CN101279803A - Processing system and method for printing and dyeing wastewater - Google Patents
Processing system and method for printing and dyeing wastewater Download PDFInfo
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- CN101279803A CN101279803A CNA2008100246773A CN200810024677A CN101279803A CN 101279803 A CN101279803 A CN 101279803A CN A2008100246773 A CNA2008100246773 A CN A2008100246773A CN 200810024677 A CN200810024677 A CN 200810024677A CN 101279803 A CN101279803 A CN 101279803A
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Abstract
The invention relates to a treatment system and a method for dyeing wastewater, which aims to solve the problem of difficult high concentration refractory dyeing and desizing wastewater treatment, and provides the system and the method for treating volumes of high concentration dyeing and desizing waste water by adopting the supercritical water oxidation technique. The treatment system has the technical proposals for realizing the invention that: the dyeing wastewater treatment system comprises a high pressure plunger pump, a feeding pipeline, a reactor and a first gas-liquid separator, the high pressure plunger pump, the reactor and the first gas-liquid separator are connected with one another sequentially through the feeding pipeline, and the system is characterized in that the treatment system is also provided with a high pressure storage tank, the high pressure storage tank is connected between the high pressure plunger pump and the reactor through the feeding pipeline, a valve is arranged on the pipeline between the high pressure storage tank and the reactor, and the high pressure storage tank is also equipped with a heater.
Description
Technical field
The present invention relates to the treatment system and the method for the waste water that produces in a kind of dyeing process, a kind of treatment system and method that contains the high density desized wastewater of more specifically saying so.
Background technology
Dyeing is the water rich and influential family, China's textile industry water is the 6th of an every profession and trade, and dyeing water accounts for 80% in the textile industry, and only 7% (mainly still being water coolant) of water reclamation rate of printing and dyeing, whole textile industry reclamation rate less than 10% is the minimum industry of water reclamation rate in all industries of the whole nation.Therefore the reclamation rate of conserve water resource, raising water is weaving, dyeing is very important and difficult task.
Dyeing and printing process comprises that pre-treatment comprises operations such as cotton fabric boiling-off, destarch, and the waste water that is produced by destarch is a kind of high-concentration organic industrial waste water, its organic pollutant content height, colourity are dark, alkalescence and the variation of pH value greatly, change of water quality is violent.PH in the waste water is generally 10～12 approximately, and CODCr is about 20000～30000, and most wastewater biological degradation property is poor, even can not be degraded by microorganisms fully, and difficulty of governance is big, becomes one of universally acknowledged serious industrial pollution source.
At present, methods such as physico-chemical process, biological process, electrolytic process, acidication method, photocatalytic oxidation, flocculation decoloration are adopted in domestic processing to dyeing waste water more.Physico-chemical process is at first to adopt flocculence to make majority of organic pollutants generation flocculating settling in the mud, adopts aeration to handle then.This method floor space is big, and the treatment time is long, but also can produce a large amount of mud and cause secondary pollution.Biological process is to handle the most cost-effective method of organic waste water.Aerobe method is the most general treatment technology of low-concentration organic waste water, but when being used to handle organic wastewater with difficult degradation thereby, then need carry out chemistry, physicochemical or biological process pre-treatment earlier, with the molecular structure that changes refractory organic or reduce the wherein concentration of some pollutent, reduce its toxicity, improve the BOD5/COD value of waste water, enable by microbiological degradation, utilization and stablize, for the stable and high treatment efficiency of subsequent biological treatment creates conditions.Anaerobic biological process often is used to high concentration hard-degraded organic waste water and handles, but the existence of high-alkali, inorganic salts that exists in the dyeing waste water and ammonia nitrogen can suppress the growth of anerobe.Supercritical water oxidation method (SCWO) mainly utilizes supercritical water, and (T=374 ℃, P=22.1MPa) for medium comes the oxygenolysis organism, this is a kind of deep oxidation method that can thoroughly destroy organic constitution.It can reach more than 99.9% general organic removal rate in the waste water.For making reaction process reach supercritical state, mixed solution must be heated to 380～700 ℃, for the bigger situation of treatment capacity, this in fact almost can't realize the very large well heater of required power.
Summary of the invention
The objective of the invention is, handle difficult problem, a kind of employing supercritical water oxidation technology is provided, the system and method that a large amount of high-concentration dye-printing desizing waste waters are handled at the high-concentration hardly-degradable dye-printing desizing waste water.
