CN102040197A - Method for removing ammonia nitrogen in hydrazine hydrate evaporation byproduct residues containing alkali salt by utilizing urea method - Google Patents
Method for removing ammonia nitrogen in hydrazine hydrate evaporation byproduct residues containing alkali salt by utilizing urea method Download PDFInfo
- Publication number
- CN102040197A CN102040197A CN 201010547834 CN201010547834A CN102040197A CN 102040197 A CN102040197 A CN 102040197A CN 201010547834 CN201010547834 CN 201010547834 CN 201010547834 A CN201010547834 A CN 201010547834A CN 102040197 A CN102040197 A CN 102040197A
- Authority
- CN
- China
- Prior art keywords
- ammonia nitrogen
- hydrazine hydrate
- alkali salt
- mass concentration
- wyler
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
Landscapes
- Water Treatment By Electricity Or Magnetism (AREA)
Abstract
The invention relates to a method for processing hydrazine hydrate evaporation byproduct residues containing alkali salt by utilizing a urea method, in particular to a method for removing ammonia nitrogen in hydrazine hydrate evaporation byproduct residues containing alkali salt by utilizing a urea method. The method provided by the invention comprises the following steps: dissolving the hydrazine hydrate evaporation byproduct residues containing the alkali salt into water to prepare crude brine; detecting and determining the mass concentration of sodium hydroxide, sodium carbonate and ammonia nitrogen in the crude brine; blasting chlorine into the crude brine to prepare sodium hypochlorite; and removing the excessive sodium hypochlorite after the content of the ammonia nitrogen is reduced to below 15ppm, thus obtaining the brine with the content of the ammonia nitrogen lower than 15ppm. The invention can treat the hydrazine hydrate evaporation byproduct residues containing the alkali salt so as to meet the requirements for the mass concentration of the ammonia nitrogen in the brine for electrolyzing caustic soda, realizes the comprehensive recycle of the hydrazine hydrate evaporation byproduct residues containing the alkali salt, fully utilizes resources, is environment-friendly, and has the advantages of less investment, simple process, easy operation, no new three-waste generation, low cost and economic feasibility.
Description
Technical field
The present invention relates to the treatment process that a kind of Wyler's process hydrazine hydrate by-product contains the alkali salt slag, particularly a kind of Wyler's process hydrazine hydrate by-product contains the removal methods of the ammonia nitrogen in the alkali salt slag.
Background technology
Hydrazine hydrate is widely used in medicine, the pesticide producing as a kind of important chemical material, and China mainly produces hydrazine hydrate with urea hypochlorite oxidation method at present, will produce a large amount of sodium-chlor and yellow soda ash inevitably in the process of production.Yellow soda ash mainly separates from hydrazine hydrate solution by the way of freezing and crystallizing, sodium-chlor and remaining a small amount of yellow soda ash then separate by consecutive evaporation, produce and contain the alkali salt slag in a large number, its composition is a sodium-chlor 70%, yellow soda ash 10～15%, sodium hydroxide 2%, water 12～15%, 0.5～0.6% hydrazine and amine.These materials that contain in the alkali salt slag all have utility value, wherein sodium-chlor, yellow soda ash are the raw and auxiliary materials of electrolysis production sodium hydroxide, but, hydrazine and ammonia etc. exist because containing the material of ammonia nitrogen, contain the alkali salt slag and in electrolytic process, can produce nitrogen trichloride, nitrogen trichloride is a kind of explosive substance, and affects safety production should strictly be controlled in suitability for industrialized production, the undressed alkali salt slag that contains can not be directly as the sodium chloride electrolysis raw material, and this has just limited the use that contains the alkali salt slag.Therefore, the ammonia nitrogen of removing wherein as economically viable mode how is to contain the key link that the alkali salt slag is effectively recycled.In the prior art, commonly used to remove ammonia nitrogen technology be the calcination method, promptly is to carry out calcination and make material decomposition, the volatilization that contains ammonia nitrogen containing the alkali salt slag, and the resulting alkali salt slag that contains promptly can be used as former, the auxiliary material of electrolysis, but its technological operation complexity, and facility investment is big.On the other hand, use this method will contain the preheating of alkali salt slag earlier, energy consumption is big, and in warm, containing hydrazine hydrate contained in the alkali salt slag can be discharged in the atmosphere contaminate environment with gas form.
