CN213357201U

CN213357201U - Zero release processing system to volatile phenol in salt waste water

Info

Publication number: CN213357201U
Application number: CN202020705892.6U
Authority: CN
Inventors: 王力兴; 苏立辉; 顾法生; 王惠; 叶春
Original assignee: Jiangsu Shuizesen Environmental Treatment Co ltd
Current assignee: Jiangsu Shuizesen Environmental Treatment Co ltd
Priority date: 2020-04-30
Filing date: 2020-04-30
Publication date: 2021-06-04
Anticipated expiration: 2030-04-30

Abstract

The utility model discloses a zero release processing system to volatile phenol in containing salt waste water, preheat heat exchanger No. two material exports and supercritical reactor upper portion feed inlets intercommunication No. one, No. two pipelines and No. two supercritical reactor upper portion feed inlets intercommunication are passed through in the material export of strand flow heat exchanger, and strand flow heat exchanger medium export and supercritical reactor lower part feed inlet, No. two supercritical reactor lower part feed inlets all communicate. The utility model discloses well earlier with gas floating tank carry out the preliminary treatment, the preceding part of the phenol that volatilizees in with the waste water after the preliminary treatment is got rid of, utilizes multi-effect evaporator will not have phenol waste water and contain phenol waste water branch matter oxidation treatment, makes the oxidation of containing phenol water at the system's inner loop, and no outer row. The trace discharge of the concentrated brine end can also be realized, and the discharge concentration is not higher than one ten thousandth or one hundred thousandth of the inlet water.

Description

Zero release processing system to volatile phenol in salt waste water

Technical Field

The utility model relates to a contain salt and contain the phenol waste water treatment field, especially relate to a zero release processing system to volatile phenol in containing salt waste water.

Background

High organic matter, high ammonia nitrogen and high toxicity salt-containing phenol wastewater discharged from chemical plants, pesticide plants and printing and dyeing plants is difficult to treat, and at present, the wastewater is usually diluted first and then treated. The treatment cost is high, and the treatment is not thorough. Some toxic substances reach the emission standard after being diluted, are not really converted into harmless substances, and the total amount of the toxic substances is unchanged.

For the treatment of waste water containing salt and phenol with high organic matter content, high ammonia nitrogen content and high toxicity, a supercritical oxidation process is mostly adopted in the prior art, but the conventional supercritical treatment is difficult to solve by two bottlenecks, wherein the reactor is blocked due to the precipitation of the salt in a supercritical state, and the size of the reactor is limited due to the influence of the pressure and the temperature of the reactor by strong oxidation corrosion, namely the size scale is limited.

Disclosure of Invention

The utility model aims at providing a zero release processing system to volatile phenol in the waste water that contains salt.

The utility model discloses an innovation point lies in the utility model discloses well earlier with gas floating tank carry out the preliminary treatment, get rid of the earlier part of the phenol that volatilizees in the waste water after the preliminary treatment, utilize multi-effect evaporator will not have phenol waste water and contain phenol waste water branch matter oxidation treatment, make contain phenol water at the system's inner loop oxidation, no outer row. The trace discharge of the concentrated brine end can also be realized, and the discharge concentration is not higher than one ten thousandth or one hundred thousandth of the inlet water. Just the utility model discloses in through feed inlet about the supercritical reactor setting, the upper portion intake surpasses the supercritical temperature of water, and the lower part is intake and is the subcritical temperature of water, forms temperature gradient from top to bottom, and upper portion salt is appeared from the aquatic, and the lower part has extremely strong salt solubility for subcritical temperature to make salt be difficult for appearing, guarantees the difficult jam in bottom.

