CN103754966A - Recycling method for inorganic salt in wastewater of phenoxy carboxylic acid weed killer - Google Patents
Recycling method for inorganic salt in wastewater of phenoxy carboxylic acid weed killer Download PDFInfo
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Abstract
The invention discloses a recycling method for inorganic salt in wastewater of a phenoxy carboxylic acid weed killer. The method comprises steps of evaporating and concentrating wastewater so as to obtain solid salt; thermal cracking organic substances in the solid salt into organic gas; allowing the organic gas obtained in thermal cracking to enter a burning device to be fully burned, shock cooling the obtained offgas and discharging; carbonizing the thermal cracked solid salt at a high temperature so as to be further purified to obtain high purity solid salt, and allowing the gas generated in carbonization to enter the burning device to be fully burned. The method has simple steps, is mature, and is applicable to industrial production. By adopting the method, the purity of the inorganic salt is improved, secondary waste difficult to process is not generated, the wastewater is recycled, the problem of treatment of high salt wastewater of the phenoxy carboxylic acid weed killer is effectively solved, and the method has prominent environment protection and social benefits.
Description
Technical field
The present invention relates to the recycling processing method of inorganic salt in a kind of trade effluent, particularly relate to the recycling processing method of inorganic salt in phenoxy carboxylic acid herbicides waste water.
Technical background
Numerous organic or inorganic Chemicals are in its production process, technique tends to because need to produce a large amount of brine wastes, sodium chloride content is wherein higher than 1%, many more than 10%, some even reaches more than 20%, for high-salt wastewater, the high-salt wastewater at present treatment process of maturation mostly is evaporation, will produce so a large amount of by-product abraum salts (NaCl).The sodium chloride content of this salt, more than 70%, contains a large amount of organic or inorganic impurity simultaneously, can not directly be used as industrial raw material salt, more can not be used for ediblely or medical, and most of producer stores away its heap.This salt is stored up not only a large amount of occupied grounds for a long time, and also to environment structure grave danger, salt and impurity very easily run off, and salinization surrounding soil jeopardizes vegetation around, simultaneously to around rivers, water source, rice field etc. pollute.
In phenoxy carboxylic acid herbicides production process, also produce a large amount of high-salt wastewaters, ripe processing mode is also to go out solid salt by evaporation concentration, can not be utilized effectively equally.Therefore, utilize suitable technology and equipment, recycle this high-salt wastewater, for an enterprise, there is far-reaching influence and social benefit.
At present, treatment technology for salt in trade effluent is disclosed less, applicant has applied for the patent of invention that " extracting method of inorganic salt and the resource utilization method of trade effluent in a kind of trade effluent " by name, application number are 201310184084.4, this patent discloses the extracting method of inorganic salt in a kind of trade effluent, step is: by trade effluent evaporation concentration, obtain solid inorganic salt, solid inorganic salt is contacted with oxygen-containing gas at the temperature that is less than or equal to 1000 ℃, and carbonization obtains high purity inorganic salt.This invention flow process is simple, the high purity that has realized inorganic salt in saliferous trade effluent, especially high salt industrial waste water reclaims, gained inorganic salt can re-use, the wasting of resources and the destruction to environment have been avoided, solved to a certain extent a processing difficult problem for high salt industrial waste water, but still there is certain deficiency in this method, in inorganic salt purge process, in high temperature cabonization process, can produce and have these toxic gases of poison gas (such as dioxin etc.) well not process, enter in air and can cause environmental pollution.
Summary of the invention
For above-mentioned deficiency, the invention provides the recycling processing method of inorganic salt in a kind of phenoxy carboxylic acid herbicides waste water, the method can well reclaim the inorganic salt in waste water, and without poisonous fume, discharge in whole process, obtaining highly purified inorganic salt can resource utilization recycle, and meets green, environmental requirement.