Chinese patent 200510021859.1 discloses a kind of urea, clorox, sodium hydroxide oxidation style used and has produced the recovery and treatment method of hydrazine hydrate to the by product in the evaporative process, it comprises the separating step of slurrying step, salt slurry and alkali slurry, the treatment step of salt slurry, the treatment step and the mother liquor reuse slurrying step of alkali slurry, this invention is adopted saline and alkaline with after the fractional separation after the hot water slurrying, to reclaim solid salt and directly change into salt solution, and obtain refined brine after the processing and return electrolyzer.But this treatment process is just simply transferred to the part ammonia nitrogen in the salt slag in the mother liquor with hot water, repeatedly turns back in the hydrazine hydrate vapo(u)rization system after the circulation again, and total ammonium can't reach the requirement of electrolysis with the total ammonium≤15ppm of salt still up to 80ppm in the salt solution after the processing.
Application number is that 00112969.4 Chinese patent has proposed a kind of method of removing ammonia nitrogen, this method is by repeatedly embathing the displacement hydrazine hydrate salt mud with the caustic soda soln that contains saturated sodium-chloride, nitrogenous substances in the salt slurry is separated with solid matter, there is following shortcoming in this method: the one, and complex process, efficient is low; The 2nd, mother liquor solubility is low, increases steam consumption after returning vapo(u)rization system, and the hydrazine hydrate cost raises; The 3rd, the caustic soda soln that contains saturated sodium-chloride that adds is brought sodium-chlor again into, increases the salt amount of adopting of vapo(u)rization system, influences hydrazine hydrate output.
Application number is a kind of method with the nitrogenous class material of hydrazine class reductibility in the saline and alkaline mud of hypochlorite heated oxide of Chinese patent proposition of 01108544.4, there is following shortcoming in this method: the one, and the clorox that adds needs preparation in addition, both consumed caustic soda, consumed chlorine again, the processing cost height; The 2nd, it is unprocessed to produce a kind of toxic gas of chloramines that cries in the reaction process, influences environment, health risk.
In sum, the whole bag of tricks of the prior art or ammonia nitrogen can not reach the standard-required of production of caustic soda, or fail to make full use of resource, cost height when reaching standard-required, no economic feasibility, or having the new three wastes to produce, technology awaits further simplification, further improves in the no new three wastes generation of realization with aspect reducing cost.
Summary of the invention
The object of the present invention is to provide a kind of Wyler's process hydrazine hydrate evaporation by-product to contain ammonia nitrogen removal method in the alkali salt slag; it can make hydrazine hydrate evaporation by-product after the processing contain the alkali salt slag to reach caustic soda electrolysis salt solution requirement; realize that hydrazine hydrate evaporation by-product contains the recycling of alkali salt slag, makes full use of resource, the protection environment; plant investment is little; technology is simple, and is easy to operate, and the no new three wastes produce; cost is low, has economic feasibility.
Technical scheme of the present invention is:
A kind of Wyler's process hydrazine hydrate evaporation by-product contains the ammonia nitrogen removal method in the alkali salt slag, and its production stage is as follows: earlier hydrazine hydrate is evaporated by-product and contain the alkali salt slag and be dissolved in water and make crude brine; Detect the mass concentration of sodium hydroxide, yellow soda ash and ammonia nitrogen in the determining step 1 gained crude brine solution; Prepare clorox to the logical chlorine of crude brine, after the ammonia nitrogen mass concentration in the crude brine solution drops to below the 15PPm, remove excessive clorox; Obtain the salt solution of ammonia-nitrogen content less than 15PPm.