The technical scheme that realizes the foregoing invention purpose is:
A kind of treatment system of dyeing waste water, comprise high pressure plunger pump, transport pipe, reactor and first gas-liquid separator, high pressure plunger pump, reactor and first gas-liquid separator are connected successively by transport pipe, described treatment system also is provided with pressure storage tank, pressure storage tank is connected between high pressure plunger pump and the reactor by transport pipe, be provided with valve on the pipeline between pressure storage tank and the reactor, pressure storage tank also is provided with well heater.
Among the present invention, by a pressure storage tank is set between high pressure plunger pump and reactor, convert the dynamic heat to the waste water mixed solution in the prior art to static heating, reduce required heating power, make the waste water mixed solution reach supercritical state with the way that prolongs heat-up time.
As a further improvement on the present invention, between the described reactor and first gas-liquid separator, be connected with the high pressure wet cyclone, the input aperture of high pressure wet cyclone connects the delivery port of described reactor, and the delivery port of high pressure wet cyclone connects the input aperture of described first gas-liquid separator.This high pressure wet cyclone can be separated the inorganic salt that produce in the reactor, avoids the damage to equipment.
As a further improvement on the present invention, second interchanger is set between high pressure plunger pump and pressure storage tank, high pressure plunger pump connects first input aperture of second interchanger, and first delivery port of second interchanger connects the input aperture of pressure storage tank by transport pipe; The delivery port of high pressure wet cyclone connects second input aperture of second interchanger by pipeline, and second delivery port of second interchanger connects the input aperture of the 3rd interchanger, and the delivery port of the 3rd interchanger connects the input aperture of second gas-liquid separator; Also be provided with first interchanger between the input aperture of the delivery port of high pressure wet cyclone and described first gas-liquid separator.The setting of second interchanger can make the output liquid after the processing and the waste water mixed solution of high pressure plunger pump output carry out heat exchange, and pre-thermal wastewater mixed solution is saved the heated waste water mixed solution to the required energy of supercritical state.
The technical scheme that realizes another goal of the invention of the present invention is:
A kind of treatment process of dyeing waste water may further comprise the steps:
(1) every liter of dyeing waste water adds 63.75～162.5g oxygen or corresponding normal oxygenant, mixes after high pressure plunger pump is injected in the pressure storage tank;
(2) make and be full of above-mentioned mixing liquid in the pressure storage tank, close high pressure plunger pump, close the valve between pressure storage tank and the reactor; With well heater the mixing liquid in the pressure storage tank is carried out the static state heating;
(3) pressure to 22 in pressure storage tank～35Mpa during temperature to 380～700 ℃, opens the valve between pressure storage tank and the reactor;
(4) start high pressure plunger pump, high pressure plunger pump is forced into 22～35Mpa with above-mentioned mixed solution, continues to inject pressure storage tank, regulates the flow of high pressure plunger pump, makes it slowly to rise to rated flow;
(5) after mixing liquid enters reactor, stop the regular hour, wherein organism, ammonia nitrogen and total phosphorus and oxygenant are reacted fully, objectionable impuritiess such as the organism in the waste water, ammonia nitrogen and total phosphorus are degraded to carbonic acid gas, oxynitride and phosphoric acid salt
(6) water after handling is cooled off, discharge the water of the corresponding emission standard that reaches national regulation.
Oxygenant in the above-mentioned steps (1) can be liquid oxygen, air, KClO
3, NaClO, KMnO4 or H
2O
2Oxygen or oxygenant also can be injected in the pressure storage tank through high pressure plunger pump respectively, mix then.
In the inventive method, by a pressure storage tank is set between high pressure plunger pump and reactor, convert the dynamic heat to the waste water mixed solution in the prior art to static heating, reduce required heating power, make the waste water mixed solution reach supercritical state with the way that prolongs heat-up time.Before the waste water mixed solution reached temperature of reaction, the liquid in the high-pressure plunger air pump inoperative, basin can not enter reactor yet.The size of basin is decided according to needed treatment capacity, and the reacting weight that is generally 5～30min gets final product.After temperature reaches temperature of reaction, waste water and oxygenant in the basin promptly begin reaction process, start ram pump this moment, open the valve between basin and the reactor, the supercritical wastewater that the cold waste water that is come by ram pump will promote in the basin enters reactor and carries out abundant oxidizing reaction, be degraded to carbonic acid gas, oxynitride and phosphoric acid salt after the reaction of processes such as the organism in the waste water, ammonia nitrogen and total phosphorus, the principal pollutant in the waste water are removed, and reach emission standard.