In order to realize the purpose of the utility model, the technical proposal of the utility model is that: a zero-emission treatment system for volatile phenol in salt-containing wastewater comprises an air flotation tank, a multi-effect evaporator, a first preheating heat exchanger, a second preheating heat exchanger, a supercritical reactor, a multi-stream heat exchanger, an incineration torch, concentration equipment and a flash tank, wherein the supercritical reactor is provided with an upper feed inlet of the supercritical reactor and a lower feed inlet of the supercritical reactor, the lower feed inlet of the supercritical reactor is positioned at the middle lower part of the side wall of the supercritical reactor, the supercritical reactor is provided with two first supercritical reactor and a second supercritical reactor respectively, gas filled in the air flotation tank is inert gas, a gas outlet of the air flotation tank is communicated with the incineration torch, and a liquid inlet of the air flotation tank is communicated with a liquid inlet of the multi-effect evaporator through a liquid inlet pipeline; the non-condensable gas outlet of the multi-effect evaporator is communicated with an incineration torch, the concentrated solution outlet of the multi-effect evaporator is communicated with the first material inlet of a first preheating heat exchanger, the first material outlet of the first preheating heat exchanger is communicated with the material inlet of a concentrating device, the condensed water outlet of the multi-effect evaporator is communicated with the second material inlet of the first preheating heat exchanger through a first pipeline, the oil outlet of an air flotation tank is communicated with a first pipeline, the second material outlet of the first preheating heat exchanger is communicated with the upper feed inlet of the first supercritical reactor, the reaction fluid outlet of the first supercritical reactor is communicated with the medium inlet of the first preheating heat exchanger, the medium outlet of the first preheating heat exchanger is communicated with the feed inlet of a flash tank, the liquid phase discharge outlet of the flash tank is communicated with a liquid inlet pipeline, and the gas phase discharge outlet of the flash; the concentrated solution outlet of the concentrating device is communicated with the first material inlet of the second preheating heat exchanger, the first material outlet of the second preheating heat exchanger is communicated with the first material inlet of the multi-stream heat exchanger, the first material outlet of the multi-stream heat exchanger is communicated with the upper feed inlet of the second supercritical reactor through a second pipeline, the clear water pipeline is communicated with the second material inlet of the second preheating heat exchanger, the second material outlet of the second preheating heat exchanger is communicated with the second material inlet of the multi-stream heat exchange medium, and the second material outlet of the multi-stream heat exchange medium is communicated with the second pipeline; the salt discharging water port of the first supercritical reactor and the salt discharging water port of the second supercritical reactor are communicated with a medium inlet of a second preheating heat exchanger, and a medium outlet of the second preheating heat exchanger is communicated with a material heating medium inlet of the concentration equipment; a reaction fluid outlet of the second supercritical reactor is communicated with a medium inlet of the multi-stream heat exchanger, and a medium outlet of the multi-stream heat exchanger is communicated with a lower feed inlet of the first supercritical reactor and a lower feed inlet of the second supercritical reactor; the exhaust port of the concentration device is communicated with the incineration torch, the heating medium outlet of the concentration device is communicated with the external discharge pipeline, and the concentration device is also provided with a steam discharge port of the concentration device.

Furthermore, self-preheating constant-temperature pipeline reactors are arranged at the rear ends of the first supercritical reactor and the second supercritical reactor, a reaction fluid outlet of the first supercritical reactor is communicated with a material inlet of the first self-preheating constant-temperature pipeline reactor through a third pipeline, and a material outlet of the first self-preheating constant-temperature pipeline reactor is communicated with a medium inlet of the first preheating heat exchanger; the reaction fluid outlet of the second supercritical reactor is communicated with the second material inlet of the self-preheating constant-temperature pipeline reactor through a fourth pipeline, and the second material outlet of the self-preheating constant-temperature pipeline reactor is communicated with the medium inlet of the multi-stream heat exchanger; and the liquid inlet pipeline is provided with a deoxidizing device, and the third pipeline and the fourth pipeline are provided with oxygen injecting devices. The oxidation reaction does not occur in the supercritical reactor, firstly desalting, then oxidizing in a self-preheating constant temperature pipeline reactor, oxidizing phenol contained in the wastewater, and respectively taking the supercritical reactor as a desalting device and the self-preheating constant temperature pipeline reactor as an oxidizer. The problems of strict requirements on materials, insufficient reaction in time, incapability of full-welding manufacturing and the like caused by using a container as an oxidation reactor are solved, and the danger of blockage caused by salt precipitation in the supercritical oxidation process of a self-preheating constant-temperature pipeline reactor is also solved.

Further, from preheating the constant temperature pipeline reactor and including reaction tube and the head that is located the reaction tube both ends, it is material coil pipe and No. two material coil pipes respectively to be equipped with two material coil pipes in the constant temperature pipeline reactor from preheating, No. one material coil pipe both ends are stretched out from preheating the constant temperature pipeline reactor and both ends are respectively for preheating the material entry of constant temperature pipeline reactor and preheating the material export of constant temperature pipeline reactor from one, No. two material coil pipe both ends are stretched out from preheating the constant temperature pipeline reactor and both ends are respectively for preheating the material entry of constant temperature pipeline reactor No. two and preheating the material export of constant temperature pipeline reactor from preheating, still be equipped with on the constant temperature reactor from preheating the constant temperature reactor medium entry and from preheating the constant temperature reactor medium export from preheating. Compared with a supercritical reactor, the pipeline type structure has few welding seams and stronger corrosion resistance.

