CN217418431U - Wet-type oxidation heat exchange network system - Google Patents
Wet-type oxidation heat exchange network system Download PDFInfo
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- CN217418431U CN217418431U CN202221363455.6U CN202221363455U CN217418431U CN 217418431 U CN217418431 U CN 217418431U CN 202221363455 U CN202221363455 U CN 202221363455U CN 217418431 U CN217418431 U CN 217418431U
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- 238000007254 oxidation reaction Methods 0.000 title abstract description 8
- 230000003647 oxidation Effects 0.000 title abstract description 7
- 238000009279 wet oxidation reaction Methods 0.000 claims abstract description 29
- 239000007788 liquid Substances 0.000 claims description 45
- 239000000463 material Substances 0.000 claims description 9
- 238000006243 chemical reaction Methods 0.000 claims description 7
- 229920001296 polysiloxane Polymers 0.000 claims 1
- 239000002351 wastewater Substances 0.000 abstract description 25
- 238000005265 energy consumption Methods 0.000 abstract description 4
- 238000013461 design Methods 0.000 abstract description 3
- 238000005516 engineering process Methods 0.000 abstract description 3
- 238000012546 transfer Methods 0.000 abstract description 3
- 230000003139 buffering effect Effects 0.000 abstract description 2
- 238000001816 cooling Methods 0.000 abstract description 2
- 238000000034 method Methods 0.000 description 17
- 239000003921 oil Substances 0.000 description 14
- 230000001590 oxidative effect Effects 0.000 description 12
- 230000015556 catabolic process Effects 0.000 description 5
- 238000006731 degradation reaction Methods 0.000 description 5
- 239000012530 fluid Substances 0.000 description 4
- 239000007789 gas Substances 0.000 description 4
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 4
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 2
- XUIMIQQOPSSXEZ-UHFFFAOYSA-N Silicon Chemical compound [Si] XUIMIQQOPSSXEZ-UHFFFAOYSA-N 0.000 description 2
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 2
- 238000011161 development Methods 0.000 description 2
- 239000010842 industrial wastewater Substances 0.000 description 2
- 229910052760 oxygen Inorganic materials 0.000 description 2
- 239000001301 oxygen Substances 0.000 description 2
- 150000003839 salts Chemical class 0.000 description 2
- 239000010865 sewage Substances 0.000 description 2
- 229910052710 silicon Inorganic materials 0.000 description 2
- 239000010703 silicon Substances 0.000 description 2
- 229910002092 carbon dioxide Inorganic materials 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 230000002860 competitive effect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000003670 easy-to-clean Effects 0.000 description 1
- 230000005611 electricity Effects 0.000 description 1
- 238000004134 energy conservation Methods 0.000 description 1
- 238000007429 general method Methods 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 239000005416 organic matter Substances 0.000 description 1
- 239000007800 oxidant agent Substances 0.000 description 1
- 238000011112 process operation Methods 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 230000001988 toxicity Effects 0.000 description 1
- 231100000419 toxicity Toxicity 0.000 description 1
- 238000009423 ventilation Methods 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
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- Heat-Exchange Devices With Radiators And Conduit Assemblies (AREA)
Abstract
The utility model discloses a wet oxidation heat exchange network system, which comprises a front section heat exchanger, a WAO reactor (14) and a rear section heat exchanger which are connected in sequence; and the shell pass outlet of the rear-section heat exchanger is sequentially connected with the heater (9), the shell pass of the front-section heat exchanger, the cooler (11) and the shell pass inlet of the rear-section heat exchanger to form heat exchange medium circulation. Waste water is through the tube side in this system, and the problem of easily blockking up among the traditional wet-type oxidation treatment technology has been solved to low viscous conduction oil through the shell side, has designed multistage heat transfer device, has solved the high problem of traditional device energy consumption, can operate under the low pressure condition, has further improved the factor of safety of device, designs buffering and cooling device simultaneously, has promoted the stability of system.
