy of the system is recycled.
(2) Saving materials: the reaction/heat exchange integrated structure reduces flue pipes, is supported by skirt supports, cancels an equipment frame structure and saves materials.
(3) The space is saved: the reaction/heat exchange integrated structure and the skirt type support are more beneficial to the arrangement of equipment pipelines, reduce the requirement on equipment arrangement and save space.
Drawings
Fig. 1 is a schematic structural view of the present invention;
the notation in the figure is:
1-SCR reaction section, 2-heat exchange section, 21-heat exchange shell, 22-heat exchange tube bundle, 23-baffle plate, 3-flue gas circulation pipeline, 4-flue gas outlet pipeline, 5-flue gas inlet pipeline and 6-skirt type support.
Detailed Description
The present invention will be described in detail below with reference to the accompanying drawings and specific embodiments. The embodiment is implemented on the premise of the technical solution of the present invention, and a detailed implementation manner and a specific operation process are given, but the scope of the present invention is not limited to the following embodiments.
In the following embodiments, unless otherwise specified, all the functional components or structures are conventional components or structures used in the art to realize the corresponding functions.
The utility model provides a reactor is synthesized to SCR, its structure is referred to as and is shown in figure 1, including SCR reaction section 1 and heat transfer section 2, wherein, SCR reaction section 1's exit linkage the tube side entry of heat transfer section 2, the tube side export of heat exchange tube is then connected and is provided with exhanst gas outlet pipeline 4, heat transfer section 2's shell side entry linkage flue gas inlet pipeline 5, heat transfer section 2's shell side export is then connected SCR reaction section 1's raw materials entry, like this, the flue gas after the reduction reaction through adopting the high temperature preheats the flue gas before the reaction, can effectually preheat the flue gas before the reaction to guarantee the active degree of the catalyst in SCR reaction section 1, also make the heat energy of system obtain effectual recycle, reduced the energy resource consumption who additionally sets up flue gas preheater. In addition, a heat exchange section 2 is directly arranged below the SCR reaction section 1, so that the SCR reaction section and the heat exchange section form an integrated structure, the pipe loss of a flue can be reduced, and materials are saved.
In a specific embodiment of the present invention, please refer to fig. 1 again, the shell side outlet of the heat exchange section 2 is connected to the raw material inlet of the SCR reaction section 1 through a flue gas circulation pipeline 3.
In a specific embodiment of the present invention, please refer to fig. 1 again, the heat exchange section 2 includes a fixed connection heat exchange shell 21 of the SCR reaction section 1 and a heat exchange tube bundle 22 arranged in the heat exchange shell 21, two ends of the heat exchange tube bundle 22 are connected to the outlet and the flue gas outlet pipeline 4 of the SCR reaction section 1 respectively. In a more specific embodiment, the heat exchange tube bundle 22 is arranged in a longitudinal direction. Whole heat transfer section 2 is vertical arrangement, can improve inside heat transfer fluid medium's mobility, and then improves the heat transfer effect.
In a more specific embodiment, please refer to fig. 1 again, a plurality of baffle plates 23 perpendicular to the heat exchange tube bundle 22 are further disposed in the heat exchange shell 21, the baffle plates 23 are staggered along the heat exchange tube bundle 22, and the arrangement of the baffle plates 23 can make the flue gas before reaction in the shell pass in a turbulent state, thereby further improving the heat exchange effect. In a further specific embodiment, please refer to fig. 1 again, one side of the baffle plate 23 is hermetically connected to the inner wall of the heat exchange shell 21, the other side of the baffle plate is spaced from the inner wall of the heat exchange shell 21, and the baffle plate 23 is further fixedly connected to a part of the heat exchange tube bundle 22, so that the occurrence of flue gas turbulence in the shell pass is ensured, and the purpose of supporting the heat exchange tube bundle 22 is also achieved. More preferably, the area of the baffle plate 23 is 2/3-3/4 of the cross section area of the heat exchange shell 21, so that the flue gas turbulence effect in the shell side can reach a better heat exchange state, and the flow of the flue gas in the shell side cannot be influenced.
In a more specific embodiment, the heat exchange tube bundle 22 is further provided with heat exchange fins.
In a specific embodiment of the present invention, please refer to fig. 1 again, the bottom of the heat exchange section 2 is further provided with a skirt type support 6, which is more beneficial to the arrangement of the equipment pipeline, reduces the requirement of the equipment arrangement, and saves space.
