CN212315825U - Contain salt and difficult oxidation organic matter branch matter processing system - Google Patents
Contain salt and difficult oxidation organic matter branch matter processing system Download PDFInfo
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- CN212315825U CN212315825U CN202020705863.XU CN202020705863U CN212315825U CN 212315825 U CN212315825 U CN 212315825U CN 202020705863 U CN202020705863 U CN 202020705863U CN 212315825 U CN212315825 U CN 212315825U
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Abstract
The utility model discloses a contain salt and difficult oxidation organic matter branch matter processing system, No. one material export of multiple strand flow heat exchanger is through a pipeline and supercritical reactor upper portion feed inlet intercommunication, and clear water pipeline intercommunication preheats No. two material inlets of heat exchanger, preheats No. two material exports of heat exchanger and No. two material inlets of multiple strand flow heat transfer medium and communicates, and No. two material exports of multiple strand flow heat transfer medium and a pipeline communicate; the salt discharging water port of the supercritical reactor is communicated with the medium inlet of the preheating heat exchanger, and the medium outlet of the preheating heat exchanger is communicated with the material heating medium inlet of the concentration equipment; the supercritical reactor reaction fluid outlet is communicated with the multi-stream heat exchanger medium inlet, and the multi-stream heat exchanger medium outlet is communicated with the supercritical reactor lower feed inlet. The utility model provides a supercritical reactor is difficult for blockking up.
Description
Technical Field
The utility model relates to a contain salt and contain phenol waste water treatment field, especially relate to contain salt and difficult oxidation organic matter branch matter processing system.
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.
SUMMERY OF THE UTILITY MODEL
The utility model aims at providing a contain salt and difficult oxidation organic matter branch matter processing system.
The utility model discloses an innovation point lies in the utility model discloses in will contain phenol through multi-effect evaporator and separate away most phenol in the salt waste water that contains, will contain salt and contain a small amount of phenol water independent processing, through feed inlet about the supercritical reactor setting, the upper portion is intake and is surpassed the supercritical temperature of water, the lower part is intake and is the subcritical temperature of water, form temperature gradient from top to bottom, upper portion salt is appeared from the aquatic, the lower part has extremely strong salt solubility for subcritical temperature to make the salt difficult to appear, guarantee that the bottom is difficult to block up; the upper salt is precipitated from the water containing organic matter, and the lower salt is dissolved in the water containing no organic matter. The upper part and the lower part have temperature gradient, and the lower part has part of water upwards, which ensures stable temperature field and isolates upper organic substance from downwards diffusion.
In order to realize the purpose of the utility model, the technical proposal of the utility model is that: a system for treating saline and difficult-to-oxidize organic matters in different qualities comprises a multi-effect evaporator, a preheating heat exchanger, a supercritical reactor, a multi-stream heat exchanger and an incineration torch, 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, a non-condensable gas outlet of the multi-effect evaporator is communicated with the incineration torch, a concentrated solution outlet of the multi-effect evaporator is communicated with a material inlet of a concentration device, a concentrated solution outlet of the concentration device is communicated with a first material inlet of the preheating heat exchanger, a first material outlet of the preheating heat exchanger is communicated with a first material inlet of the multi-stream heat exchanger, a first material outlet of the multi-stream heat exchanger is communicated with the upper feed inlet of the supercritical reactor through a first pipeline, a clear water pipeline is communicated with a second material inlet of the preheating heat exchanger, a second material outlet of the preheating heat exchanger, the second material outlet of the multi-stream heat exchange medium is communicated with the first pipeline; the salt discharging water port of the supercritical reactor is communicated with the medium inlet of the preheating heat exchanger, and the medium outlet of the preheating heat exchanger is communicated with the material heating medium inlet of the concentration equipment; the supercritical reactor reaction fluid outlet is communicated with the multi-stream heat exchanger medium inlet, and the multi-stream heat exchanger medium outlet is communicated with a feed inlet at the lower part of the 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.