Description
Technical Field
The utility model belongs to the technical field of high COD sewage treatment, specifically be a wet-type oxidation heat exchange network system.
Background
The rapid industrial development is accompanied by the problem of huge discharge of three wastes, and industrial wastewater generally has the characteristics of high organic matter concentration, high salt content, strong toxicity and the like, and has great harm to the environment, so that the treatment of the wastewater is urgent.
The wet oxidation technology is to put the material to be treated in a closed container and introduce air as oxidant under the condition of high temperature and high pressure to degrade the organic matters in the sewage. The development to date has been quite competitive in the market for the treatment of industrial waste water, but the current wet oxidation reactor is basically a single packed bubble column structure and has the following disadvantages: (1) the heat exchanger has low heat exchange efficiency, high energy consumption and large equipment investment; (2) the device has large ventilation volume, generally low oxidation efficiency, insufficient treatment and unstable operation system; (3) the device is inconvenient to clean and maintain, and if the salt concentration of the waste water is higher, the blockage is easily caused. In view of the above, it is desirable to design a new wet oxidation treatment system.
SUMMERY OF THE UTILITY MODEL
The utility model provides a wet oxidation heat exchange network system to easy jam, energy consumption height, the technological operation flow that traditional wet oxidation technique exists stable inadequately, operating pressure shortcoming such as too high.
In order to solve the above problem, the utility model discloses mainly realize through heat exchange network system, technical scheme is as follows:
a wet oxidation heat exchange network system comprises a front-stage heat exchanger, a WAO reactor 14 and a rear-stage heat exchanger which are connected in sequence; and the shell pass outlet of the rear-section heat exchanger is sequentially connected with the heater 9, the shell pass of the front-section heat exchanger, the cooler 11 and the shell pass inlet of the rear-section heat exchanger to form heat exchange medium circulation.
Further, the front-stage heat exchanger comprises a first heat exchanger 6 and a second heat exchanger 7 which are arranged in series according to the flowing direction of the reaction materials, and the shell side of the first heat exchanger 6 and the shell side of the second heat exchanger 7 are connected in series in the heat exchange medium circulation.
Further, the rear-stage heat exchanger comprises a third heat exchanger 13 and a fourth heat exchanger 12 which are arranged in series according to the flowing direction of the reaction materials, and the shell side of the third heat exchanger 13 and the shell side of the fourth heat exchanger 12 are connected in series in the heat exchange medium circulation.
Further, a gas-liquid mixer 3 is arranged in front of the inlet of the front-section heat exchanger. In the gas-liquid mixer, the concentration of high-pressure air and COD is 2-5 x 10 4 The mg/L waste water is mixed, so that oxygen in the air is fully contacted with the waste water, and a foundation is laid for further improving the subsequent degradation efficiency.
Further, the outlet of the rear-stage heat exchanger is connected with a gas-liquid separator 15.
Further, a liquid buffer tank 8 is arranged between the shell side of the front-stage heat exchanger and the cooler 11.
Further, a pump is arranged between the liquid buffer tank 8 and the cooler 11.
Further, the heater 9 is a steam generator.
Further, the heat exchange medium is heat conduction oil.
Furthermore, the heat conduction oil is organic silicon heat conduction oil.