As to further improvement of the present invention, the mass concentration of sodium-chlor is 250～280g/l in the described crude brine.
As to further improvement of the present invention, the temperature of reaction of described logical chlorine reaction is controlled at 20～80 ℃, and the reaction times is 14～16 hours.
As to further improvement of the present invention, described method of removing excessive clorox is to add an amount of sulphite according to the clorox mass concentration in the crude brine solution.
As to further improvement of the present invention, described ammonia nitrogen mass concentration is carried out sedimentation less than the salt solution of 15PPm and is handled, and removes insoluble impurities in the salt solution, obtains being fit to the salt solution that caustic soda electrolysis is used.
As to further improvement of the present invention, the described settling time is 4～5 hours.
As to further improvement of the present invention, the logical chlorine reaction institute of described crude brine expellant gas absorbs by device for absorbing tail gas, and absorption liquid is a service water.
Principal reaction mechanism of the present invention is: chlorine and sodium hydroxide, yellow soda ash reaction generate clorox, and clorox and ammonia nitrogen reaction generate nitrogen, chloramines, react as follows:
2NaOH+Cl
2→NaClO+NaCl+H
2O
2Na
2CO
3+Cl
2+H
2O→2NaHCO
3+NaClO+NaCl
NH
3+NaClO→NH
2CL↑+NaOH
N
2H
4·H
2O+2NaClO→N
2↑+3H
2O+2NaCl
Beneficial effect of the present invention is:
The present invention compared with prior art has the following advantages: the present invention utilizes chlorine to generate clorox with sodium hydroxide, the yellow soda ash reaction in the salt slag, clorox generates nitrogen, chloramines with the ammonia nitrogen reaction again, gas such as nitrogen, chloramines volatilizees from salt solution, realizes removing of ammonia nitrogen.Compare with Chinese patent 200510021859.1, the present invention adopts the chemical process removal of ammonia and nitrogen, has characteristics such as technology is simple, ammonia nitrogen removal is effective, handles the mass concentration≤15ppm of total ammonium in the salt solution of back, can reach the requirement that caustic soda electrolysis is used.Compare with Chinese patent 00112969.4, salt solution after the present invention handles can directly use for caustic soda, do not have any material and return the hydrazine hydrate production system, mother liquor returns production system after no a large amount of processing, avoid bringing into a large amount of moisture content and sodium-chlor, the steam consumption when not increasing evaporation, the salt amount of adopting in the evaporation step does not increase yet, do not influence the ordinary production of hydrazine hydrate production, its output and energy consumption are not had influence.Compare with Chinese patent 01108544.4, the present invention makes full use of the sodium hydroxide, yellow soda ash and the chlorine reaction that contain in the alkali salt slag and generates clorox, do not need to consume in addition caustic soda, cost is lower, increased device for absorbing tail gas simultaneously, absorb the toxic gas that produces in the treating processes, avoided secondary pollution.
In a word; the present invention can make hydrazine hydrate evaporation by-product contain the brinish requirement that the alkali salt slag reaches the caustic soda electrolysis use after treatment; realization comprehensively recyles hydrazine hydrate evaporation by-product and contains the alkali salt slag, makes full use of resource, the protection environment; invest little; technology is simple, and is easy to operate, and the no new three wastes produce; cost is low, has economic feasibility.
Embodiment
Below in conjunction with embodiment the present invention is described in further detail, but the present invention has more than and is limited to these embodiment.