Further, a self-preheating constant-temperature pipeline reactor is also arranged between the supercritical reactor and the multi-stream heat exchanger, a reaction fluid outlet of the supercritical reactor is communicated with a material inlet of the self-preheating constant-temperature pipeline reactor through a second pipeline, and a material outlet of the self-preheating constant-temperature pipeline reactor is communicated with a medium inlet of the multi-stream heat exchanger; and the oxygen removing device is arranged on the pipeline at the front ends of the upper feed inlet and the lower feed inlet of the supercritical reactor, and the oxygen injecting device is arranged on the second pipeline. The oxidation reaction does not occur in the supercritical reactor, firstly desalting, then oxidizing in a self-preheating constant temperature pipeline reactor, oxidizing a small amount of 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, be equipped with the material coil pipe in preheating the constant temperature pipeline reactor, the material coil pipe both ends stretch out from preheating the constant temperature pipeline reactor and both ends are respectively for preheating constant temperature pipeline reactor material entry and from preheating the constant temperature pipeline reactor material export, still are equipped with from preheating the constant temperature reactor medium entry and from preheating the constant temperature reactor medium export on preheating the constant temperature reactor. 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 second pipeline. Used for adjusting COD.
The utility model has the advantages that:
1. in the utility model, the upper feed inlet and the lower feed inlet are arranged on the supercritical reactor, the upper water inlet exceeds the supercritical temperature of water, the lower water inlet is the subcritical temperature of water, the temperature gradient is formed from top to bottom, the upper salt is separated out from the water, and the lower subcritical temperature has strong salt solubility to ensure that the salt is not separated out easily, thereby ensuring that the bottom is not blocked easily; the upper salt is precipitated from the water containing organic matter, and the lower salt is dissolved in the water containing no organic matter. The upper part and the lower part have temperature gradient, and the lower part has part of water upwards, which ensures stable temperature field and isolates upper organic substance from downwards diffusion.
2. 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.
3. 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.
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 figure 1, the system for treating the saline and difficult-to-oxidize organic substances in different qualities comprises a multi-effect evaporator 1, a preheating heat exchanger 2, a supercritical reactor 3, a multi-stream heat exchanger 4, an incineration torch 5 and a concentration device 6, wherein the supercritical reactor 2 is provided with a supercritical reactor upper feed inlet 3.1 and a supercritical reactor lower feed inlet 3.2, the supercritical reactor lower feed inlet 3.2 is positioned at the middle lower part of the side wall of the supercritical reactor 3, the multi-effect evaporator 4 is condensed by circulating water, a multi-effect evaporator non-condensed gas outlet 1.1 is communicated with the incineration torch 5, a multi-effect evaporator concentrated solution outlet 1.2 is communicated with a concentration device material inlet 6.1, a concentration device concentrated solution outlet 6.2 is communicated with a preheating heat exchanger first material inlet 2.1, a preheating heat exchanger first material outlet 2.2 is communicated with a multi-stream heat exchanger first material inlet 4.1, a multi-stream heat exchanger first material outlet 4.2 is communicated with a supercritical reactor upper feed inlet 3.1 through a first pipeline 7, the clear water pipeline 8 is communicated with a second material inlet 2.3 of the preheating heat exchanger, a second material outlet 2.4 of the preheating heat exchanger is communicated with a second material inlet 4.3 of the multi-stream heat exchange medium, and a second material outlet 4.4 of the multi-stream heat exchange medium is communicated with a first pipeline 7; a salt discharging water port 3.3 of the supercritical reactor is communicated with a medium inlet 2.5 of the preheating heat exchanger, and a medium outlet 2.6 of the preheating heat exchanger is communicated with a material heating medium inlet 6.3 of the concentration equipment; a supercritical reactor reaction fluid outlet 3.4 is communicated with a multi-stream heat exchanger medium inlet 4.5, and a multi-stream heat exchanger medium outlet 4.6 is communicated with a supercritical reactor lower feed inlet 3.2; the exhaust port 6.4 of the concentration device is communicated with the incineration torch 5, the heating medium outlet 6.5 of the concentration device is communicated with the external discharge pipeline 9, and the steam discharge port 6.6 of the concentration device is also arranged on the concentration device 6.