As a further improvement on the present invention, between above-mentioned steps (5) and (6), also comprise the following steps:
Phosphoric acid salt in the product of step (5) is separated.Because the solubleness of phosphoric acid salt in supercritical water is less, can realize separating by the high pressure wet cyclone.
As a further improvement on the present invention, in above-mentioned steps (6), further comprise the following steps:
(6.1) heat that reaction is produced reclaims and utilizes;
(6.2) water after handling is cooled off and gas-liquid separation, discharge the water of the corresponding emission standard that reaches national regulation.
In above-mentioned steps (6.1), further comprise the following steps:
(6.1.1) mixing liquid with reacted high-temp liquid and high pressure plunger pump output in the step (5) carries out heat exchange, and the temperature of mixing liquid is risen as far as possible, and the temperature of high-temp liquid is descended.
Because the wastewater treatment reaction process is emitted a large amount of heat, and the mixed solution before the reaction need be heated to necessary temperature, so can reduce the energy consumption of process by this step.If the COD in the waste water reaches more than 35000, the heat that reaction is emitted is enough to make the temperature of cold liquid to rise to thermotonus, and just can stop heater heats this moment.
Can further include the following step in the above-mentioned steps (6.1):
Reacted high-temp liquid in the step (5) is divided into two strands, and one carries out preheating through interchanger to the waste water mixed solution before reacting earlier, and then cools off through interchanger, after gas-liquid separator carries out gas-liquid separation, can discharge or reuse; Another burst elder generation directly through interchanger producing steam, and then after gas-liquid separator carries out gas-liquid separation, discharge or reuse.
The invention provides a kind of supercritical water oxidation treatment method that can handle a large amount of dye-printing desizing waste waters, can be according to the water quality characteristic and the draining water quality requirement of dye-printing desizing waste water, processing condition such as the pressure by regulating operating process, temperature, and depending on the circumstances or the needs of the situation whether determine whether to add catalyzer, effluent index all can reach country's " integrated wastewater discharge standard " (GB8978-96) first discharge standard or direct reuse.
Embodiment
Be described further below in conjunction with embodiment.
As shown in Figure 1, a kind of treatment system of dyeing waste water, comprise high pressure plunger pump 1, transport pipe 14, reactor 4 and first gas-liquid separator 7, high pressure plunger pump 1, reactor 4 and first gas-liquid separator 7 are connected successively by transport pipe 14, pressure storage tank is connected between high pressure plunger pump 1 and the reactor 4 by transport pipe, be provided with valve 15 on the pipeline 14 between pressure storage tank 3 and the reactor 4, pressure storage tank 3 also is provided with well heater 31.Reactor 4 adopts tubular reactor, because reactor has certain length, mixed solution flows within it, produces one period the residence time.
Between the reactor 4 and first gas-liquid separator 7, be connected with the high pressure wet cyclone 5 and first interchanger 6, the input aperture 51 of high pressure wet cyclone connects the delivery port of reactor, the delivery port 62 that the delivery port 52 of high pressure wet cyclone connects input aperture 61, the first interchanger of first interchanger connects the input aperture of first gas-liquid separator 7.High pressure wet cyclone 5 can be separated the inorganic salt that produce in the reactor 4, avoids the damage to equipment.
As shown in Figure 2, present embodiment and last example are basic identical, and different is:
The setting of second interchanger 2 can make the output liquid after reactor 4 is handled and the waste water mixed solution of high pressure plunger pump output carry out heat exchange, and pre-thermal wastewater mixed solution is saved the heated waste water mixed solution to the required energy of supercritical state.
A kind of treatment process of dyeing waste water may further comprise the steps:
(1) in every liter of dyeing waste water, adds 63.75g oxygen, behind the thorough mixing, inject pressure storage tank by high pressure plunger pump;
(2) make and be full of above-mentioned mixing liquid in the pressure storage tank, close high pressure plunger pump, close the valve between pressure storage tank and the reactor; With well heater the mixing liquid in the pressure storage tank is carried out the static state heating;
(3) pressure in pressure storage tank is to 22Mpa, during temperature to 380 ℃, opens the valve between pressure storage tank and the reactor, starts high pressure plunger pump simultaneously;
(4) high pressure plunger pump is forced into 22Mpa with above-mentioned mixed solution, injects pressure storage tank, regulates the flow of high pressure plunger pump, makes it slowly to rise to rated flow;
(5) mixing liquid enters reactor, stops the regular hour, and wherein organism, ammonia nitrogen and total phosphorus and oxygenant are reacted fully, and objectionable impuritiess such as the organism in the waste water, ammonia nitrogen and total phosphorus are degraded to carbonic acid gas, oxynitride and phosphoric acid salt;
(6) mixing liquid with reacted high-temp liquid and high pressure plunger pump output carries out heat exchange, and the temperature of mixing liquid is risen as far as possible, and the temperature of high-temp liquid is descended.