Furthermore, an organic matter dosing device is further arranged on the third pipeline and the fourth pipeline. Used for adjusting COD.

The utility model has the advantages that:

1. the utility model discloses well earlier with gas floating tank carry out the preliminary treatment, the preceding part of the phenol that volatilizees in with the waste water after the preliminary treatment is got rid of, utilizes multi-effect evaporator will not have phenol waste water and contain phenol waste water branch matter oxidation treatment, makes the oxidation of containing phenol water at the system's inner loop, and no outer row. The trace discharge of the concentrated brine end can also be realized, and the discharge concentration is not higher than one ten thousandth or one hundred thousandth of the inlet water.

2. The utility model discloses in through feed inlet about the supercritical reactor setting, the supercritical temperature of water is surpassed in the upper portion intaking, and the lower part is intake for the subcritical temperature of water, forms temperature gradient from top to bottom, and upper portion salt is appeared from the aquatic, and the lower part has extremely strong salt solubility for subcritical temperature to make salt be difficult for appearing, guarantees the difficult jam in bottom.

3. In the utility model, because a part of waste water at the front end of the self-preheating constant temperature pipeline reactor is discharged from the reaction of the supercritical reactor, under the condition of meeting the same treatment capacity, the flow of the waste water entering the self-preheating constant temperature pipeline reactor is relatively reduced, the equipment of the self-preheating constant temperature pipeline reactor can be made relatively smaller, the material cost is greatly reduced, deoxidization is carried out before the waste water enters the supercritical reactor, oxidation reaction can be avoided from occurring in the supercritical reactor, the requirement can be relaxed in the material use of the supercritical reactor, then oxidation reaction occurs in the self-preheating constant temperature pipeline reactor, because the self-preheating constant temperature pipeline reactor is of a pipeline structure, the welding seams are few relative to the supercritical reactor, the material is good, the corrosion resistance is stronger, the oxidation reaction is placed for the reaction in the self-preheating constant temperature pipeline reactor, therefore, the supercritical reactor is taken as a desalter and the self-preheating constant-temperature pipeline reactor is taken as an oxidizer respectively. The problems of strict requirements on materials, insufficient reaction in time, incapability of full-welding manufacturing and the like caused by using a container as an oxidation reactor are solved, and the danger of blockage caused by salt precipitation in the supercritical oxidation process of a self-preheating constant-temperature pipeline reactor is also solved.

4. The utility model discloses in will remove salt and separate with the oxidation, remove the material cost and the manufacturing cost who has reduced this set of device by a wide margin, technically, also make supercritical oxidation be applied to great treatment capacity scale and become possible.

5. The utility model discloses in with the salt waste water that contains of a supercritical reactor and No. two supercritical reactors, water in the supercritical reactor is phenol-containing waste water, and the salt content is less for mixing the salt waste water that contains of No. two supercritical reactors, can avoid the salt elimination pipeline jam of No. two supercritical reactor departments.

6. The utility model discloses in will not have phenol waste water heat transfer to sub supercritical state to flow back to supercritical reactor lower part feed inlet, utilize the superstrong salt solubility of dissolving under the nearly supercritical to take out the salt that appears in with the supercritical reaction and arrange outward. Meanwhile, effective isolation of phenol is formed between the discharge port and the reaction cavity, and the discharge of phenol is further fundamentally avoided.

7. The whole system fully distributes and utilizes the heat energy.

Drawings

Fig. 1 is a schematic structural view of

embodiments

1 and 3.

Fig. 2 is a schematic structural diagram of

embodiments

2, 4 and 5.

FIG. 3 is a schematic diagram of the structure of a self-preheating isothermal pipe reactor.

Detailed Description

The technical solution in the embodiments of the present invention will be clearly and completely described below with reference to the accompanying drawings.