Example 2: as shown in figure 2, the system for treating the saline and difficult-to-oxidize organic substances in different qualities comprises a multi-effect evaporator 1, a preheating heat exchanger 2, a supercritical reactor 3, a multi-stream heat exchanger 4, an incineration torch 5 and a concentration device 6, wherein the supercritical reactor 2 is provided with a supercritical reactor upper feed inlet 3.1 and a supercritical reactor lower feed inlet 3.2, the supercritical reactor lower feed inlet 3.2 is positioned at the middle lower part of the side wall of the supercritical reactor 3, the multi-effect evaporator 4 is condensed by circulating water, a multi-effect evaporator non-condensed gas outlet 1.1 is communicated with the incineration torch 5, a multi-effect evaporator concentrated solution outlet 1.2 is communicated with a concentration device material inlet 6.1, a concentration device concentrated solution outlet 6.2 is communicated with a preheating heat exchanger first material inlet 2.1, a preheating heat exchanger first material outlet 2.2 is communicated with a multi-stream heat exchanger first material inlet 4.1, a multi-stream heat exchanger first material outlet 4.2 is communicated with a supercritical reactor upper feed inlet 3.1 through a first pipeline 7, the clear water pipeline 8 is communicated with a second material inlet 2.3 of the preheating heat exchanger, a second material outlet 2.4 of the preheating heat exchanger is communicated with a second material inlet 4.3 of the multi-stream heat exchange medium, and a second material outlet 4.4 of the multi-stream heat exchange medium is communicated with a first pipeline 7; a salt discharging water port 3.3 of the supercritical reactor is communicated with a medium inlet 2.5 of the preheating heat exchanger, and a medium outlet 2.6 of the preheating heat exchanger is communicated with a material heating medium inlet 6.3 of the concentration equipment; a self-preheating constant temperature pipeline reactor 10 is further arranged between the supercritical reactor 3 and the multi-stream heat exchanger 4, the self-preheating constant temperature pipeline reactor 10 comprises a reaction pipeline 10.3 and end sockets 10.4 positioned at two ends of the reaction pipeline 10.3, a material coil 10.5 is arranged in the self-preheating constant temperature pipeline reactor 10, two ends of the material coil 10.5 extend out of the self-preheating constant temperature pipeline reactor 10, two ends of the material coil are respectively a self-preheating constant temperature pipeline reactor material inlet 10.1 and a self-preheating constant temperature pipeline reactor material outlet 10.2, the self-preheating constant temperature reactor 10 is further provided with a self-preheating constant temperature reactor medium inlet 10.6 and a self-preheating constant temperature reactor medium outlet 10.7, the supercritical reactor reaction fluid outlet 3.4 is communicated with the self-preheating constant temperature pipeline reactor material inlet 10.1 through a second pipeline 11, and the self-preheating constant temperature pipeline reactor material outlet 10.2 is communicated with the multi-stream heat exchanger medium inlet 4.5; a deoxidizing device 12 is arranged on the pipeline at the front end of the upper feed inlet 2.1 of the supercritical reactor and the front end of the lower feed inlet 2.2 of the supercritical reactor, an oxygen injecting device 13 is arranged on the second pipeline 11, and an organic chemical adding device 14 is also arranged on the second pipeline 11; a medium outlet 4.6 of the multi-stream heat exchanger is communicated with a feed inlet 3.2 at the lower part of the supercritical reactor; the exhaust port 6.4 of the concentration device is communicated with the incineration torch 5, the heating medium outlet 6.5 of the concentration device is communicated with the external discharge pipeline 9, and the steam discharge port 6.6 of the concentration device is also arranged on the concentration device 6.