The utility model discloses an among the specific embodiment, please refer to again that fig. 1 is shown, the shell side entry of heat transfer section 2 is located the below position of heat transfer section 2, and the shell side export of heat exchanger is located the top position of heat transfer section 2 for fluid in the 2 shell sides of heat transfer section is the contact against the current rather than the fluid in the tube side, and the shell side adopts the form of arranging of contact against the current with the tube side, has also improved the heat transfer effect of the flue gas after flue gas before the reaction and the reduction reaction, improves energy utilization efficiency.
The above embodiments can be implemented individually, in any combination of two or more.
The above embodiments will be described in more detail with reference to specific examples.
Example 1:
the embodiment provides a reactor is synthesized to SCR, its structure is shown in figure 1, including SCR reaction section 1 and heat-transfer section 2, wherein, the tube side entry of the exit linkage heat-transfer section 2 of SCR reaction section 1, the tube side export of heat exchange tube is then connected and is provided with exhanst gas outlet pipeline 4, the shell side entry linkage flue gas inlet pipeline 5 of heat-transfer section 2, the raw materials entry of SCR reaction section 1 is then connected to the shell side export of heat-transfer section 2, thus, flue gas before the reduction reaction through adopting the high temperature preheats the reaction, can effectually preheat the flue gas before the reaction, thereby guarantee the active degree of the catalyst in SCR reaction section 1, also make the heat energy of system obtain effectual recycle, the energy resource consumption who additionally sets up flue gas preheater has been reduced. In addition, a heat exchange section 2 is directly arranged below the SCR reaction section 1, so that the SCR reaction section and the heat exchange section form an integrated structure, the pipe loss of a flue can be reduced, and materials are saved.
Referring to fig. 1 again, the shell side outlet of the heat exchange section 2 is connected to the raw material inlet of the SCR reaction section 1 through a flue gas circulation pipe 3.
Referring to fig. 1 again, the heat exchange section 2 includes a heat exchange shell 21 fixedly connected to the SCR reaction section 1, and a heat exchange tube bundle 22 disposed in the heat exchange shell 21, and two ends of the heat exchange tube bundle 22 are respectively connected to the outlet of the SCR reaction section 1 and the flue gas outlet pipe 4. In a more specific embodiment, heat exchange tube bundle 22 is arranged in a longitudinal direction. Whole heat transfer section 2 is vertical arrangement, can improve inside heat transfer fluid medium's mobility, and then improves the heat transfer effect.
Referring to fig. 1 again, a plurality of baffle plates 23 perpendicular to the heat exchange tube bundle 22 are further disposed in the heat exchange shell 21, the baffle plates 23 are staggered along the heat exchange tube bundle 22, and the arrangement of the baffle plates 23 can make the flue gas before reaction in the shell pass in a turbulent state, thereby further improving the heat exchange effect. In a further specific embodiment, please refer to fig. 1 again, one side of the baffle plate 23 is hermetically connected to the inner wall of the heat exchange shell 21, the other side of the baffle plate is spaced from the inner wall of the heat exchange shell 21, and the baffle plate 23 is further fixedly connected to a part of the heat exchange tube bundle 22, so that the occurrence of the flue gas turbulence in the shell pass is ensured, and the purpose of supporting the heat exchange tube bundle 22 is also achieved. More preferably, the area of the baffle plate 23 is between 2/3 and 3/4 of the cross-sectional area of the heat exchange shell 21, so that the flue gas turbulence effect in the shell side can reach a better heat exchange state, and the flow of the flue gas in the shell side cannot be influenced. Heat exchange fins are also disposed on the heat exchange tube bundle 22.
Referring to fig. 1 again, the bottom of the heat exchange section 2 is further provided with a skirt-type support 6, which is more beneficial to the arrangement of the equipment pipelines, reduces the requirement of the equipment arrangement, and saves the space.
Referring to fig. 1 again, the shell-side inlet of the heat exchange section 2 is located below the heat exchange section 2, and the shell-side outlet of the heat exchanger is located above the heat exchange section 2, so that the fluid in the shell-side of the heat exchange section 2 is in countercurrent contact with the fluid in the tube-side thereof, and the shell-side and the tube-side are in countercurrent contact, thereby improving the heat exchange effect between the flue gas before reaction and the flue gas after reduction reaction and improving the energy utilization efficiency.
