Catalytic oxidation system capable of recycling tail gas waste heat
By adding a second heat exchanger to the catalytic oxidation system, secondary steam heat exchange of exhaust gas is solved, environmental pollution and resource waste caused by high exhaust gas temperature are solved, and the reuse of exhaust gas heat and the reduction of production costs are achieved.
Patent Information
- Application Number
- CN202421814637.X
- Authority / Receiving Office
- CN · China
- Patent Type
- Utility models(China)
- Current Assignee / Owner
- Filing Date
- 2024-07-30
- Publication Date
- 2025-06-20
- Estimated Expiration
- 2034-07-30
AI Technical Summary
In existing production systems, the temperature of exhaust gas generated by the catalytic reactor is high, resulting in environmental pollution and underutilization of heat, resulting in waste of resources and increased production costs.
A second heat exchanger is added to the catalytic oxidation system to perform secondary steam heat exchange, reduce the temperature of the exhaust gas from 180 degrees Celsius to 120 degrees Celsius, and realize the reuse of the heat of the exhaust gas.
Through secondary steam heat exchange, the adverse effects on the environment can be reduced, the exhaust heat is reused, resources are saved, production costs are reduced, and production efficiency is improved.
Smart Images
Figure CN223005398U_ABST
Abstract
Description
Technical Field
[0001] The utility model belongs to the technical field of low-pressure steam production and processing, and particularly relates to a catalytic oxidation system capable of recovering waste heat of tail gas. Background Technique
[0002] Both phenol and acetone are important organic chemical materials. Phenol is generally widely used in industries such as medicine, organic synthesis, and construction for disinfection, synthetic fibers, plastics, etc. Acetone is mainly used as a chemical reagent and is used as a solvent in industries such as rubber, plastics, explosives, and painting. In actual production, the production process for producing phenol and acetone is the cumene process, and low-pressure steam is an important material for producing phenol and acetone by the cumene process.
[0003] In the currently commonly used production system, the catalytic reactor will produce tail gas during the production process. The temperature of these tail gases is generally relatively high. During the tail gas treatment process, the tail gas is generally passed through a heat exchanger once and then discharged through a chimney. In this way, on the one hand, the temperature of the tail gas can be reduced, and on the other hand, the heat of the tail gas can be used to heat the steam to increase the steam temperature. However, the temperature of the tail gas discharged to the chimney after passing through the heat exchanger can sometimes still be as high as 180 °C. On the one hand, this will have a certain adverse impact on the environment, and on the other hand, the heat of the tail gas is not fully utilized, resulting in a certain waste of resources and an increase in production costs. Content of the Utility Model
[0004] The purpose of the utility model is to provide a catalytic oxidation system capable of recovering waste heat of tail gas, aiming to solve the above technical problems. Through the setting of the second heat exchanger, the utility model can perform secondary steam heat exchange utilization on the tail gas, and can reduce the temperature of the tail gas from 180 °C to 120 °C. On the one hand, this reduces the adverse impact on the environment, and on the other hand, it can achieve the effect of recycling the tail gas, achieving the purpose of saving resources and reducing costs.
[0005] In order to achieve the above purpose, the utility model is realized through the following technical solutions:
[0006] A catalytic oxidation system with recoverable waste heat from tail gas, comprising a reactor, a first heat exchanger, a second heat exchanger and an electric heater. One input port of the first heat exchanger is connected to a phenol acetone unit through a first section of the main gas path, one output port of the first heat exchanger is connected to the input port of the electric heater through a second section of the main gas path, the output port of the electric heater is connected to the input port of the reactor through a third section of the main gas path, the output port of the reactor is connected to the other input port of the first heat exchanger through a fourth section of the main gas path, the other output port of the first heat exchanger is connected to one input port of the second heat exchanger through a fifth section of the main gas path, one output port of the second heat exchanger is connected to a first chimney through a sixth section of the main gas path, the other input port of the second heat exchanger is connected to a steam condensation device through a first section of the steam path, and the other output port of the second heat exchanger is connected to a low steam main pipe through a second section of the steam path.
[0007] Further, a flow meter, a cut-off valve, a pressure gauge and a thermometer are sequentially provided on the first section of the main gas path from the phenol acetone unit to the first heat exchanger, and the flow meter, the cut-off valve, the pressure gauge and the thermometer can monitor the material transfer situation in the first section of the main gas path in real time.
[0008] Further, the first section of the main gas path is connected to a blower through an air path, the connection port of the air path is located between the thermometer and the first heat exchanger, and a pressure gauge and a cut-off valve are provided on the air path.
[0009] Further, a first branch is also provided on the first section of the main gas path. One end of the first branch is connected between the flow meter and the cut-off valve, and the other end of the first branch is connected to the first chimney. A cut-off valve is provided on the first branch. When the gas output from the phenol acetone unit needs to be directly discharged, the passage of the first section of the main gas path can be closed through the cut-off valve, and the first branch can be opened through the cut-off valve, so that the gas is discharged from the first chimney.