Embodiment 1:
Prepare hydrazine hydrate by ordinary method of the prior art, at first 30% caustic soda put into the diluted alkaline Preparation tank, add certain amount of industrial water again, with pump constantly circulation mix, the diluted alkaline that is mixed with the sodium hydroxide mass concentration and is after 22～24% is stand-by; Service water is put into urea liquid Preparation tank again, under agitation added solid urea and catalyzer, it is solution for later use behind 310～340g/l that solid urea is dissolved into mass concentration; Then diluted alkaline is sent in the sodium hypochlorite reaction device by certain flow, fed chlorine, with-5～5 ℃ of chilled brines coolings, control reaction temperature is below 30 ℃, makes that to contain available chlorine be 8～12% chlorine bleach liquor.With pump chlorine bleach liquor and urea liquid are mixed the back contains hydrazine hydrate with steam heating to 100～110 ℃ reaction generation thick solution by a certain percentage, the thick solution of hydrazine hydrate is cooled to＜sends in the crystallization kettle after 50 ℃ with recirculated water then, with＜cooling of-5 ℃ chilled brine, after temperature was reduced to 0 ℃, centrifugation went out in the thick hydrazine hydrate solution 70% yellow soda ash.Send in the pump feed evaporator and evaporate removing the thick solution of hydrazine hydrate behind the yellow soda ash, after water and the hydrazine hydrate evaporation, the Chemical Composition mass percent that contains the alkali salt slag that obtains is as follows:
Sodium-chlor: 65～70% yellow soda ash: 10～15% caustic soda: 3～4%
N
2H
4H
2O:0.5～0.6% surplus is 12～20% to be water and other trace impurity.
Embodiment 2:
A kind of Wyler's process hydrazine hydrate evaporation by-product contains the ammonia nitrogen removal method in the alkali salt slag, and the hydrazine hydrate evaporation by-product of getting embodiment 1 method gained contains the alkali salt slag, and its Chemical Composition is as follows:
Sodium-chlor: 65% yellow soda ash: 15% caustic soda: 3%
N
2H
4H
2All the other 16.5% are water and other trace impurity for O:0.5%.
Above-mentioned salt slag is handled by following production stage:
Step 1: 1000kg hydrazine hydrate by-product is contained the alkali salt slag be made into 250g/l salt solution with the service water water dissolution;
Step 2: detect in step 1 solution sodium hydroxide, the total mass concentration of yellow soda ash and be 4% and the ammonia nitrogen mass concentration be 2000PPm;
Step 3: to the logical equably chlorine of saturated crude brine of step 1, control reaction temperature is 20 ℃;
Step 4: gases such as the chloramines of discharge absorb by device for absorbing tail gas;
Step 5: logical chlorine after 16 hours the ammonia nitrogen mass concentration reduce to 14.5PPm, detecting the clorox mass concentration is 3.0g/l, adds 15Kg sodium sulfate and removes excessive clorox;
Step 6:, remove insoluble impurities in the salt solution and obtain being fit to the salt solution that caustic soda electrolysis is used with salt solution sedimentation 4 hours.
Embodiment 3:
A kind of Wyler's process hydrazine hydrate evaporation by-product contains the ammonia nitrogen removal method in the alkali salt slag, and the hydrazine hydrate evaporation by-product of getting embodiment 1 method gained contains the alkali salt slag, and its Chemical Composition is as follows:
Sodium-chlor: 68% yellow soda ash: 13% caustic soda: 4%
N
2H
4H
2All the other 14.6% are water and other trace impurity for O:0.4%.
Above-mentioned salt slag is handled by following production stage:
Step 1: 1000kg hydrazine hydrate by-product is contained the alkali salt slag be made into 270g/l salt solution with the service water water dissolution;
Step 2: detect in step 1 solution sodium hydroxide, the total mass concentration of yellow soda ash and be 4.5% and the ammonia nitrogen mass concentration be 1900PPm;
Step 3: to the logical equably chlorine of saturated crude brine of step 1, control reaction temperature is 50 ℃;
Step 4: gases such as the chloramines of discharge absorb by device for absorbing tail gas;
Step 5: logical chlorine after 15 hours ammonia-nitrogen content reduce to 13PPm, detecting the clorox mass concentration is 4.0g/l, adds the 20Kg S-WAT and removes excessive clorox;
Step 6:, remove insoluble impurities in the salt solution and obtain being fit to the salt solution that caustic soda electrolysis is used with salt solution sedimentation 5 hours.