The size of basin is decided according to needed treatment capacity among the embodiment, and the reacting weight that is generally 5～30min gets final product.
A kind of treatment process of dyeing waste water may further comprise the steps:
(1) hydrogen peroxide of adding 1255.8927.5% in every liter of dyeing waste water behind the thorough mixing, injects pressure storage tank by high pressure plunger pump;
(2) make and be full of above-mentioned mixing liquid in the pressure storage tank, close high pressure plunger pump, close the valve between pressure storage tank and the reactor; With well heater the mixing liquid in the pressure storage tank is carried out the static state heating;
(3) pressure in pressure storage tank is to 35Mpa, during temperature to 700 ℃, opens the valve between pressure storage tank and the reactor, starts high pressure plunger pump simultaneously;
(4) high pressure plunger pump is forced into 35Mpa with above-mentioned mixed solution, injects pressure storage tank, regulates the flow of high pressure plunger pump, makes it slowly to rise to rated flow;
(5) mixing liquid enters reactor, stops the regular hour, and wherein organism, ammonia nitrogen and total phosphorus and oxygenant are reacted fully, and objectionable impuritiess such as the organism in the waste water, ammonia nitrogen and total phosphorus are degraded to carbonic acid gas, oxynitride and phosphoric acid salt;
(6) phosphoric acid salt in the product of step (5) is realized separating with the high pressure wet cyclone;
(7) be two strands with the moisture after separating in the step (6), one carries out preheating through interchanger to the waste water mixed solution before reacting earlier, and then cools off through interchanger, after gas-liquid separator carries out gas-liquid separation, can discharge or reuse; Another burst elder generation directly through interchanger producing steam, and then after gas-liquid separator carries out gas-liquid separation, discharge or reuse.
A kind of treatment process of dyeing waste water may further comprise the steps:
(1), waste water and NaClO are injected pressure storage tank, thorough mixing then by high pressure plunger pump respectively according to the ratio that adds NaClO511.8g in every liter of dyeing waste water;
(2) make and be full of above-mentioned mixing liquid in the pressure storage tank, close high pressure plunger pump, close the valve between pressure storage tank and the reactor; With well heater the mixing liquid in the pressure storage tank is carried out the static state heating;
(3) pressure in pressure storage tank is to 25Mpa, during temperature to 600 ℃, opens the valve between pressure storage tank and the reactor, starts high pressure plunger pump simultaneously;
(4) high pressure plunger pump is forced into 25Mpa with above-mentioned mixed solution, injects pressure storage tank, regulates the flow of high pressure plunger pump, makes it slowly to rise to rated flow;
(5) mixing liquid enters reactor, stops the regular hour, and wherein organism, ammonia nitrogen and total phosphorus and oxygenant are reacted fully, and objectionable impuritiess such as the organism in the waste water, ammonia nitrogen and total phosphorus are degraded to carbonic acid gas, oxynitride and phosphoric acid salt;
(6) phosphoric acid salt in the product of step (5) is realized separating with the high pressure wet cyclone;
(7) be two strands with the moisture after separating in the step (6), one water is used for preheating from the effusive cold liquid of high pressure plunger pump, then this is water-cooled to the temperature that needs; Another strand uses it for anything else in addition according to the needs generation steam of production process, then this is water-cooled to the temperature that needs, reuse or directly discharging after cooled two strands of water converge.
Claims (9)
1, a kind of treatment system of dyeing waste water, comprise high pressure plunger pump, transport pipe, reactor and first gas-liquid separator, high pressure plunger pump, reactor and first gas-liquid separator are connected successively by transport pipe, it is characterized in that, described treatment system also is provided with pressure storage tank, pressure storage tank is connected between high pressure plunger pump and the reactor by transport pipe, is provided with valve on the pipeline between pressure storage tank and the reactor, and pressure storage tank also is provided with well heater.