Example 1: as shown in fig. 1, a zero-emission treatment system for volatile phenol in salt-containing wastewater comprises an air flotation tank 1, a multi-effect evaporator 2, a first preheating heat exchanger 3, a second preheating heat exchanger 4, a supercritical reactor, a multi-stream heat exchanger 6, an incineration torch 7, a concentration device 8 and a flash tank 9, wherein the supercritical reactor is provided with an upper feed inlet of the supercritical reactor and a lower feed inlet of the supercritical reactor, the lower feed inlet of the supercritical reactor is positioned at the middle lower part of the side wall of the supercritical reactor, the supercritical reactor is provided with two first supercritical reactor 5-1 and second supercritical reactor 5-2 respectively, gas filled in the air flotation tank 1 is inert gas, a gas outlet 1.1 of the air flotation tank is communicated with the incineration torch 7, and a water outlet 1.2 of the air flotation tank is communicated with a feed liquid inlet 2.1 of the multi-effect evaporator through a liquid inlet pipeline 10; a noncondensable gas outlet 2.2 of the multi-effect evaporator is communicated with an incineration torch 7, a concentrated solution outlet 2.3 of the multi-effect evaporator is communicated with a first material inlet 3.1 of a preheating heat exchanger, a first material outlet 3.2 of the preheating heat exchanger is communicated with a material inlet 8.1 of concentration equipment, a condensed water outlet 2.4 of the multi-effect evaporator is communicated with a second material inlet 3.3 of the preheating heat exchanger through a first pipeline 11, an oil outlet 1.3 of an air flotation tank is communicated with the first pipeline 11, a second material outlet 3.4 of the preheating heat exchanger is communicated with an upper feed inlet 5-1.1 of the supercritical reactor, a reaction fluid outlet 5-1.2 of the supercritical reactor is communicated with a medium inlet 3.5 of the preheating heat exchanger, a medium outlet 3.6 of the preheating heat exchanger is communicated with a feed inlet 9.1 of a flash tank, a liquid phase discharge outlet 9.2 of the flash tank is communicated with a liquid inlet 10, and a gas phase discharge outlet 9.3 of the flash tank is communicated with a steam inlet 2.5 of; a concentrated solution outlet 8.2 of the concentration equipment is communicated with a first material inlet 4.1 of a second preheating heat exchanger, a first material outlet 4.2 of the second preheating heat exchanger is communicated with a first material inlet 6.1 of a multi-strand heat exchanger, a first material outlet 6.2 of the multi-strand heat exchanger is communicated with an upper feed inlet 5-2.1 of the second supercritical reactor through a second pipeline 12, a clear water pipeline 13 is communicated with a second material inlet 4.3 of the second preheating heat exchanger, a second material outlet 4.4 of the second preheating heat exchanger is communicated with a second material inlet 6.3 of a multi-strand heat exchange medium, and a second material outlet 6.3 of the multi-strand heat exchange medium is communicated with a second pipeline 12; a salt discharging water port 5-1.3 of the first supercritical reactor and a salt discharging water port 5-2.3 of the second supercritical reactor are communicated with a medium inlet 4.5 of the second preheating heat exchanger, and a medium outlet 4.6 of the second preheating heat exchanger is communicated with a material heating medium inlet 8.3 of the concentration equipment; a reaction fluid outlet 5-2.2 of the second supercritical reactor is communicated with a medium inlet 6.5 of the multi-stream heat exchanger, and a medium outlet 6.6 of the multi-stream heat exchanger is communicated with a lower feed inlet 5-1.4 of the first supercritical reactor and a lower feed inlet 5-2.4 of the second supercritical reactor; the exhaust port 8.4 of the concentration device is communicated with the incineration torch 7, the heating medium outlet 8.5 of the concentration device is communicated with the external discharge pipeline 14, and the steam discharge port 8.6 of the concentration device is also arranged on the concentration device 8.