The present invention adopts waste water evaporation concentration desalination, and---the high exhaust temperatures after-flame that thermo-cracking (organic substance decomposing is low hydrocarbon thing)---carbonization---produces, the operational path of chilling discharge are processed the inorganic salt in waste water.Objectionable impurities in thorough innoxious waste gas, use thermo-cracking and carbonizing treatment industrial waste salt, organism in salt thoroughly can be removed, and by the high temperature after-flame of waste gas and the treatment technology of chilling, can farthest reduce and burn mephitical generation in organism process, objectionable impurities in the gas that makes to produce is thoroughly innoxious, has reduced environmental pollution.
Concrete technical scheme of the present invention is as follows:
A recycling processing method for inorganic salt in phenoxy carboxylic acid herbicides waste water, is characterized in that comprising the following steps:
(1) phenoxy carboxylic acid herbicides waste water is carried out to evaporation concentration, obtain solid salt;
(2) gained solid salt is added to thermal cracker, making the organic substance thermo-cracking in solid salt is organic gas;
(3) organic gas of thermo-cracking gained enters combustion unit and fully burns, and after gained tail gas quenching, discharges;
(4) solid salt after thermo-cracking enters carbonizing plant, by high temperature cabonization, solid salt is further purified, and obtains high-purity solid salt, and the gas that carbonization produces also enters combustion unit and fully burns.
The inventive method is to propose for the factory effluent of phenoxy carboxylic acid herbicides, and its key is that the salt high purity in waste water is reclaimed, and guarantees removal process non-environmental-pollution.The waste water that the factory effluent of the phenoxy carboxylic acid herbicides of present method indication directly produces in both can pesticide producing process, also can be the waste water that the waste water directly producing is obtained after processing, the operations such as composition, rectifying such as that described processing comprises is concentrated, adjusting pH, separate raw materials solvent by product.The inventive method can be share with additive method, so that waste water is comprehensively processed, the composition in waste water is carried out to the comprehensive utilization of resources and recovery.Waste water first can be carried out after other recyclable compositions are removed in pre-treatment enabling again present method, after also can adopting the present invention to remove to desalt, enable again additive method residue waste water is processed.
In above-mentioned resource utilization method, the factory effluent of described phenoxy carboxylic acid herbicides includes but not limited to 2,4-drips, 2 first 4 chlorine, 2,4-d butyl ester, 2,4-drips different monooctyl ester, cover grass energy (haloxyfop), haloxyfop-r-methyl (haloxyfop-r-methyl), Vi par, Thistrol, 2,4-drips propionic acid or 2,4-Embutox in process of production directly produce waste water or carry out waste water after treatment, described processing includes but not limited to concentrate, regulates the operations such as composition, rectifying such as pH, separate raw materials solvent by product.
In above-mentioned resource utilization method, thermo-cracking is carried out under oxygen free condition, and thermo-cracking temperature is 350-550 ℃.The thermo-cracking time is 5-60min, generally in 5-10min thermo-cracking, can complete.Time lengthening does not have much affect to result.
In above-mentioned resource utilization method, carbonization is carried out under the existence of oxygen-containing gas, and oxygen-containing gas is one or more in air, oxygen-rich air and oxygen.Carbonization is carried out at the temperature of 650-750 ℃.Carbonization time is 10-60min, generally in 10-15min carbonization, can complete.Time lengthening does not have much affect to result.
In above-mentioned resource utilization method, the gas of thermo-cracking and the carbonization gained 2-5s that burns at 900-1100 ℃, discharge after burning gained tail gas quenching to 200 is ℃ following.
In above-mentioned resource utilization method, the method for waste water evaporation concentration is single-effect evaporation, multiple-effect evaporation or MVR evaporation.
In above-mentioned resource utilization method, thermal cracker is tubular type pyrolysis reactor, rotary kiln pyrolysis reactor, bubbling fluidization bed bioreactor, circle transmission bed bioreactor, circulating fluid bed reactor, ablation reactor, rotating cone reactor or vacuum moving-burden bed reactor.
In above-mentioned resource utilization method, carbonizing plant is selected from rotary kiln, vertical incinerator, horizontal incinerator, box-type furnace, fluidizing furnace, grate incinerator or fluidized bed incinerator, preferably rotary kiln.