Embodiment 4:
A kind of Wyler's process hydrazine hydrate evaporation by-product contains the ammonia nitrogen removal method in the alkali salt slag,, the hydrazine hydrate evaporation by-product of getting embodiment 1 method gained contains the alkali salt slag, and its Chemical Composition is as follows:
Sodium-chlor: 70% yellow soda ash: 10% caustic soda: 4%
N
2H
4H
2All the other 15.5% are water and other trace impurity for O:0.5%.
Above-mentioned salt slag is handled by following production stage:
Step 1: 1000kg hydrazine hydrate by-product is contained the alkali salt slag be made into 280g/l salt solution with the service water water dissolution;
Step 2: detect in step 1 solution sodium hydroxide, the total mass concentration of yellow soda ash and be 3.5% and the ammonia nitrogen mass concentration be 2200PPm;
Step 3: to the logical equably chlorine of saturated crude brine of step 1, control reaction temperature is 80 ℃;
Step 4: gases such as the chloramines of discharge absorb by device for absorbing tail gas;
Step 5: logical chlorine after 14 hours the ammonia nitrogen mass concentration reduce to 10PPm, detecting the clorox mass concentration is 2.0g/l, adds the 10Kg S-WAT and removes excessive clorox;
Step 6:, remove insoluble impurities in the salt solution and obtain being fit to the salt solution that caustic soda electrolysis is used with salt solution sedimentation 5 hours.
Embodiment 5:
A kind of Wyler's process hydrazine hydrate evaporation by-product contains the ammonia nitrogen removal method in the alkali salt slag, and the hydrazine hydrate evaporation by-product of getting embodiment 1 method gained contains the alkali salt slag, and its Chemical Composition is as follows:
Sodium-chlor: 68% yellow soda ash: 13% caustic soda: 4%
N
2H
4H
2All the other 14.6% are water and other trace impurity for O:0.4%.
Above-mentioned salt slag is handled by following production stage:
Step 1: 1000kg hydrazine hydrate by-product is contained the alkali salt slag be made into 270g/l salt solution with the service water water dissolution;
Step 2: detect in step 1 solution sodium hydroxide, the total mass concentration of yellow soda ash and be 4.5% and ammonia nitrogen mass concentration 1900PPm;
Step 3: to the logical equably chlorine of saturated crude brine of step 1, control reaction temperature is 50 ℃;
Step 4: gases such as the chloramines of discharge absorb by device for absorbing tail gas;
Step 5: logical chlorine after 15 hours ammonia-nitrogen content reduce to 13PPm, detecting the clorox mass concentration is 4.0g/l, adds the 25Kg potassium sulfite and removes excessive clorox;
Step 6:, remove insoluble impurities in the salt solution and obtain being fit to the salt solution that caustic soda electrolysis is used with salt solution sedimentation 5 hours.
Claims (7)
1. Wyler's process hydrazine hydrate evaporation by-product contains the ammonia nitrogen removal method in the alkali salt slag, it is characterized in that:
Its production stage is as follows: earlier hydrazine hydrate is evaporated by-product and contain the alkali salt slag and be dissolved in water and make crude brine; Detect the mass concentration of determining sodium hydroxide, yellow soda ash and ammonia nitrogen in the gained crude brine solution; Generate clorox to the logical chlorine reaction of crude brine, after the ammonia-nitrogen content in the crude brine solution drops to mass concentration and is lower than below the 15PPm, remove excessive clorox, obtain the salt solution of ammonia nitrogen mass concentration less than 15PPm.
2. Wyler's process hydrazine hydrate evaporation by-product according to claim 1 contains the ammonia nitrogen removal method in the alkali salt slag, and it is characterized in that: the mass concentration of sodium-chlor is 250～280g/l in the described crude brine.