The wet oxidation heat exchange network system can be operated by adopting a general method in the field, and can also adopt the following operation modes for improving the efficiency:
the method comprises the following steps of enabling pressurized air and wastewater to form a gas-liquid mixed liquid, enabling the gas-liquid mixed liquid to flow into a front-section heat exchanger, enabling the gas-liquid mixed liquid to be subjected to heat exchange and temperature rise through the front-section heat exchanger, enabling the gas-liquid mixed liquid to flow into a WAO reactor 14 after the temperature reaches 170-280 ℃ and enabling the gas-liquid mixed liquid to react to form an oxidation liquid;
the oxidizing solution is discharged after being subjected to heat exchange and temperature reduction by a rear-section heat exchanger to 40-60 ℃;
the heat exchange medium exchanges heat with the oxidizing liquid in the shell pass of the rear-section heat exchanger, flows into the shell pass of the front-section heat exchanger after the temperature is raised, exchanges heat with the gas-liquid mixed liquid, reduces the temperature and returns to the shell pass of the rear-section heat exchanger, when the temperature of the heat conduction medium is not sufficiently raised, the heat is supplemented by a heater in the heat exchange medium circulation, and when the temperature of the heat conduction medium is too high, the temperature is reduced by a cooler in the heat exchange medium circulation.
In the process, adopt heat exchange circulation system to replace traditional direct heat transfer process, improved heat exchange efficiency, the low energy-conservation that consumes.
In the wet oxidation process, waste water and air two-phase fluid are heated to enable organic matters to undergo oxidation reaction and further degrade, a large amount of energy needs to be provided in the process, but the traditional process has low heat exchange efficiency and is not stable and controllable enough in the process operation process; in addition, in the whole process, the device has higher cost and is not easy to clean and easy to block. The heat exchange network system of the utility model firstly effectively improves the heat exchange efficiency, the multi-stage heat exchange device is combined with the cooler and the steam generator, and the heat conduction oil circulates through the shell side, thereby increasing the heat exchange area, achieving the purpose of low consumption and energy saving, and simultaneously, the system is more stable and controllable; secondly, the whole process of the waste water is processed by a pipe pass, so that the problem of blockage is solved.
Preferably, in the wet oxidation heat exchange network system described above, the feed rate of the WAO reactor is 2 to 4 times the feed rate of the wastewater;
preferably, in the wet oxidation heat exchange network system, the temperature of the second heat exchanger is 180-290 ℃, and the temperature of the third heat exchanger is 30-50 ℃;
waste water is through the tube side in this system, and the problem of easily blockking up among the traditional wet-type oxidation treatment technology has been solved to low viscous conduction oil through the shell side, has designed multistage heat transfer device, has solved the high problem of traditional device energy consumption, can operate under the low pressure condition, has further improved the factor of safety of device, designs buffering and cooling device simultaneously, has promoted the stability of system.
Drawings
Fig. 1 is a schematic structural diagram of a wet oxidation heat exchange network system according to the present invention.
Where 1 is pressurized air, 2 is wastewater, 3 is a business mixer, 4 is water, 5 is steam, 6 is a first heat exchanger, 7 is a second heat exchanger, 8 is a liquid buffer tank, 9 is a steam generator, 10 is a pump, 11 is a cooler, 12 is a fourth heat exchanger, 13 is a third heat exchanger, 14 is a WAO reactor, 15 is a gas-liquid separator, 16 is tail gas, and 17 is effluent.
Detailed Description
The wet oxidation heat exchange network system is described in further detail below with reference to fig. 1 and the following detailed description:
example 1
A wet oxidation heat exchange network system comprises a front-stage heat exchanger, a WAO reactor 14 and a rear-stage heat exchanger which are connected in sequence; and the shell pass outlet of the rear-section heat exchanger is sequentially connected with the heater 9, the shell pass of the front-section heat exchanger, the cooler 11 and the shell pass inlet of the rear-section heat exchanger to form heat exchange medium circulation.
The front-stage heat exchanger comprises a first heat exchanger 6 and a second heat exchanger 7 which are arranged in series according to the flowing direction of reaction materials, and the shell side of the first heat exchanger 6 and the shell side of the second heat exchanger 7 are connected in series in the heat exchange medium circulation.
The rear-stage heat exchanger comprises a third heat exchanger 13 and a fourth heat exchanger 12 which are arranged in series according to the flowing direction of reaction materials, wherein the shell side of the third heat exchanger 13 and the shell side of the fourth heat exchanger 12 are connected in series in the heat exchange medium circulation.