In above-mentioned resource utilization method, combustion unit is the disclosed roasting kiln for organic gas burning in existing field, for example in waste incineration for the treatment of the dual firing chamber of flue gas.
In above-mentioned resource utilization method, the inorganic salt purity after carbonization is more than 99%.
In above-mentioned resource utilization method, the high purity inorganic salt water wiring solution-forming obtaining, can be as ionogen or for other field.For example, when described inorganic salt are sodium-chlor, gained sodium chloride solution can, for chlorine industry, be preferably ionic membrane caustic soda.
Flow process of the present invention is simple, and technical maturity is applicable to industrialized utilization.The present invention first carries out high temperature pyrolysis to the inorganic salt that extract in waste water, carry out again high temperature cabonization, remove a small amount of organic substance wherein containing, improved the purity of inorganic salt, it can be re-used, not only reduce the waste of resource, also reduced the destruction of waste water to environment, there is good economic and social benefit.
The present invention can not produce reluctant secondary refuse, has realized the recycling of waste water, efficiently solves the processing problem of phenoxy carboxylic acid herbicides high-salt wastewater, and environmental protection and social benefit are outstanding.
Embodiment
Below by specific embodiment, the present invention is further elaborated, should be understood that, following explanation is only in order to explain the present invention, its particular content is not limited.
The effect of the present invention's thermal cracker used is exactly to make a small amount of organic substance generation thermo-cracking in inorganic salt become organic gas.Thermal cracker is a kind of process furnace of temperature controllable, adopts the mode of continuously feeding, interrupted discharging, by the organic substance decomposing of cleavable in material, is low hydrocarbon thing, in stove, is subnormal ambient, and the organic gas that organic cracking is produced is drawn.Those skilled in the art can select in prior art the disclosed device that meets above-mentioned requirements for the present invention as required, such as tubular type pyrolysis reactor (USC pyrolyzer, SRT pyrolyzer etc.), rotary kiln pyrolysis reactor, bubbling fluidization bed bioreactor, circle transmission bed bioreactor, circulating fluid bed reactor, ablation reactor, rotating cone reactor or vacuum moving-burden bed reactor.
The present invention's combustion unit used can be the disclosed roasting kiln for organic gas burning in existing field, and those skilled in the art can select voluntarily, as the dual firing chamber for the treatment of flue gas in waste incineration.
Carbonization equipment therefor of the present invention can be selected rotary kiln, vertical incinerator, horizontal incinerator, box-type furnace, fluidizing furnace, grate incinerator or fluidized bed incinerator, is preferably rotary kiln.
embodiment 1
Get 2, 4-D factory effluent, waste water is evaporated through MVR, obtain Industrial Salt, get the Industrial Salt 1000Kg of gained, detect to obtain sodium chloride content 90%, moisture 9.03%, TOC 0.95%, throw to tubular type pyrolysis reactor, under starvation, at 380 ℃ of high temperature pyrolysises, time 10min, the organic gas producing passes in combustion unit, under 1000 ℃ of high temperature, stop 2s, remaining solid is thrown to rotary kiln, under logical oxygen, at 700 ℃ of high temperature cabonization 15min, obtain high purity salt, sodium chloride content 99.94%, TOC content is 0.003%, the gas that carbonization produces also passes in combustion unit, with at high temperature fully burning together with the organic gas of thermo-cracking, the tail gas quenching to 200 producing ℃ following rear discharge.
Get above-mentioned steps gained high purity salt 300Kg, be made into 1000L salt solution, gained salt solution, as electrolysis with ion-exchange film salt solution, by Electrowinning caustic soda, chlorine and hydrogen, can be back to use in the middle of production.
embodiment 2
Get 2, 4-D factory effluent, by waste water through triple effect evaporation, obtain Industrial Salt, get the Industrial Salt 1000Kg of gained, detect to obtain KCE content 92.2%, moisture 6.74%, TOC 1.04%, throw to rotary kiln pyrolysis reactor, under starvation, at 400 ℃ of high temperature pyrolysis 8min, the organic gas producing passes in combustion unit, under 1000 ℃ of high temperature, stop 3s, remaining solid is thrown to rotary kiln, under logical oxygen, at 720 ℃ of high temperature cabonization 30min, obtain high purity salt, sodium chloride content 99.96%, TOC content is 0.003%, the gas that carbonization produces also passes in combustion unit, with at high temperature fully burning together with the organic gas of thermo-cracking, the tail gas quenching to 200 producing ℃ following rear discharge.