Example 2: as shown in fig. 2, a zero-emission treatment system for volatile phenol in salt-containing wastewater comprises an air flotation tank 1, a multi-effect evaporator 2, a first preheating heat exchanger 3, a second preheating heat exchanger 4, a supercritical reactor 5, a multi-stream heat exchanger 6, an incineration torch 7, a concentration device 8 and a flash tank 9, wherein the supercritical reactor 5 is provided with an upper feed inlet of the supercritical reactor and a lower feed inlet of the supercritical reactor, the lower feed inlet of the supercritical reactor is positioned at the middle lower part of the side wall of the supercritical reactor 5, the supercritical reactor 5 is provided with two first supercritical reactor 5-1 and second supercritical reactor 5-2 respectively, a gas outlet 1.1 of the air flotation tank is communicated with the incineration torch 7, and a water outlet 1.2 of the air flotation tank is communicated with an inlet 2.1 of the multi-effect feed liquid evaporator through a liquid inlet pipeline 10; a noncondensable gas outlet 2.2 of a multi-effect evaporator is communicated with an incineration torch 7, a concentrated solution outlet 2.3 of the multi-effect evaporator is communicated with a first material inlet 3.1 of a preheating heat exchanger, a first material outlet 3.2 of the preheating heat exchanger is communicated with a material inlet 8.1 of concentration equipment, a condensed water outlet 2.4 of the multi-effect evaporator is communicated with a second material inlet 3.3 of the preheating heat exchanger through a first pipeline 11, an oil outlet 1.3 of an air flotation tank is communicated with the first pipeline 11, a second material outlet 3.4 of the preheating heat exchanger is communicated with an upper feed inlet 5-1.1 of the supercritical reactor, a self-preheating constant temperature pipeline reactor 15 is arranged at the rear end of each of a first supercritical reactor 5-1 and a second supercritical reactor 5-2, the self-preheating constant temperature pipeline reactor 15 comprises a reaction pipeline 15.6 and end sockets 15.7 positioned at two ends of the reaction pipeline 15.6, two coils of materials, a first material coil 15.8 and a second material coil 15.9 are respectively arranged in the self-preheating constant temperature pipeline reactor 15, two ends of a first material coil 15.8 extend out of the self-preheating constant-temperature pipeline reactor 15, two ends of the first material coil are respectively a first material inlet 15.1 of the self-preheating constant-temperature pipeline reactor and a first material outlet 15.2 of the self-preheating constant-temperature pipeline reactor, two ends of a second material coil 15.9 extend out of the self-preheating constant-temperature pipeline reactor, two ends of the second material coil are respectively a second material inlet 15.3 of the self-preheating constant-temperature pipeline reactor and a second material outlet 15.4 of the self-preheating constant-temperature pipeline reactor, and a medium inlet 15.10 of the self-preheating constant-temperature reactor and a medium outlet 15.11 of the self-preheating constant-temperature reactor are further arranged on the self-preheating constant-temperature. A first supercritical reactor reaction fluid outlet 5-1.2 is communicated with a first material inlet 15.1 of a self-preheating constant temperature pipeline reactor through a third pipeline 16, and a first material outlet 15.2 of the self-preheating constant temperature pipeline reactor is communicated with a first preheating heat exchanger medium inlet 3.5; a medium outlet 3.6 of the first preheating heat exchanger is communicated with a feed inlet 9.1 of the flash tank, a liquid phase discharge port 9.2 of the flash tank is communicated with a liquid inlet pipeline 10, and a gas phase discharge port 9.3 of the flash tank is communicated with a steam inlet 2.5 of the multi-effect evaporator; a concentrated solution outlet 8.2 of the concentration equipment is communicated with a first material inlet 4.1 of a second preheating heat exchanger, a first material outlet 4.2 of the second preheating heat exchanger is communicated with a first material inlet 6.1 of a multi-strand heat exchanger, a first material outlet 6.2 of the multi-strand heat exchanger is communicated with an upper feed inlet 5-2.1 of the second supercritical reactor through a second pipeline 12, a clear water pipeline 13 is communicated with a second material inlet 4.3 of the second preheating heat exchanger, a second material outlet 4.4 of the second preheating heat exchanger is communicated with a second material inlet 6.3 of a multi-strand heat exchange medium, and a second material outlet 6.4 of the multi-strand heat exchange medium is communicated with a second pipeline 12; a salt discharging water port 5-1.3 of the first supercritical reactor and a salt discharging water port 5-2.3 of the second supercritical reactor are communicated with a medium inlet 4.5 of the second preheating heat exchanger, and a medium outlet 4.6 of the second preheating heat exchanger is communicated with a material heating medium inlet 8.3 of the concentration equipment; a second supercritical reactor reaction fluid outlet 5-2.2 is communicated with a second material inlet 15.3 of the self-preheating constant temperature pipeline reactor through a fourth pipeline 17, and a second material outlet 15.4 of the self-preheating constant temperature pipeline reactor is communicated with a multi-stream heat exchanger medium inlet 6.5; the liquid inlet pipeline 10 is provided with a deoxidizing device 18, the third pipeline 16 and the fourth pipeline 17 are provided with oxygen injecting devices 19, and the third pipeline 16 and the fourth pipeline 17 are also provided with organic matter dosing devices 20. A medium outlet 6.6 of the multi-stream heat exchanger is communicated with a lower feed inlet 5-1.4 of the first supercritical reactor and a lower feed inlet 5-2.4 of the second supercritical reactor; the exhaust port 8.4 of the concentration device is communicated with the incineration torch 7, the heating medium outlet 8.5 of the concentration device is communicated with the external discharge pipeline 14, and the steam discharge port 8.6 of the concentration device is also arranged on the concentration device 8.