2, the treatment process of dyeing waste water according to claim 1, it is characterized in that, between the described reactor and first gas-liquid separator, be connected with the high pressure wet cyclone, the input aperture of high pressure wet cyclone connects the delivery port of described reactor, and the delivery port of high pressure wet cyclone connects the input aperture of described first gas-liquid separator.
3, the treatment process of dyeing waste water according to claim 1, it is characterized in that, second interchanger is set between described high pressure plunger pump and pressure storage tank, high pressure plunger pump connects first input aperture of second interchanger, and first delivery port of second interchanger connects the input aperture of pressure storage tank by transport pipe; The delivery port of high pressure wet cyclone connects second input aperture of second interchanger by pipeline, and second delivery port of second interchanger connects the input aperture of the 3rd interchanger, and the delivery port of the 3rd interchanger connects the input aperture of second gas-liquid separator; Also be provided with first interchanger between the input aperture of the delivery port of high pressure wet cyclone and described first gas-liquid separator.
4, a kind of treatment process of dyeing waste water is characterized in that, this method may further comprise the steps:
(1) every liter of dyeing waste water adds 63.75～162.5g oxygen or corresponding normal oxygenant, behind the thorough mixing, is injected in the pressure storage tank by high pressure plunger pump; Or add the ratio of 63.75～162.5g oxygen or corresponding normal oxygenant according to every liter of dyeing waste water, and waste water and oxygen or corresponding normal oxygenant are injected in the pressure storage tank by high pressure plunger pump respectively, mix then;
(2) make and be full of above-mentioned mixing liquid in the pressure storage tank, close high pressure plunger pump, close the valve between pressure storage tank and the reactor; With well heater the mixing liquid in the pressure storage tank is carried out the static state heating;
(3) pressure to 22 in pressure storage tank～35Mpa during temperature to 380～700 ℃, opens the valve between pressure storage tank and the reactor;
(4) start high pressure plunger pump, high pressure plunger pump is forced into 22～35Mpa with above-mentioned mixed solution, continues to inject pressure storage tank, regulates the flow of high pressure plunger pump, makes it slowly to rise to rated flow;
(5) mixing liquid enters reactor, stops the regular hour, and wherein organism, ammonia nitrogen and total phosphorus and oxygenant are reacted fully, and objectionable impuritiess such as the organism in the waste water, ammonia nitrogen and total phosphorus are degraded to carbonic acid gas, oxynitride and phosphoric acid salt;
(6) water after handling is cooled off, discharge the water of the corresponding emission standard that reaches national regulation.
5, the treatment process of dyeing waste water according to claim 4 is characterized in that, the oxygenant in the above-mentioned steps (1) is liquid oxygen, air, KClO
3, NaClO, KMnO4 or H
2O
2
6, the treatment process of dyeing waste water according to claim 4 is characterized in that, also comprises the following steps: the phosphoric acid salt in the product of step (5) is separated between above-mentioned steps (5) and (6).
7, the treatment process of dyeing waste water according to claim 4 is characterized in that, further comprises the following steps: in above-mentioned steps (6)
(6.1) heat that reaction is produced reclaims and utilizes;
(6.2) water after handling is cooled off and gas-liquid separation, discharge the water of the corresponding emission standard that reaches national regulation.
8, the treatment process of dyeing waste water according to claim 7 is characterized in that, further comprises the following steps: in above-mentioned steps (6.1)
(6.1.1) the waste water mixing liquid with reacted high-temp liquid and high pressure plunger pump output in the step (5) carries out heat exchange, and the temperature of waste water mixing liquid is risen, and the temperature of high-temp liquid is descended.
9, the treatment process of dyeing waste water according to claim 7, it is characterized in that, in above-mentioned steps (6.1), further comprise the following steps: reacted high-temp liquid in the step (5) is divided into two strands, one carries out preheating through interchanger to the waste water mixed solution before reacting earlier, and then cool off through interchanger, after gas-liquid separator carries out gas-liquid separation, can discharge or reuse; Another burst elder generation directly through interchanger producing steam, and then after gas-liquid separator carries out gas-liquid separation, discharge or reuse.