Get above-mentioned steps gained high purity salt 305Kg, be made into 1000L salt solution, gained salt solution, as electrolysis with ion-exchange film salt solution, by Electrowinning caustic soda, chlorine and hydrogen, can be back to use in the middle of production.
embodiment 3
Get 2 first 4 chlorine factory effluents, waste water is evaporated through MVR, obtain Industrial Salt, get the Industrial Salt 1000Kg of gained, detect to obtain sodium chloride content 91.6%, moisture 7.3%, TOC 1.06%, throw to bubbling fluidization bed bioreactor, under starvation, at 450 ℃ of high temperature pyrolysises, time 15min, the organic gas producing passes in dual firing chamber, under 1100 ℃ of high temperature, stop 2s, remaining solid is thrown to fluidized bed incinerator, under blowing air, at 750 ℃ of high temperature cabonization 10min, obtain high purity salt, sodium chloride content 99.90, TOC content is 0.002%, the gas that carbonization produces also passes in dual firing chamber, with at high temperature fully burning together with the organic gas of thermo-cracking, the tail gas quenching to 200 producing ℃ following rear discharge.
Get above-mentioned steps gained high purity salt 310Kg, be made into 1000L salt solution, gained salt solution, as electrolysis with ion-exchange film salt solution, by Electrowinning caustic soda, chlorine and hydrogen, can be back to use in the middle of production.
embodiment 4
Get 2, 4-d butyl ester factory effluent, waste water is evaporated through MVR, obtain Industrial Salt, get the Industrial Salt 1000Kg of gained, detect to obtain sodium chloride content 92.2%, moisture 6.8%, TOC 0.98%, throw to circle transmission bed bioreactor, under starvation, at 480 ℃ of high temperature pyrolysises, time 10min, the organic gas producing passes in combustion unit, under 1000 ℃ of high temperature, stop 2.5s, remaining solid is thrown to fluidizing furnace, under logical oxygen, at 700 ℃ of high temperature cabonization 30min, obtain high purity salt, sodium chloride content is more than 99.9%, TOC content is 0.003%, the gas that carbonization produces also passes in combustion unit, with at high temperature fully burning together with the organic gas of thermo-cracking, the tail gas quenching to 200 producing ℃ following rear discharge.
Get above-mentioned steps gained high purity salt 300Kg, be made into 1000L salt solution, gained salt solution, as electrolysis with ion-exchange film salt solution, by Electrowinning caustic soda, chlorine and hydrogen, can be back to use in the middle of production.
embodiment 5
Get 2, 4-drips propionic acid factory effluent, by waste water through triple effect evaporation, obtain Industrial Salt, get the Industrial Salt 1000Kg of gained, detect to obtain sodium chloride content 91.2%, moisture 7.8%, TOC 0.99%, throw to circulating fluid bed reactor, under starvation, at 500 ℃ of high temperature pyrolysises, time 5min, the organic gas producing passes in combustion unit, under 1100 ℃ of high temperature, stop 2s, remaining solid is thrown to horizontal incinerator, under blowing air, at 750 ℃ of high temperature cabonization 10min, obtain high purity salt, sodium chloride content 99.93%, TOC content is 0.003%, the gas that carbonization produces also passes in combustion unit, with at high temperature fully burning together with the organic gas of thermo-cracking, the tail gas quenching to 200 producing ℃ following rear discharge.