Example 3: as shown in fig. 1, a zero-emission treatment process for volatile phenol in salt-containing wastewater comprises the following steps: oil, gas and waste water are separated from the salt and phenol-containing waste water through an air floating tank 1, waste gas separated from the air floating tank 1 is incinerated through an incineration torch 7, waste water at the separation part of the air floating tank 1 is evaporated through a multi-effect evaporator 2, waste gas of the multi-effect evaporator 2 is incinerated through the incineration torch 7, concentrated waste water after multi-effect evaporation is heated through a first preheating heat exchanger 3 and then enters a concentration device 8 for concentration, waste gas generated after concentration is incinerated through the incineration torch 7, concentrated steam is discharged outside, concentrated solution is heated through a second preheating heat exchanger 4 and then is further heated through a multi-stream heat exchanger 6, and clear water heated through the second preheating heat exchanger 4 and the multi-stream heat exchanger 6 in sequence is mixed to be higher than the supercritical temperature of the water and then enters a feed inlet 5-2.1 at the upper part of the second supercritical reactor; condensed water of the multi-effect evaporator 2 is heated to be higher than the supercritical temperature of water through the first preheating heat exchanger 3 and then enters a feed inlet 5-1.1 at the upper part of the first supercritical reactor; the reaction fluid of the second supercritical reactor 5-2 is used as a heating medium, enters a multi-stream heat exchanger for heat exchange 6, is divided into two parts when reaching the subcritical temperature of water, and enters a first supercritical reactor lower feed inlet 5-1.4 and a second supercritical reactor lower feed inlet 5-2.4 respectively; the reaction fluid of the first supercritical reactor 5-1 is used for heating the first preheating heat exchanger 3, the reaction fluid discharged from the first supercritical reactor 5-1 is exchanged with the first preheating heat exchanger 3 and then enters a flash tank 9 for flash evaporation, the gas phase of the flash tank 9 is used for heating the multi-effect evaporator 2, and the liquid phase of the flash tank 9 and the wastewater separated from the gas floating tank 1 are mixed and enter the multi-effect evaporator 2 for circular treatment; the salt-containing wastewater of the first supercritical reactor 5-1 and the salt-containing wastewater of the second supercritical reactor 5-2 are mixed and then are used for heat exchange of the second preheating heat exchanger 4, and the salt-containing wastewater is used as a heat source of the concentration equipment 8 after heat exchange with the second preheating heat exchanger 4 and is discharged after being used as the heat source.

Example 4: as shown in fig. 2, a zero-emission treatment process for volatile phenol in salt-containing wastewater comprises the following steps: oil, gas and waste water are separated from the salt and phenol-containing waste water through an air floating tank 1, waste gas separated from the air floating tank 1 is incinerated through an incineration torch 7, waste water at the separation part of the air floating tank 1 is evaporated through a multi-effect evaporator 2, waste gas of the multi-effect evaporator 2 is incinerated through the incineration torch 7, concentrated waste water after multi-effect evaporation is heated through a first preheating heat exchanger 3 and then enters a concentration device 8 for concentration, waste gas generated after concentration is incinerated through the incineration torch 7, concentrated steam is discharged outside, concentrated solution is heated through a second preheating heat exchanger 4 and then is further heated through a multi-stream heat exchanger 6, and clear water heated through the second preheating heat exchanger 4 and the multi-stream heat exchanger 6 in sequence is mixed to be higher than the supercritical temperature of the water and then enters a feed inlet 5-2.1 at the upper part of the second supercritical reactor; condensed water of the multi-effect evaporator 2 is heated to be higher than the supercritical temperature of water through the first preheating heat exchanger 3 and then enters a feed inlet 5-1.1 at the upper part of the first supercritical reactor; mixing the liquid phase of the flash tank 9 and the wastewater separated from the gas floating tank 1, deoxidizing, entering a multi-effect evaporator 2, adding oxygen to the reaction fluid of a second supercritical reactor 5-2, adjusting COD, entering a self-preheating constant-temperature pipeline reactor 15 for oxidation reaction, keeping constant temperature in the self-preheating constant-temperature pipeline reactor 15 by adjusting circulating water quantity, discharging the reaction fluid of the second supercritical reactor 5-2 for heating of a multi-stream heat exchanger 6 after oxidation reaction, exchanging heat with the multi-stream heat exchanger 6 until the temperature is the subcritical temperature of water, and dividing the reaction fluid into two parts which respectively enter a first supercritical reactor lower feed inlet 5-1.4 and a second supercritical reactor lower feed inlet 5-2.4; the reaction fluid of the first supercritical reactor 5-1 is added with oxygen and adjusted with COD, enters a self-preheating constant temperature pipeline 15 reactor for oxidation reaction, the self-preheating constant temperature pipeline reactor 15 is kept at a constant temperature by adjusting the circulating water quantity, and the reaction fluid of the first supercritical reactor 5-1 is discharged for heating of the first preheating heat exchanger 3 after oxidation reaction; reaction fluid discharged from the first supercritical reactor 5-1 exchanges heat with the first preheating heat exchanger 3 and then enters a flash tank 9 for flash evaporation, the gas phase of the flash tank 9 is used for heating the multi-effect evaporator 2, and the liquid phase of the flash tank 9 and wastewater separated from the gas floating tank 1 are mixed and enter the multi-effect evaporator 2 for circular treatment; the salt-containing wastewater of the first supercritical reactor 5-1 and the salt-containing wastewater of the second supercritical reactor 5-2 are mixed and then are used for heat exchange of the second preheating heat exchanger 4, and the salt-containing wastewater is used as a heat source of the concentration equipment 8 after heat exchange with the second preheating heat exchanger 4 and is discharged after being used as the heat source.