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| CN101979337A (en) * | 2010-10-27 | 2011-02-23 | 南京工业大学 | System and method for treating garbage percolate by supercritical water oxidation method |
| CN101993143A (en) * | 2010-10-27 | 2011-03-30 | 南京工业大学 | System and method for processing alkaline residue wastewater by utilizing supercritical water oxidation method |
| CN102010054A (en) * | 2010-10-27 | 2011-04-13 | 南京工业大学 | System and method for processing blue-green algae by using supercritical water oxidation (SCWO) |
| CN102249461A (en) * | 2011-06-16 | 2011-11-23 | 西安交通大学 | Supercritical water oxidation treatment system for high-salt high-chlorine organic wastewater |
| CN102642965A (en) * | 2012-04-23 | 2012-08-22 | 西安交通大学 | Supercritical water oxidization treatment device for organic waste water and temperature control method |
| CN102849888A (en) * | 2012-10-11 | 2013-01-02 | 南京师范大学 | Zero-release organic wastewater treating device and zero-release organic wastewater treating method |
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| CN103601282A (en) * | 2013-11-25 | 2014-02-26 | 中国科学院山西煤炭化学研究所 | Method for treating refractory wastewater by virtue of supercritical water oxidation technology |
| CN103848530A (en) * | 2014-03-03 | 2014-06-11 | 无锡市中岳石化设备有限公司 | DDISO-integrated synchronous oxidation and desalination device |
| CN104030427A (en) * | 2014-06-16 | 2014-09-10 | 西安交通大学 | Supercritical water oxidation treatment system for printing and dyeing wastewater and sludge |
| CN104478519A (en) * | 2014-12-17 | 2015-04-01 | 河海大学 | Device and method for recovering nitrogen and phosphorus from supercritical water gasification products of blue algae liquid |
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| CN106082426A (en) * | 2016-08-10 | 2016-11-09 | 广州中国科学院先进技术研究所 | With H2o2supercritical water oxidation system and technique as oxidant |
| CN106123087A (en) * | 2016-06-15 | 2016-11-16 | 安徽省绿巨人环境技术有限公司 | A kind of industrial wastewater secondary reclamation set |
| CN108251093A (en) * | 2018-01-31 | 2018-07-06 | 南京工业大学 | The preparation system and method for a kind of supercritical fluid for heavy crude heat extraction |
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2008
- 2008-04-01 CN CN2008100246773A patent/CN101279803B/en not_active Expired - Fee Related
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| CN101993143A (en) * | 2010-10-27 | 2011-03-30 | 南京工业大学 | System and method for processing alkaline residue wastewater by utilizing supercritical water oxidation method |
| CN102010054A (en) * | 2010-10-27 | 2011-04-13 | 南京工业大学 | System and method for processing blue-green algae by using supercritical water oxidation (SCWO) |
| CN101993143B (en) * | 2010-10-27 | 2012-07-25 | 南京工业大学 | System and method for processing alkaline residue wastewater by utilizing supercritical water oxidation method |
| CN102249461A (en) * | 2011-06-16 | 2011-11-23 | 西安交通大学 | Supercritical water oxidation treatment system for high-salt high-chlorine organic wastewater |
| CN102249461B (en) * | 2011-06-16 | 2012-09-05 | 西安交通大学 | Supercritical water oxidation treatment system for high-salt high-chlorine organic wastewater |
| CN102642965A (en) * | 2012-04-23 | 2012-08-22 | 西安交通大学 | Supercritical water oxidization treatment device for organic waste water and temperature control method |
| CN102849888A (en) * | 2012-10-11 | 2013-01-02 | 南京师范大学 | Zero-release organic wastewater treating device and zero-release organic wastewater treating method |
| CN103496814A (en) * | 2013-09-29 | 2014-01-08 | 内蒙古工业大学 | Supercritical water oxidation treatment method for rubber industrial wastewater |
| CN103601282A (en) * | 2013-11-25 | 2014-02-26 | 中国科学院山西煤炭化学研究所 | Method for treating refractory wastewater by virtue of supercritical water oxidation technology |
| CN103848530A (en) * | 2014-03-03 | 2014-06-11 | 无锡市中岳石化设备有限公司 | DDISO-integrated synchronous oxidation and desalination device |
| CN104030427A (en) * | 2014-06-16 | 2014-09-10 | 西安交通大学 | Supercritical water oxidation treatment system for printing and dyeing wastewater and sludge |
| CN104478519A (en) * | 2014-12-17 | 2015-04-01 | 河海大学 | Device and method for recovering nitrogen and phosphorus from supercritical water gasification products of blue algae liquid |
| CN105953287A (en) * | 2016-06-15 | 2016-09-21 | 安徽省绿巨人环境技术有限公司 | Industrial wastewater recycling device |
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