Get above-mentioned steps gained high purity salt 310Kg, be made into 1000L salt solution, gained salt solution, as electrolysis with ion-exchange film salt solution, by Electrowinning caustic soda, chlorine and hydrogen, can be back to use in the middle of production.
embodiment 6
Get 2, 4-Embutox factory effluent, waste water is evaporated through MVR, obtain Industrial Salt, get the Industrial Salt 1000Kg of gained, detect to obtain sodium chloride content 93%, moisture 5.72%, TOC1.25%, throw to ablation reactor, under starvation, at 500 ℃ of high temperature pyrolysises, time 10min, organic gas passes in combustion unit, under 1100 ℃ of high temperature, stop 3s, remaining solid is thrown to grate incinerator, under logical oxygen, at 720 ℃ of high temperature cabonization 15min, obtain high purity salt, sodium chloride content 99.98%, TOC content is 0.003%, the gas that carbonization produces also passes in combustion unit, with at high temperature fully burning together with the organic gas of thermo-cracking, the tail gas quenching to 200 producing ℃ following rear discharge.
Get above-mentioned steps gained high purity salt 305Kg, be made into 1000L salt solution, gained salt solution, as electrolysis with ion-exchange film salt solution, by Electrowinning caustic soda, chlorine and hydrogen, can be back to use in the middle of production.
embodiment 7
Get 2, 4-D factory effluent, by waste water through triple effect evaporation, obtain Industrial Salt, get the Industrial Salt 1000Kg of gained, detect to obtain KCE content 91.2%, moisture 7.43%, TOC 1.34%, throw to rotating cone reactor, under starvation, at 550 ℃ of high temperature pyrolysis 30min, organic gas passes in combustion unit, under 1100 ℃ of high temperature, stop 2s, remaining solid is thrown to rotary kiln, under logical oxygen, at 750 ℃ of high temperature cabonization 5min, obtain high purity salt, sodium chloride content 99.91%, TOC content is 0.003%, the gas that carbonization produces also passes in combustion unit, with at high temperature fully burning together with the organic gas of thermo-cracking, the tail gas quenching to 200 producing ℃ following rear discharge.
Get above-mentioned steps gained high purity salt 310Kg, be made into 1000L salt solution, gained salt solution, as electrolysis with ion-exchange film salt solution, by Electrowinning caustic soda, chlorine and hydrogen, can be back to use in the middle of production.
embodiment 8
Get 2, 4-D factory effluent, by waste water through triple effect evaporation, obtain Industrial Salt, get the Industrial Salt 1000Kg of gained, detect to obtain KCE content 91.5%, moisture 7.25%, TOC 1.34%, throw to vacuum moving-burden bed reactor, under starvation, at 350 ℃ of high temperature pyrolysis 60min, organic gas passes in combustion unit, under 900 ℃ of high temperature, stop 3s, remaining solid is thrown to rotary kiln, under logical oxygen, at 650 ℃ of high temperature cabonization 50min, obtain high purity salt, sodium chloride content 99.95%, TOC content is 0.003%, the gas that carbonization produces also passes in combustion unit, with at high temperature fully burning together with the organic gas of thermo-cracking, the tail gas quenching to 200 producing ℃ following rear discharge.
Get above-mentioned steps gained high purity salt 310Kg, be made into 1000L salt solution, gained salt solution, as electrolysis with ion-exchange film salt solution, by Electrowinning caustic soda, chlorine and hydrogen, can be back to use in the middle of production.
embodiment 9
Get 2, 4-drips different monooctyl ester factory effluent, by waste water through triple effect evaporation, obtain Industrial Salt, get the Industrial Salt 1000Kg of gained, detect to obtain KCE content 91.1%, moisture 6.25%, TOC 0.94%, throw to vacuum moving-burden bed reactor, under starvation, at 400 ℃ of high temperature pyrolysis 20min, organic gas passes in combustion unit, under 1050 ℃ of high temperature, stop 5s, remaining solid is thrown to rotary kiln, under logical oxygen, at 680 ℃ of high temperature cabonization 35min, obtain high purity salt, sodium chloride content 99.95%, TOC content is 0.002%, the gas that carbonization produces also passes in combustion unit, with at high temperature fully burning together with the organic gas of thermo-cracking, the tail gas quenching to 200 producing ℃ following rear discharge.