[0010] Further, a second branch is also provided on the first section of the main gas path. One end of the second branch is connected between the thermometer and the first heat exchanger, and the other end of the second branch is connected to the electric heater. A regulating valve is provided on the second branch. When the temperature of the gas discharged from the phenol acetone unit does not reach the required temperature of the first heat exchanger, the first section of the main gas path of the first heat exchanger can be closed, and the second branch can be opened through the regulating valve, so that the gas directly enters the electric heater from the second branch, and the gas temperature is regulated by the electric heater.
[0011] Further, a thermometer is provided on the second section of the main gas path, a pressure gauge is provided on the third section of the main gas path, a thermometer and an oxygen analyzer are provided on the fourth section of the main gas path, and a thermometer is provided on the sixth section of the main gas path.
[0012] Further, flow meters are provided on both the first section and the second section of the steam path.
[0013] Further, one outlet of the second heat exchanger is connected to the second chimney through a third branch, and one outlet of the second heat exchanger is connected to a trench through a fourth branch. A control valve is provided on the third branch. When the sixth section of the main gas path cannot exhaust gas to the first chimney normally, the cut-off valve on the third branch is closed, and the tail gas is discharged through the third branch by the second chimney.
[0014] Further, a differential pressure gauge is provided between the upper end and the lower end of the reactor, a thermometer is provided on the side of the reactor, a thermometer is provided on the electric heater, and a pressure gauge and a liquid level gauge are provided on the second heat exchanger.
[0015] The present utility model relates to a catalytic oxidation system with recoverable tail gas waste heat, and has the following beneficial effects:
[0016] 1. For the catalytic oxidation system with recoverable tail gas waste heat of the present utility model, by adding a second heat exchanger, the tail gas is subjected to secondary steam heat exchange, and the temperature of the tail gas can be reduced from 180 °C to 120 °C. On the one hand, this can reduce the adverse impact on the environment, and on the other hand, the heat in the tail gas can be reused, realizing the function of recycling and reusing the tail gas, and achieving the purpose of saving resources and reducing costs;
[0017] 2. For the catalytic oxidation system with recoverable tail gas waste heat of the present utility model, while using the second heat exchanger for steam heat exchange, the temperature of the low-pressure steam can be changed to make the produced low-pressure steam meet the requirements of subsequent production and processing, and it can also be continuously transported to the production system of phenol and acetone for further processing and utilization. In this way, the economic effect of the production line is greatly increased, which helps to reduce costs and increase efficiency and improve production capacity. Description of the Drawings
[0018] Figure 1 It is a schematic diagram of the overall structure of a catalytic oxidation system with recoverable tail gas waste heat of the present utility model;
[0019] Figure 2 It is a schematic diagram of the structure of a partial system in a catalytic oxidation system with recoverable tail gas waste heat of the present utility model;
[0020] Figure 3 It is a schematic diagram of the structure of a partial system in a catalytic oxidation system with recoverable tail gas waste heat of the present utility model. Detailed Embodiment
[0021] In order to enable those skilled in the art to better understand the technical solutions of the present utility model, the products of the present utility model will be further described in detail below in conjunction with embodiments and drawings.
[0022] It should be noted that when an element is referred to as "fixed to" another element, it can be directly on the other element or there may also be an intermediate element; when an element is considered to be "connected" to another element, it can be directly connected to the other element or there may be an intermediate element at the same time. The terms "vertical", "horizontal", "left", "right" and similar expressions used herein are only for illustrative purposes and do not represent the only implementation.
[0023] Unless otherwise defined, all technical and scientific terms used herein have the same meaning as commonly understood by those skilled in the technical field to which this utility model belongs. The terms used herein in the specification of this utility model are only for the purpose of describing specific embodiments and are not intended to limit this utility model. The term "and / or" used herein includes any and all combinations of one or more of the related listed items.
[0024] As Figure 1 、 Figure 2 and Figure 3 shown, a catalytic oxidation system with recoverable tail gas waste heat includes a reactor 2, a first heat exchanger 4, a second heat exchanger 7 and an electric heater 1. One input port of the first heat exchanger 4 is connected to a phenol acetone unit 19 through a first section of the main gas path 101, and one output port of the first heat exchanger 4 is connected to the input port of the electric heater 1 through a second section of the main gas path 102. The output port of the electric heater 1 is connected to the input port of the reactor 2 through a third section of the main gas path 103. The output port of the reactor 2 is connected to the other input port of the first heat exchanger 4 through a fourth section of the main gas path 104. The other output port of the first heat exchanger is connected to one input port of the second heat exchanger 7 through a fifth section of the main gas path 105. One output port of the second heat exchanger 7 is connected to a first chimney 5 through a sixth section of the main gas path 106. The other input port of the second heat exchanger 7 is connected to a steam condensation device 8 through a first section of the steam path 301. The other output port of the second heat exchanger 7 is connected to a low steam main pipe 9 through a second section of the steam path 302.