3. Wyler's process hydrazine hydrate evaporation by-product according to claim 1 contains the ammonia nitrogen removal method in the alkali salt slag, and it is characterized in that: the temperature of reaction of described logical chlorine reaction is controlled at 20～80 ℃, and the reaction times is 14～16 hours.
4. Wyler's process hydrazine hydrate evaporation by-product according to claim 1 contains the ammonia nitrogen removal method in the alkali salt slag, and it is characterized in that: described method of removing excessive clorox is to add an amount of sulphite according to the clorox mass concentration in the crude brine solution.
5. Wyler's process hydrazine hydrate evaporation by-product according to claim 1 contains the ammonia nitrogen removal method in the alkali salt slag, it is characterized in that: described ammonia nitrogen mass concentration is carried out the sedimentation processing less than the salt solution of 15PPm, remove insoluble impurities in the salt solution, obtain being fit to the salt solution that caustic soda electrolysis is used.
6. Wyler's process hydrazine hydrate evaporation by-product according to claim 1 contains the ammonia nitrogen removal method in the alkali salt slag, and it is characterized in that: the described settling time is 4～5 hours.
7. Wyler's process hydrazine hydrate evaporation by-product according to claim 1 contains the ammonia nitrogen removal method in the alkali salt slag, it is characterized in that: the logical chlorine reaction institute of described crude brine expellant gas absorbs by device for absorbing tail gas, and absorption liquid is a service water.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2010105478346A CN102040197B (en) | 2010-11-17 | 2010-11-17 | Method for removing ammonia nitrogen in hydrazine hydrate evaporation byproduct residues containing alkali salt by utilizing urea method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2010105478346A CN102040197B (en) | 2010-11-17 | 2010-11-17 | Method for removing ammonia nitrogen in hydrazine hydrate evaporation byproduct residues containing alkali salt by utilizing urea method |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN102040197A true CN102040197A (en) | 2011-05-04 |
| CN102040197B CN102040197B (en) | 2012-10-31 |
Family
ID=43906792
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2010105478346A Expired - Fee Related CN102040197B (en) | 2010-11-17 | 2010-11-17 | Method for removing ammonia nitrogen in hydrazine hydrate evaporation byproduct residues containing alkali salt by utilizing urea method |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN102040197B (en) |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104817098A (en) * | 2015-04-15 | 2015-08-05 | 杭州海虹精细化工有限公司 | Industrial by-product high ammonia-nitrogen sodium chloride treatment method |
| CN107001076A (en) * | 2014-11-26 | 2017-08-01 | 三菱重工环境·化学工程株式会社 | ammonia treatment system |
| CN109534361A (en) * | 2018-12-19 | 2019-03-29 | 青海盐湖工业股份有限公司 | A method of purifying sodium chloride from by-product salt-mixture |
| CN111233126A (en) * | 2020-03-30 | 2020-06-05 | 西北民族大学 | Treatment method of tricyclazole production wastewater |
| CN111485247A (en) * | 2020-05-31 | 2020-08-04 | 湖南申联环保科技有限公司 | Resourceful treatment device and method for high-chlorine organic hazardous waste incineration fly ash |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1322684A (en) * | 2001-06-15 | 2001-11-21 | 赖中胜 | Method of eliminating nitrogenous matters from hydrazine hydrate saline-alkali mud |
| CN1686856A (en) * | 2005-04-22 | 2005-10-26 | 宜宾天原股份有限公司 | Method of treating wastewater containing salt for producing hydrazine hydrate by carbamide method |
| CN101058468A (en) * | 2006-04-18 | 2007-10-24 | 潍坊亚星集团有限公司 | Method of processing hydrazine hydrate waste water by ketone linking nitrogen method |