Get above-mentioned steps gained high purity salt 310Kg, be made into 1000L salt solution, gained salt solution, as electrolysis with ion-exchange film salt solution, by Electrowinning caustic soda, chlorine and hydrogen, can be back to use in the middle of production.
embodiment 10
Get cover grass energy factory effluent, by waste water through triple effect evaporation, obtain Industrial Salt, get the Industrial Salt 1000Kg of gained, detect to obtain KCE content 90.1%, moisture 7.22%, TOC 0.99%, throw to vacuum moving-burden bed reactor, under starvation, at 430 ℃ of high temperature pyrolysis 40min, organic gas passes in combustion unit, under 1050 ℃ of high temperature, stop 3.5s, remaining solid is thrown to rotary kiln, under logical oxygen, at 680 ℃ of high temperature cabonization 40min, obtain high purity salt, sodium chloride content 99.96%, TOC content is 0.001%, the gas that carbonization produces also passes in combustion unit, with at high temperature fully burning together with the organic gas of thermo-cracking, the tail gas quenching to 200 producing ℃ following rear discharge.
Get above-mentioned steps gained high purity salt 310Kg, be made into 1000L salt solution, gained salt solution, as electrolysis with ion-exchange film salt solution, by Electrowinning caustic soda, chlorine and hydrogen, can be back to use in the middle of production.
embodiment 11
Get haloxyfop-r-methyl factory effluent, by waste water through triple effect evaporation, obtain Industrial Salt, get the Industrial Salt 1000Kg of gained, detect to obtain KCE content 91.1%, moisture 6.03%, TOC 1.03%, throw to vacuum moving-burden bed reactor, under starvation, at 520 ℃ of high temperature pyrolysis 45min, organic gas passes in combustion unit, under 1100 ℃ of high temperature, stop 4.5s, remaining solid is thrown to rotary kiln, under logical oxygen, at 680 ℃ of high temperature cabonization 30min, obtain high purity salt, sodium chloride content 99.91%, TOC content is 0.001%, the gas that carbonization produces also passes in combustion chamber, with at high temperature fully burning together with the organic gas of thermo-cracking, the tail gas quenching to 200 producing ℃ following rear discharge.
Get above-mentioned steps gained high purity salt 305Kg, be made into 1000L salt solution, gained salt solution, as electrolysis with ion-exchange film salt solution, by Electrowinning caustic soda, chlorine and hydrogen, can be back to use in the middle of production.
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embodiment 12
Get mecopropP factory effluent, by waste water through triple effect evaporation, obtain Industrial Salt, get the Industrial Salt 1000Kg of gained, detect to obtain KCE content 91.1%, moisture 6.03%, TOC 1.00%, throw to vacuum moving-burden bed reactor, under starvation, at 350 ℃ of high temperature pyrolysis 45min, organic gas passes in combustion unit, under 1100 ℃ of high temperature, stop 4s, remaining solid is thrown to rotary kiln, under logical oxygen, at 650 ℃ of high temperature cabonization 30min, obtain high purity salt, sodium chloride content 99.91%, TOC content is 0.001%, the gas that carbonization produces also passes in combustion unit, with at high temperature fully burning together with the organic gas of thermo-cracking, the tail gas quenching to 200 producing ℃ following rear discharge.
Get above-mentioned steps gained high purity salt 305Kg, be made into 1000L salt solution, gained salt solution, as electrolysis with ion-exchange film salt solution, by Electrowinning caustic soda, chlorine and hydrogen, can be back to use in the middle of production.
embodiment 13
Get Thistrol factory effluent, by waste water through triple effect evaporation, obtain Industrial Salt, get the Industrial Salt 1000Kg of gained, detect to obtain KCE content 91.6%, moisture 5.16%, TOC 1.23%, throw to vacuum moving-burden bed reactor, under starvation, at 350 ℃ of high temperature pyrolysis 45min, organic gas passes in combustion unit, under 1100 ℃ of high temperature, stop 2.5s, remaining solid is thrown to rotary kiln, under logical oxygen, at 700 ℃ of high temperature cabonization 30min, obtain high purity salt, sodium chloride content 99.93%, TOC content is 0.001%, the gas that carbonization produces also passes in combustion unit, with at high temperature fully burning together with the organic gas of thermo-cracking, the tail gas quenching to 200 producing ℃ following rear discharge.