[0025] As Figure 1 、 Figure 2 and Figure 3 shown, a flow meter 11, a cut-off valve 16, a pressure gauge 15 and a thermometer 12 are successively arranged on the first section of the main gas path 101 from the phenol acetone unit 19 to the first heat exchanger 4. The flow meter 11, the cut-off valve 16, the pressure gauge 15 and the thermometer 12 can monitor the tail gas transfer situation in the first section of the main gas path 101 in real time.
[0026] As Figure 1 、 Figure 2 and Figure 3As shown, the first section 101 of the main gas path is connected to the fan 17 through the air path 401. The connection interface of the air path 401 is located between the thermometer 12 and the first heat exchanger 4. A pressure gauge 15 and a cut-off valve 16 are provided on the air path 401.
[0027] As Figure 1 and Figure 2 shown, a first branch 201 is also provided on the first section 101 of the main gas path. One end of the first branch 201 is connected between the flow meter 11 and the cut-off valve 16, and the other end of the first branch 201 is connected to the first chimney 5. A cut-off valve 16 is provided on the first branch 201. When the gas output by the phenol acetone unit 19 needs to be directly discharged, the passage of the first section 101 of the main gas path can be closed through the cut-off valve 16, and the first branch 201 can be opened through the cut-off valve 16, so that the gas is discharged from the first chimney 5.
[0028] As Figure 1 and Figure 2 shown, a second branch 202 is also provided on the first section 101 of the main gas path. One end of the second branch 202 is connected between the thermometer 12 and the first heat exchanger 4, and the other end of the second branch 202 is connected to the electric heater 1. A regulating valve 18 is provided on the second branch 202. When the temperature of the gas discharged from the phenol acetone unit does not reach the required temperature of the first heat exchanger 4, the first section 101 of the main gas path of the first heat exchanger 4 can be closed, and the second branch 202 can be opened through the regulating valve 18, so that the gas directly enters the electric heater 1 from the second branch 202, and the gas temperature is regulated by the electric heater 1.
[0029] As Figure 1 , Figure 2 and Figure 3 shown, a thermometer 12 is provided on the second section 102 of the main gas path, a pressure gauge 15 is provided on the third section 103 of the main gas path, a thermometer 12 and an oxygen analyzer 3 are provided on the fourth section 104 of the main gas path. The oxygen analyzer 3 is used to detect the oxygen content in the fourth section 104 of the main gas path. A thermometer 12 is provided on the sixth section 106 of the main gas path. Flow meters 11 are provided on both the first section 301 and the second section 302 of the steam path.
[0030] As Figure 1 , Figure 2 and Figure 3 shown, one output port of the second heat exchanger 7 is connected to the second chimney 6 through the third branch 203, and one output port of the second heat exchanger 7 is connected to the trench 10 through the fourth branch 204. A control valve is provided on the third branch 203. When the sixth section 106 of the main gas path cannot exhaust gas to the first chimney 5 normally, the cut-off valve 16 on the third branch 203 is opened, and the tail gas is discharged from the second chimney 6 through the third branch 203.
[0031] AsFigure 1 , Figure 2 and Figure 3 As shown in Figure 1 , Figure 2 and Figure 3 , a differential pressure gauge 14 is provided between the upper and lower ends of the reactor 2, a thermometer 12 is provided on the side of the reactor 2, a thermometer 12 is provided on the electric heater 1, and a pressure gauge 15 and a liquid level gauge 13 are provided on the second heat exchanger 7.