Example 5: as shown in fig. 2, a zero-emission treatment process for volatile phenol in salt-containing wastewater comprises the following steps: oil, gas and waste water are separated from the saliferous phenol-containing waste water through an air floating tank 1, waste gas separated from the air floating tank 1 is incinerated through an incineration torch 7, waste water at the separation part of the air floating tank 1 is evaporated through a multi-effect evaporator 2, waste gas of the multi-effect evaporator 2 is incinerated through the incineration torch 7, concentrated waste water after multi-effect evaporation is heated through a first preheating heat exchanger 3 and then enters a concentration device 8 for concentration, waste gas generated after concentration is incinerated through the incineration torch 7, concentrated steam is discharged outside, concentrated liquid is heated through a second preheating heat exchanger 4 and then is further heated through a multi-stream heat exchanger 6, and clear water after being sequentially heated through the second preheating heat exchanger 4 and the multi-stream heat exchanger 6 is mixed to 390 ℃ and then enters an upper feeding port 5-2.1 of the second supercritical reactor; condensed water of the multi-effect evaporator 2 is heated to 390 ℃ by a first preheating heat exchanger 3 and enters a feed inlet 5-1.1 at the upper part of a first supercritical reactor; mixing the liquid phase of the flash tank 9 and the wastewater separated from the gas floating tank 1, deoxidizing, entering a multi-effect evaporator 2, adding oxygen to the reaction fluid of a second supercritical reactor 5-2, adjusting COD, entering a self-preheating constant-temperature pipeline reactor 15 for oxidation reaction, adjusting the amount of circulating water in the self-preheating constant-temperature pipeline reactor 15 to keep the temperature in the self-preheating constant-temperature pipeline reactor 15 at 500 ℃, discharging the reaction fluid of the second supercritical reactor 5-2 for heating of a multi-stream heat exchanger 6 after oxidation reaction, exchanging heat with the multi-stream heat exchanger 6 until the temperature is 365 ℃, and respectively entering a feed inlet 5-1.4 at the lower part of the first supercritical reactor and a feed inlet 5-2.4 at the lower part of the second supercritical reactor; the reaction fluid of the first supercritical reactor 5-1 is added with oxygen and adjusted with COD, enters a self-preheating constant temperature pipeline 15 reactor for oxidation reaction, the self-preheating constant temperature pipeline reactor 15 is kept at a constant temperature by adjusting the circulating water quantity, and the reaction fluid of the first supercritical reactor 5-1 is discharged for heating of the first preheating heat exchanger 3 after oxidation reaction; reaction fluid discharged from the first supercritical reactor 5-1 exchanges heat with the first preheating heat exchanger 3 and then enters a flash tank 9 for flash evaporation, the gas phase of the flash tank 9 is used for heating the multi-effect evaporator 2, and the liquid phase of the flash tank 9 and wastewater separated from the gas floating tank 1 are mixed and enter the multi-effect evaporator 2 for circular treatment; the salt-containing wastewater of the first supercritical reactor 5-1 and the salt-containing wastewater of the second supercritical reactor 5-2 are mixed and then are used for heat exchange of the second preheating heat exchanger 4, and the salt-containing wastewater is used as a heat source of the concentration equipment 8 after heat exchange with the second preheating heat exchanger 4 and is discharged after being used as the heat source.

The described embodiments are only some, but not all embodiments of the invention. Based on the embodiments in the present invention, all other embodiments obtained by a person skilled in the art without creative work belong to the protection scope of the present invention.