Get above-mentioned steps gained high purity salt 310Kg, be made into 1000L salt solution, gained salt solution, as electrolysis with ion-exchange film salt solution, by Electrowinning caustic soda, chlorine and hydrogen, can be back to use in the middle of production.
Above-described embodiment is only exemplary the inventive method have been carried out enumerating; in addition to the above methods; in prior art, the evaporating concentrating method of disclosed other waste water, waste water are removed organic method and also be may be used in the present invention, within also all belonging to protection domain of the present invention.
Claims (10)
1. a recycling processing method for inorganic salt in phenoxy carboxylic acid herbicides waste water, is characterized in that comprising the following steps:
(1) phenoxy carboxylic acid herbicides waste water is carried out to evaporation concentration, obtain solid salt;
(2) gained solid salt is added to thermal cracker, making the organic substance thermo-cracking in solid salt is organic gas;
(3) organic gas of thermo-cracking gained enters combustion unit and fully burns, and after gained tail gas quenching, discharges;
(4) solid salt after thermo-cracking enters carbonizing plant, by high temperature cabonization, solid salt is further purified, and obtains high-purity solid salt, and the gas that carbonization produces also enters combustion unit and fully burns.
2. recycling processing method according to claim 1, it is characterized in that: described phenoxy carboxylic acid herbicides waste water is 2,4-drips, 2 first 4 chlorine, 2,4-d butyl ester, 2,4-drips different monooctyl ester, cover grass energy, haloxyfop-r-methyl, Vi par, Thistrol, 2,4-drips the waste water that propionic acid or 2,4-Embutox directly produce in process of production or carries out waste water after treatment.
3. according to the recycling processing method of claim 1, it is characterized in that: thermo-cracking is carried out under oxygen free condition, thermo-cracking temperature is 350-550 ℃; Carbonization is carried out at the temperature of 650-750 ℃.
4. according to the recycling processing method of claim 1, it is characterized in that: the gas of thermo-cracking and the carbonization gained 2-5s that burns at 900-1100 ℃, discharge after burning gained tail gas quenching to 200 is ℃ following.
5. according to the recycling processing method of claim 1 or 3, it is characterized in that: carbonization is carried out under the existence of oxygen-containing gas, oxygen-containing gas is one or more in air, oxygen-rich air and oxygen.
6. according to the recycling processing method of claim 1 or 3, it is characterized in that: the thermo-cracking time is 5-60min, preferably 5-10min; Carbonization time is 10-60min, preferably 10-15min.
7. recycling processing method according to claim 1, is characterized in that: the method for waste water evaporation concentration is single-effect evaporation, multiple-effect evaporation or MVR evaporation; Thermal cracker is tubular type pyrolysis reactor, rotary kiln pyrolysis reactor, bubbling fluidization bed bioreactor, circle transmission bed bioreactor, circulating fluid bed reactor, ablation reactor, rotating cone reactor or vacuum moving-burden bed reactor; Carbonizing plant is rotary kiln, vertical incinerator, horizontal incinerator, box-type furnace, fluidizing furnace, grate incinerator or fluidized bed incinerator, preferably rotary kiln; Combustion unit is the roasting kiln for organic gas burning.
8. according to the recycling processing method of claim 1, it is characterized in that: the inorganic salt purity after carbonization is more than 99%.
9. recycling processing method according to claim 1, is characterized in that: the high purity inorganic salt water wiring solution-forming obtaining, and as ionogen or for other field.
10. recycling processing method according to claim 9, is characterized in that: when described inorganic salt are sodium-chlor, gained sodium chloride solution is for chlorine industry.