And a gas-liquid mixer 3 is also arranged in front of the inlet of the front-section heat exchanger. In the gas-liquid mixer, the concentration of high-pressure air and COD is 2-5 x 10 4 The mg/L waste water is mixed, so that oxygen in the air is fully contacted with the waste water, and a foundation is laid for further improving the subsequent degradation efficiency.
The outlet of the rear-section heat exchanger is connected with a gas-liquid separator 15.
And a liquid buffer tank 8 is also arranged between the shell side of the front-section heat exchanger and the cooler 11.
A pump is also arranged between the liquid buffer tank 8 and the cooler 11.
The heater 9 is a steam generator.
The heat exchange medium is heat conduction oil.
The heat conduction oil is organic silicon heat conduction oil.
The water phase in the process passes through a tube pass, and the steps are as follows:
s1: gas-liquid mixing: pressurizing air to 5.5Mpa, introducing pressurized air 1 into the waste water 2 in a gas-liquid mixer 3Line mixing, the COD of the waste water is 2.5 x 10 4 mg/L, fully mixing gas and liquid to form two-phase fluid;
s2: heat exchange-temperature rise: then the two-phase fluid enters a first heat exchanger 6 through a tube pass, heat conducting oil is loaded in a shell pass of the first heat exchanger 6, a liquid outlet of the shell pass is connected with a liquid buffer tank 8, an inlet of the shell pass is connected with a second heat exchanger 7, and the temperature of the two-phase fluid is increased through the first heat exchanger 6 and the second heat exchanger 7 and enters a WAO reactor 14;
s3: wet oxidation reaction: the organic wastewater is oxidized in the WAO reactor 14 to generate water and carbon dioxide, and after the reaction is finished, an oxidizing solution is generated, the temperature reaches 230 ℃, and then the organic wastewater is discharged to the third heat exchanger 13;
s4: heat exchange-temperature reduction: the oxidizing liquid enters a third heat exchanger 13 through a pipe pass, the shell pass of the third heat exchanger 13 is respectively connected with the shell pass of a fourth heat exchanger 12 and a steam generator 9, the oxidizing liquid exchanges heat with heat conduction oil in the shell pass through the third heat exchanger 13 and the fourth heat exchanger 12, and the temperature is kept at 40 ℃ after the heat exchange is finished;
s5: gas-liquid separation: then the oxidizing liquid enters a gas-liquid separator 15, and gas in the liquid is discharged through formed tail gas 16 and effluent 17;
s6: a heat exchange circulation system: when the temperature of the first heat exchanger 6 and the second heat exchanger 7 is too low, the heat conducting oil in the third heat exchanger 13 is heated by the steam generator 9 and then sequentially circulates to the second heat exchanger 7 and the first heat exchanger 6; when the temperature of the heat conducting oil in the fourth heat exchanger 12 is too high, the heat conducting oil passes through the pump 10 and the cooler 11 to be cooled and circulated to the fourth heat exchanger 12.
The feeding amount of the WAO reactor pair is 2.5 times of the feeding amount of the wastewater;
the temperature of the oxidizing liquid output by the WAO reactor is 230 ℃, and the temperature of the oxidizing liquid output by the third heat exchanger is 40 ℃;
the temperature of the second heat exchanger is 240 ℃, and the temperature of the third heat exchanger is 39 ℃;
example 2
The same heat exchange network system as in example 1 was used, and the water phase in the process was passed through the tube pass, which differs from example 1 only in that:
s1, pressurizing the air to 9Mpa, and making COD of the waste water be 4 x 10 4 mg/L。
The temperature of the oxidizing solution in S3 was 270 ℃.
The temperature of the heat conducting oil in the S4 is kept at 50 ℃ after heat exchange.