Example 3: as shown in figure 1, a quality-divided treatment process for organic matters containing salt and difficult to oxidize comprises the following steps: the method comprises the following steps that (1) salt-containing phenol wastewater is evaporated through a multi-effect evaporator 1, waste gas of the multi-effect evaporator 1 is burnt by a burning torch 5, concentrated wastewater after multi-effect evaporation enters a concentrating device 6 for concentration, waste gas generated after the concentration of the concentrating device 6 is burnt by the burning torch 5, steam generated after the concentration of the concentrating device 6 is discharged outside, concentrated liquid after the concentration of the concentrating device 6 is heated through a preheating heat exchanger 2, is further heated through a multi-stream heat exchanger 4, is mixed with clean water heated through the preheating heat exchanger 2 and the multi-stream heat exchanger 4 in sequence to reach the supercritical temperature higher than that of the water, and then enters a feed inlet 3.1 at the upper part of a; the reaction fluid of the supercritical reactor 3 is used as a heating medium, enters the multi-stream heat exchanger 4 for heat exchange, and then enters the feed inlet 3.2 at the lower part of the supercritical reactor when the temperature is the subcritical temperature of water; the salt-containing wastewater of the supercritical reactor 3 is used for heat exchange of the preheating heat exchanger 2, and the salt-containing wastewater is used as a heat source of the concentration equipment 6 after heat exchange with the preheating heat exchanger 2 and is discharged after being used as the heat source.
Example 4: as shown in FIG. 2, a treatment process for the organic substances containing salt and difficult to oxidize includes the following steps: the method comprises the following steps that (1) salt-containing phenol wastewater is evaporated through a multi-effect evaporator 1, waste gas of the multi-effect evaporator 1 is incinerated by an incineration torch 5, concentrated wastewater after multi-effect evaporation enters a concentration device 6 for concentration, waste gas generated after concentration of the concentration device 6 is incinerated by the incineration torch 5, steam generated after concentration of the concentration device 6 is discharged outside, concentrated liquid after concentration of the concentration device 6 is deaerated, is heated through a preheating heat exchanger 2, is further heated through a multi-stream heat exchanger 4, is mixed with clean water heated through the preheating heat exchanger 2 and the multi-stream heat exchanger 4 in sequence to reach the supercritical temperature higher than that of the water, and then enters a feed inlet 3.1 at the upper part of a; the method comprises the following steps that a reaction fluid of a supercritical reactor 3 is added with oxygen and COD is adjusted, then the reaction fluid enters a self-preheating constant-temperature pipeline reactor 10 for oxidation reaction, the self-preheating constant-temperature pipeline reactor 10 is kept at a constant temperature by adjusting the amount of circulating water, the reaction fluid of the supercritical reactor 3 is discharged out of the self-preheating constant-temperature pipeline reactor 10 after oxidation reaction and is used for heating a multi-stream heat exchanger 4, and the reaction fluid enters a feed inlet 3.2 at the lower part of the supercritical reactor when the temperature is controlled to be the subcritical temperature of water after heat exchange of the multi-stream heat exchanger 4; the salt-containing wastewater of the supercritical reactor 3 is used for heat exchange of the preheating heat exchanger 2, and the salt-containing wastewater is used as a heat source of the concentration equipment 6 after heat exchange with the preheating heat exchanger 2 and is discharged after being used as the heat source.
Example 5: as shown in FIG. 2, a treatment process for the organic substances containing salt and difficult to oxidize includes the following steps: the method comprises the following steps that (1) salt-containing phenol wastewater is evaporated through a multi-effect evaporator 1, waste gas of the multi-effect evaporator 1 is incinerated by an incineration torch 5, concentrated wastewater after multi-effect evaporation enters a concentration device 6 for concentration, waste gas generated after concentration of the concentration device 6 is incinerated by the incineration torch 5, steam generated after concentration of the concentration device 6 is discharged outside, concentrated liquid after concentration of the concentration device 6 is deaerated, is heated through a preheating heat exchanger 2, is further heated through a multi-stream heat exchanger 4, is mixed with clean water heated through the preheating heat exchanger 2 and the multi-stream heat exchanger 4 in sequence until the water temperature is 390 ℃, and then enters a feed inlet 3.1 at the upper part of a supercritical reactor; the method comprises the steps that a reaction fluid of a supercritical reactor 3 is added with oxygen and COD is adjusted, then the reaction fluid enters a self-preheating constant-temperature pipeline reactor 10 for oxidation reaction, the temperature in the self-preheating constant-temperature pipeline reactor 10 is kept at 500 ℃ by adjusting the amount of circulating water, the reaction fluid of the supercritical reactor 3 is discharged out of the self-preheating constant-temperature pipeline reactor 10 for heating of a multi-stream heat exchanger 4 after oxidation reaction, and then the reaction fluid enters a feed inlet 3.2 at the lower part of the supercritical reactor after heat exchange of the multi-stream heat exchanger 4 until the temperature is controlled to be 365 ℃; the salt-containing wastewater of the supercritical reactor 3 is used for heat exchange of the preheating heat exchanger 2, and the salt-containing wastewater is used as a heat source of the concentration equipment 6 after heat exchange with the preheating heat exchanger 2 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 (4)