[0032] It should be noted that in this embodiment, the phenol acetone unit 19 generates tail gas during the production process. The tail gas is transported to the first heat exchanger 4 through the first section 101 of the main gas path. The transportation condition can be detected in real time by the thermometer 12, pressure gauge 15 and flowmeter 11 on the first section 101 of the main gas path. After the tail gas is heat-exchanged in the first heat exchanger 4, it is then transferred to the electric heater 1 through the second section 102 of the main gas path. The tail gas heated by the electric heater 1 then reaches the reactor 2 through the third section 103 of the main gas path. The tail gas after the reaction passes through the fourth section 104 of the main gas path to reach the first heat exchanger 4. The arriving tail gas is low-temperature tail gas and can be heat-exchanged. The heat-exchanged tail gas is then transferred to the second heat exchanger 7 through the fifth section 105 of the main gas path. Finally, the tail gas after the secondary heat exchange reaches the first chimney 5 through the sixth section 106 of the main gas path for discharge; when the tail gas produced from the phenol acetone unit 19 needs to be directly discharged, the cut-off valve 16 on the first section 101 of the main gas path is opened, and the cut-off valve 16 on the first branch 201 is closed, and the unnecessary tail gas is directly discharged from the first chimney 5; if the tail gas produced by the phenol acetone unit 19 does not meet the requirements of the first heat exchanger 4, the second branch 202 is directly opened through the regulating valve 18, so that the tail gas directly reaches the electric heater 1 through the second branch 202. After the electric heater 1 adjusts the temperature of the tail gas, it is discharged into the reactor 2 through the third section 103 of the main gas path; the heat exchange source required by the second heat exchanger 7 is provided by the low-pressure steam produced by the steam condensation device 8. The low-pressure steam enters the second heat exchanger 7 through the first section 301 of the steam path for heat exchange, and then the low-pressure steam is transferred to the low-pressure steam main pipe 9 through the second section 302 of the steam path for subsequent processing. Such a setting can not only provide a heat exchange source for the secondary heat exchange of the tail gas, but also enable the low-pressure steam to meet the temperature requirements of the subsequent processing. The produced waste water and waste residues are discharged to the trench 10 through the fourth branch 204 for treatment.
[0033] The above is only a preferred embodiment of the present invention, and it does not impose any form of limitation on the present invention; any ordinary technician in the industry can smoothly implement the present invention according to the illustrations in the specification and the above description; however, any minor changes, modifications and equivalent changes made by those skilled in the art within the scope of the technical solution of the present invention by using the technical content disclosed above are all equivalent embodiments of the present invention; at the same time, any equivalent changes, modifications and evolutions made to the above embodiments based on the essential technology of the present invention still belong to the technical solution of the present invention.
Claims
1. A catalytic oxidation system with recoverable tail gas waste heat, characterized in that: The invention comprises a reactor, a first heat exchanger, a second heat exchanger and an electric heater, wherein an input port of the first heat exchanger is connected to a phenol-acetone device through a first section of a main gas path, an output port of the first heat exchanger is connected to an input port of the electric heater through a second section of a main gas path, an output port of the electric heater is connected to an input port of the reactor through a third section of a main gas path, an output port of the reactor is connected to another input port of the first heat exchanger through a fourth section of a main gas path, another output port of the first gas exchanger is connected to an input port of the second heat exchanger through a fifth section of a main gas path, an output port of the second heat exchanger is connected to a first chimney through a sixth section of a main gas path, another input port of the second heat exchanger is connected to a steam condensing device through a first section of a steam path, and another output port of the second heat exchanger is connected to a low steam main pipe through a second section of a steam path.
2. The catalytic oxidation system with recoverable exhaust heat according to claim 1, characterized in that: A flow meter, a cut-off valve, a pressure gauge and a thermometer are sequentially arranged on a section of the main gas path from the phenol-acetone device to the first heat exchanger.
3. The catalytic oxidation system with recoverable exhaust heat according to claim 2, characterized in that: A section of the main gas path is connected to the fan through an air path, a phase interface of the air path is located between the thermometer and the first heat exchanger, and a pressure gauge and a cut-off valve are provided on the air path.
4. The catalytic oxidation system with recoverable exhaust heat according to claim 1, characterized in that: A first branch is also provided on the main gas path section, one end of the first branch is connected between the flow meter and the cut-off valve, the other end of the first branch is connected to the first chimney, and a cut-off valve is provided on the first branch.
5. The catalytic oxidation system with recoverable exhaust heat according to claim 1, characterized in that: A second branch is also provided on the main gas path section, one end of the second branch is connected between the thermometer and the first heat exchanger, the other end of the second branch is connected to the electric heater, and a regulating valve is provided on the second branch.
6. The catalytic oxidation system with recoverable exhaust heat according to claim 1, characterized in that: The second section of the main gas line is provided with a thermometer, the third section of the main gas line is provided with a pressure gauge, the fourth section of the main gas line is provided with a thermometer and an oxygen analyzer, and the sixth section of the main gas line is provided with a thermometer.
7. The catalytic oxidation system with recoverable exhaust heat according to claim 1, characterized in that: Flow meters are provided on the first section of the steam path and the second section of the steam path.
8. The catalytic oxidation system with recoverable exhaust heat according to claim 1, characterized in that: One output port of the second heat exchanger is connected to the second chimney through a third branch, and one output port of the second heat exchanger is connected to the ditch through a fourth branch. A control valve is arranged on the third branch.
9. The catalytic oxidation system with recoverable exhaust heat according to claim 1, characterized in that: A differential pressure gauge is provided between the upper end and the lower end of the reactor, a thermometer is provided on the side of the reactor, a thermometer is provided on the electric heater, and a pressure gauge and a liquid level gauge are provided on the second heat exchanger.