The feeding amount of the WAO reactor pair is 2 times of the feeding amount of the wastewater;
the temperature of the oxidizing liquid output by the WAO reactor is 270 ℃, and the temperature of the oxidizing liquid output by the heat exchanger 4 is 50 ℃;
the temperature of the second heat exchanger 7 is 280 ℃, and the temperature of the third heat exchanger 13 is 45 ℃;
example 3
Taking a factory wastewater sample, wherein the COD content in the wastewater is 2 x 10 4 mg/L, density 1100kg/m 3 The wastewater temperature is 40 ℃, and the daily discharge amount of the wastewater is 15m 3 H is used as the reference value. The conventional wet oxidation process and the process of embodiment 1 of the present invention are used to treat the wastewater respectively, and the degradation rate is compared, wherein embodiment 1 of the present invention uses a wet oxidation heat exchange network system, and the conventional wet oxidation process only uses a conventional heat exchange manner, and the two processes are compared: the degradation rate of a wet oxidation heat exchange network system reaches 96% when 40min, and the operation cost (the energy and material consumption is 45 yuan/ton) is low; the degradation rate of the wet oxidation process is 90% at 40min, and the running cost (the energy and material consumption is 85 yuan/ton, and is related to the electricity price) is low.
In summary, the above-mentioned embodiments are only preferred embodiments of the present invention, and all equivalent changes and modifications made within the scope of the claims of the present invention should be covered by the present invention.
Claims (10)
1. A wet oxidation heat exchange network system is characterized by comprising a front-stage heat exchanger, a WAO reactor (14) and a rear-stage heat exchanger which are sequentially connected; and the shell pass outlet of the rear-section heat exchanger is sequentially connected with the heater (9), the shell pass of the front-section heat exchanger, the cooler (11) and the shell pass inlet of the rear-section heat exchanger to form heat exchange medium circulation.
2. The wet oxidation heat exchange network system according to claim 1, wherein the front-end heat exchanger comprises a first heat exchanger (6) and a second heat exchanger (7) arranged in series in the order of the flow direction of the reaction materials, and the shell side of the first heat exchanger (6) and the shell side of the second heat exchanger (7) are connected in series in the heat exchange medium circulation.
3. The wet oxidation heat exchange network system according to claim 1, wherein the back-end heat exchanger comprises a third heat exchanger (13) and a fourth heat exchanger (12) arranged in series in the order of the flow direction of the reaction materials, and the shell side of the third heat exchanger (13) and the shell side of the fourth heat exchanger (12) are connected in series in the heat exchange medium cycle.
4. The wet oxidation heat exchange network system according to claim 1, wherein a gas-liquid mixer (3) is further provided in front of the inlet of the front-stage heat exchanger.
5. The wet oxidation heat exchange network system according to claim 1, wherein the outlet of the back stage heat exchanger is connected to a gas-liquid separator (15).
6. The wet oxidation heat exchange network system according to claim 1, wherein a liquid surge tank (8) is further provided between the shell side of the front-end heat exchanger and the cooler (11).
7. The system according to claim 6, characterized in that a pump is further provided between the liquid buffer tank (8) and the cooler (11).
8. The wet oxidation heat exchange network system according to claim 1, wherein the heater (9) is a steam generator.
9. The wet oxidation heat exchange network system of claim 1, wherein the heat exchange medium is a thermal oil.
10. The system for wet oxidation heat exchange according to claim 9, wherein the thermal oil is a silicone thermal oil.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202221363455.6U CN217418431U (en) | 2022-06-02 | 2022-06-02 | Wet-type oxidation heat exchange network system |
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| CN202221363455.6U CN217418431U (en) | 2022-06-02 | 2022-06-02 | Wet-type oxidation heat exchange network system |
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| CN217418431U true CN217418431U (en) | 2022-09-13 |
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| CN202221363455.6U Active CN217418431U (en) | 2022-06-02 | 2022-06-02 | Wet-type oxidation heat exchange network system |
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- 2022-06-02 CN CN202221363455.6U patent/CN217418431U/en active Active
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