Claims

1. The zero-emission treatment system for volatile phenol in salt-containing wastewater is characterized by comprising an air flotation tank, a multi-effect evaporator, a first preheating heat exchanger, a second preheating heat exchanger, a supercritical reactor, a multi-stream heat exchanger, an incineration torch, concentration equipment and a flash tank, wherein the supercritical reactor is provided with an upper feed inlet of the supercritical reactor and a lower feed inlet of the supercritical reactor, the lower feed inlet of the supercritical reactor is positioned at the middle lower part of the side wall of the supercritical reactor, the supercritical reactor is provided with two first supercritical reactor and two supercritical reactor respectively, gas filled in the air flotation tank is inert gas, a gas outlet of the air flotation tank is communicated with the incineration torch, and a feed liquid inlet of the air flotation tank is communicated with a feed liquid inlet of the multi-effect evaporator through a liquid inlet pipeline; the non-condensable gas outlet of the multi-effect evaporator is communicated with an incineration torch, the concentrated solution outlet of the multi-effect evaporator is communicated with the first material inlet of a first preheating heat exchanger, the first material outlet of the first preheating heat exchanger is communicated with the material inlet of a concentrating device, the condensed water outlet of the multi-effect evaporator is communicated with the second material inlet of the first preheating heat exchanger through a first pipeline, the oil outlet of an air flotation tank is communicated with a first pipeline, the second material outlet of the first preheating heat exchanger is communicated with the upper feed inlet of the first supercritical reactor, the reaction fluid outlet of the first supercritical reactor is communicated with the medium inlet of the first preheating heat exchanger, the medium outlet of the first preheating heat exchanger is communicated with the feed inlet of a flash tank, the liquid phase discharge outlet of the flash tank is communicated with the liquid inlet pipeline, and the gas phase discharge outlet of the; the concentrated solution outlet of the concentrating device is communicated with the first material inlet of the second preheating heat exchanger, the first material outlet of the second preheating heat exchanger is communicated with the first material inlet of the multi-stream heat exchanger, the first material outlet of the multi-stream heat exchanger is communicated with the upper feed inlet of the second supercritical reactor through a second pipeline, the clear water pipeline is communicated with the second material inlet of the second preheating heat exchanger, the second material outlet of the second preheating heat exchanger is communicated with the second material inlet of the multi-stream heat exchange medium, and the second material outlet of the multi-stream heat exchange medium is communicated with the second pipeline; the salt discharging water port of the first supercritical reactor and the salt discharging water port of the second supercritical reactor are communicated with a medium inlet of a second preheating heat exchanger, and a medium outlet of the second preheating heat exchanger is communicated with a material heating medium inlet of the concentration equipment; a reaction fluid outlet of the second supercritical reactor is communicated with a medium inlet of the multi-stream heat exchanger, and a medium outlet of the multi-stream heat exchanger is communicated with a lower feed inlet of the first supercritical reactor and a lower feed inlet of the second supercritical reactor; the exhaust port of the concentration device is communicated with the incineration torch, the heating medium outlet of the concentration device is communicated with the external discharge pipeline, and the concentration device is also provided with a steam discharge port of the concentration device.

2. The zero-emission treatment system for volatile phenol in salt-containing wastewater according to claim 1, wherein self-preheating constant-temperature pipeline reactors are arranged at the rear ends of the first supercritical reactor and the second supercritical reactor, a reaction fluid outlet of the first supercritical reactor is communicated with a material inlet of the self-preheating constant-temperature pipeline reactor through a third pipeline, and a material outlet of the self-preheating constant-temperature pipeline reactor is communicated with a medium inlet of the first preheating heat exchanger; the reaction fluid outlet of the second supercritical reactor is communicated with the second material inlet of the self-preheating constant-temperature pipeline reactor through a fourth pipeline, and the second material outlet of the self-preheating constant-temperature pipeline reactor is communicated with the medium inlet of the multi-stream heat exchanger; and the liquid inlet pipeline is provided with a deoxidizing device, and the third pipeline and the fourth pipeline are provided with oxygen injecting devices.

3. The zero emission treatment system for volatile phenol in salt-containing wastewater according to claim 2, the self-preheating constant-temperature pipeline reactor is characterized by comprising a reaction pipeline and end sockets positioned at two ends of the reaction pipeline, two material coils are arranged in the self-preheating constant-temperature pipeline reactor and are respectively a material coil and a material coil, two ends of the material coil stretch out of the self-preheating constant-temperature pipeline reactor, two ends of the material coil are respectively a material inlet of the self-preheating constant-temperature pipeline reactor and a material outlet of the self-preheating constant-temperature pipeline reactor, and a medium inlet of the self-preheating constant-temperature reactor and a medium outlet of the self-preheating constant-temperature reactor are further arranged on the self-preheating constant.

4. The zero emission treatment system for volatile phenol in salt-containing wastewater according to claim 2, wherein an organic chemical dosing device is further arranged on the third pipeline and the fourth pipeline.