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105948150A (en) * | 2016-04-26 | 2016-09-21 | 天津理工大学 | Process and system for recycling high-chloride high-concentration non-degradable organic wastewater |
| CN107803395A (en) * | 2017-12-11 | 2018-03-16 | 广州叶林环保科技有限公司 | A kind of organic abraum salt low-temperature carbonization handling process |
| CN111689634A (en) * | 2020-06-10 | 2020-09-22 | 南京工业大学 | Method for treating trichloropyridine sodium alcoholate wastewater |
Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101161598A (en) * | 2007-08-10 | 2008-04-16 | 南京大学 | Resource method of deposed salt slag or heavy metal sewage sludge and its private facilities |
| CN102134072A (en) * | 2011-03-04 | 2011-07-27 | 南京工业大学 | Process for preparing activated carbon by utilizing residual sludge from sewage treatment in pesticide chemistry industry |
| CN102459091A (en) * | 2009-05-18 | 2012-05-16 | 孟山都技术公司 | Recovery of phosphorus values and salt impurities from aqueous waste streams |
| CN102765850A (en) * | 2012-05-15 | 2012-11-07 | 山西三维丰海化工有限公司 | Treatment process for 3,5,6-Trichloropyridin-2-ol sodium and chlorpyrifos production wastewater |
| CN102875005A (en) * | 2012-09-07 | 2013-01-16 | 广东省生态环境与土壤研究所 | Sludge biological carbonizing technology based on hydrothermal reaction |
| JP5224500B2 (en) * | 2007-07-20 | 2013-07-03 | 独立行政法人農業環境技術研究所 | Recycling system for rice husk gasification residue |
| CN103224261A (en) * | 2013-05-17 | 2013-07-31 | 山东潍坊润丰化工有限公司 | Method for extracting inorganic salt in industrial wastewater and method for recycling industrial wastewater |
| CN103342398A (en) * | 2013-07-17 | 2013-10-09 | 山东潍坊润丰化工有限公司 | Method for recovering high-purity organic salt from phosphorous-containing industrial wastewater |
-
2014
- 2014-01-09 CN CN201410009899.3A patent/CN103754966B/en active Active
Patent Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP5224500B2 (en) * | 2007-07-20 | 2013-07-03 | 独立行政法人農業環境技術研究所 | Recycling system for rice husk gasification residue |
| CN101161598A (en) * | 2007-08-10 | 2008-04-16 | 南京大学 | Resource method of deposed salt slag or heavy metal sewage sludge and its private facilities |
| CN102459091A (en) * | 2009-05-18 | 2012-05-16 | 孟山都技术公司 | Recovery of phosphorus values and salt impurities from aqueous waste streams |
| CN102134072A (en) * | 2011-03-04 | 2011-07-27 | 南京工业大学 | Process for preparing activated carbon by utilizing residual sludge from sewage treatment in pesticide chemistry industry |
| CN102765850A (en) * | 2012-05-15 | 2012-11-07 | 山西三维丰海化工有限公司 | Treatment process for 3,5,6-Trichloropyridin-2-ol sodium and chlorpyrifos production wastewater |
| CN102875005A (en) * | 2012-09-07 | 2013-01-16 | 广东省生态环境与土壤研究所 | Sludge biological carbonizing technology based on hydrothermal reaction |
| CN103224261A (en) * | 2013-05-17 | 2013-07-31 | 山东潍坊润丰化工有限公司 | Method for extracting inorganic salt in industrial wastewater and method for recycling industrial wastewater |
| CN103342398A (en) * | 2013-07-17 | 2013-10-09 | 山东潍坊润丰化工有限公司 | Method for recovering high-purity organic salt from phosphorous-containing industrial wastewater |
Non-Patent Citations (1)
| Title |
|---|
| 无锡染料厂: "碳化法治理染料工业含盐废水", 《化工环保》 * |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105948150A (en) * | 2016-04-26 | 2016-09-21 | 天津理工大学 | Process and system for recycling high-chloride high-concentration non-degradable organic wastewater |
| CN107803395A (en) * | 2017-12-11 | 2018-03-16 | 广州叶林环保科技有限公司 | A kind of organic abraum salt low-temperature carbonization handling process |
| CN111689634A (en) * | 2020-06-10 | 2020-09-22 | 南京工业大学 | Method for treating trichloropyridine sodium alcoholate wastewater |
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