In this embodiment, SCR reaction section 1 is roughly the same with the structure setting of conventional SCR reactor, reacts through flange sealing connection between section 1 and the heat transfer section 2 in the SCR, simultaneously, guarantees that only the tube side of heat transfer section 2 and the exit linkage of SCR reaction section 1, and simultaneously, the tube side lower extreme export of heat transfer section 2 is also concentrated and is connected external system or lug connection outside atmosphere through gas outlet pipeline 4. During specific work, low-temperature flue gas before reaction is sent into the shell side of the heat exchange section 2 and is in countercurrent contact heat exchange with high-temperature flue gas after reduction reaction discharged by the heat exchange tube bundle 22, the preheated flue gas before reaction is sent into the SCR reaction section 1 through the flue gas circulation pipeline 3 (a flue gas preheater can be arranged as required to ensure that the flue gas is preheated to a proper temperature range before being sent into the SCR reaction section 1), catalytic reduction reaction is carried out through the catalytic action of the catalyst in the SCR reaction section 1, high-temperature reduction reaction flue gas is generated, and the flue gas is discharged through the flue gas outlet pipeline 4 after heat is recovered in the tube side of the heat exchange section 2.
The embodiments described above are intended to facilitate the understanding and use of the invention by those skilled in the art. It will be readily apparent to those skilled in the art that various modifications to these embodiments may be made, and the generic principles described herein may be applied to other embodiments without the use of the inventive faculty. Therefore, the present invention is not limited to the above embodiments, and those skilled in the art should make improvements and modifications within the scope of the present invention according to the disclosure of the present invention.
Claims (10)
1. The SCR integrated reactor is characterized by comprising an SCR reaction section and a heat exchange section, wherein an outlet of the SCR reaction section is connected with a tube side inlet of the heat exchange section, a tube side outlet of the heat exchange section is connected with a flue gas outlet pipeline, a shell side inlet of the heat exchange section is connected with a flue gas inlet pipeline, and a shell side outlet of the heat exchange section is connected with a raw material inlet of the SCR reaction section.
2. The SCR integrated reactor of claim 1, wherein the shell side outlet of the heat exchange section is connected to the feedstock inlet of the SCR reaction section by a flue gas recirculation conduit.
3. The SCR integrated reactor according to claim 1, wherein the heat exchange section comprises a heat exchange shell fixedly connected with the SCR reaction section, and a heat exchange tube bundle arranged in the heat exchange shell, and two ends of the heat exchange tube bundle are respectively connected with an outlet of the SCR reaction section and a flue gas outlet pipeline.
4. An SCR integrated reactor as claimed in claim 3, wherein the heat exchanger tube bundle is arranged in a longitudinal direction.
5. The SCR integrated reactor of claim 3, wherein the heat exchange shell further comprises a plurality of baffles perpendicular to the heat exchange tube bundle, and the baffles are staggered along the heat exchange tube bundle.
6. The SCR integrated reactor of claim 5, wherein one side of the baffle plate is hermetically connected to the inner wall of the heat exchange shell, the other side of the baffle plate is spaced from the inner wall of the heat exchange shell, and the baffle plate is further fixedly connected to a portion of the heat exchange tube bundle.
7. The SCR integrated reactor of claim 6, wherein the area of the baffle is between 2/3 and 3/4 of the cross-sectional area of the heat exchange shell.
8. An SCR integrated reactor as claimed in claim 3, wherein the heat exchanger bundle is further provided with heat exchanger fins.
9. An SCR integrated reactor as claimed in claim 1, wherein the bottom of the heat exchange section is further provided with a skirt support.
10. The SCR integrated reactor of claim 1, wherein the shell-side inlet of the heat exchange section is located below the heat exchange section and the shell-side outlet of the heat exchanger is located above the heat exchange section such that fluid in the shell-side of the heat exchange section is in countercurrent contact with fluid in the tube-side of the heat exchange section.
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| Application Number | Priority Date | Filing Date | Title |
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| CN202022471939.XU CN214468739U (en) | 2020-10-31 | 2020-10-31 | SCR (Selective catalytic reduction) comprehensive reactor |
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| CN202022471939.XU CN214468739U (en) | 2020-10-31 | 2020-10-31 | SCR (Selective catalytic reduction) comprehensive reactor |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN112197287A (en) * | 2020-10-31 | 2021-01-08 | 上海建安化工设计有限公司 | SCR (Selective catalytic reduction) comprehensive reactor |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112197287A (en) * | 2020-10-31 | 2021-01-08 | 上海建安化工设计有限公司 | SCR (Selective catalytic reduction) comprehensive reactor |
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