1. A system for treating saline and difficult-to-oxidize organic matters in different qualities is characterized by comprising a multi-effect evaporator, a preheating heat exchanger, a supercritical reactor, a multi-stream heat exchanger and an incineration torch, 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, a non-condensable gas outlet of the multi-effect evaporator is communicated with the incineration torch, a concentrated solution outlet of the multi-effect evaporator is communicated with a material inlet of a concentration device, a concentrated solution outlet of the concentration device is communicated with a first material inlet of the preheating heat exchanger, a first outlet of the preheating heat exchanger is communicated with a first material inlet of the multi-stream heat exchanger, a first material outlet of the multi-stream heat exchanger is communicated with the upper feed inlet of the supercritical reactor through a first pipeline, a clear water pipeline is communicated with a second material, a second material outlet of the preheating heat exchanger is communicated with a second material inlet of the multi-stream heat exchange medium, and a second material outlet of the multi-stream heat exchange medium is communicated with a first pipeline; the salt discharging water port of the supercritical reactor is communicated with the medium inlet of the preheating heat exchanger, and the medium outlet of the preheating heat exchanger is communicated with the material heating medium inlet of the concentration equipment; the supercritical reactor reaction fluid outlet is communicated with the multi-stream heat exchanger medium inlet, and the multi-stream heat exchanger medium outlet is communicated with a feed inlet at the lower part of the 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 system for treating the salt-containing and difficult-to-oxidize organic substances according to claim 1, wherein a self-preheating constant temperature pipeline reactor is further arranged between the supercritical reactor and the multi-stream heat exchanger, the supercritical reactor reaction fluid outlet is communicated with a self-preheating constant temperature pipeline reactor material inlet through a second pipeline, and the self-preheating constant temperature pipeline reactor material outlet is communicated with a multi-stream heat exchanger medium inlet; and the oxygen removing device is arranged on the pipeline at the front ends of the upper feed inlet and the lower feed inlet of the supercritical reactor, and the oxygen injecting device is arranged on the second pipeline.
3. The system for treating the separated substances containing the salts and the organic substances difficult to oxidize according to claim 2, wherein the self-preheating constant temperature pipeline reactor comprises a reaction pipeline and end sockets positioned at two ends of the reaction pipeline, a material coil is arranged in the self-preheating constant temperature pipeline reactor, two ends of the material coil extend out of the self-preheating constant temperature pipeline reactor, the 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 temperature reactor.
4. The system for treating the substances containing the salts and the organic substances difficult to oxidize according to claim 2, wherein an organic substance feeding device is further arranged on the second pipeline.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
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| CN202020705863.XU CN212315825U (en) | 2020-04-30 | 2020-04-30 | Contain salt and difficult oxidation organic matter branch matter processing system |
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| Application Number | Priority Date | Filing Date | Title |
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| CN202020705863.XU CN212315825U (en) | 2020-04-30 | 2020-04-30 | Contain salt and difficult oxidation organic matter branch matter processing system |
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| CN212315825U true CN212315825U (en) | 2021-01-08 |
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| CN202020705863.XU Withdrawn - After Issue CN212315825U (en) | 2020-04-30 | 2020-04-30 | Contain salt and difficult oxidation organic matter branch matter processing system |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111533351A (en) * | 2020-04-30 | 2020-08-14 | 江苏水泽森环境治理有限公司 | System and process for treating salt-containing and difficult-to-oxidize organic matters according to quality |
-
2020
- 2020-04-30 CN CN202020705863.XU patent/CN212315825U/en not_active Withdrawn - After Issue
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111533351A (en) * | 2020-04-30 | 2020-08-14 | 江苏水泽森环境治理有限公司 | System and process for treating salt-containing and difficult-to-oxidize organic matters according to quality |
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