-
2010
- 2010-11-17 CN CN2010105478346A patent/CN102040197B/en not_active Expired - Fee Related
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1322684A (en) * | 2001-06-15 | 2001-11-21 | 赖中胜 | Method of eliminating nitrogenous matters from hydrazine hydrate saline-alkali mud |
| CN1686856A (en) * | 2005-04-22 | 2005-10-26 | 宜宾天原股份有限公司 | Method of treating wastewater containing salt for producing hydrazine hydrate by carbamide method |
| CN101058468A (en) * | 2006-04-18 | 2007-10-24 | 潍坊亚星集团有限公司 | Method of processing hydrazine hydrate waste water by ketone linking nitrogen method |
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107001076A (en) * | 2014-11-26 | 2017-08-01 | 三菱重工环境·化学工程株式会社 | ammonia treatment system |
| CN104817098A (en) * | 2015-04-15 | 2015-08-05 | 杭州海虹精细化工有限公司 | Industrial by-product high ammonia-nitrogen sodium chloride treatment method |
| CN109534361A (en) * | 2018-12-19 | 2019-03-29 | 青海盐湖工业股份有限公司 | A method of purifying sodium chloride from by-product salt-mixture |
| CN111233126A (en) * | 2020-03-30 | 2020-06-05 | 西北民族大学 | Treatment method of tricyclazole production wastewater |
| CN111233126B (en) * | 2020-03-30 | 2022-05-20 | 西北民族大学 | Treatment method of tricyclazole production wastewater |
| CN111485247A (en) * | 2020-05-31 | 2020-08-04 | 湖南申联环保科技有限公司 | Resourceful treatment device and method for high-chlorine organic hazardous waste incineration fly ash |
Also Published As
| Publication number | Publication date |
|---|---|
| CN102040197B (en) | 2012-10-31 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN108046295B (en) | Method for producing sodium bicarbonate and ammonium sulfate by using sodium sulfate solution | |
| WO2021227438A1 (en) | Method for co-producing sodium bicarbonate and ammonium sulfate from sodium sulfate | |
| CN102040197B (en) | Method for removing ammonia nitrogen in hydrazine hydrate evaporation byproduct residues containing alkali salt by utilizing urea method | |
| CN112850745B (en) | Method for recycling waste incineration fly ash | |
| CN109019638B (en) | Mother liquor treatment method for preparing sodium carbonate by taking mirabilite as raw material | |
| US20230103792A1 (en) | Soda ash and sodium bicarbonate production method | |
| CN105000579A (en) | Technology for combined production of sodium carbonate and ammonium chloride through sodium sulfate type brine thermal cycle method | |
| CN112723391B (en) | Process for co-producing soda ash and calcium sulfate from ammonium bicarbonate and glauberite tailings | |
| CN102408359A (en) | Clean production method of azodicarbonamide | |
| CN109592699B (en) | Preparation method of battery-grade lithium hydroxide | |
| CN100389892C (en) | Recovering treatment of hydrated hydrazine by-product saline-alkali by urea method | |
| CN112250049B (en) | Separation method of hydrazine hydrate byproduct saline-alkali by urea method | |
| CN114180601A (en) | Green low-carbon process for producing sodium carbonate and caustic soda from waste salt and waste residues | |
| CN109928408A (en) | The method and system of ammonia is recycled from potassium nitrate process by-product ammonium chloride | |
| CN102491559A (en) | Treatment method for urea-method hydrazine hydrate recovered saline water | |
| US5288472A (en) | Process for the recovery of the sodium hydroxide and sodium chloride from the effluent of a diaphragm cell as solid sodium bicarbonate | |
| CN106044714A (en) | Integrated ClO2 preparation system with relatively independent processes of electrolysis and ClO2 preparation | |
| CN103172090A (en) | Process for producing sodium bicarbonate | |
| CN104788346A (en) | Biurea production process through urea method | |
| CN115353125A (en) | Preparation method of sodium carbonate | |
| CN103980214A (en) | Method for treating waste gas and wastewater in trichloroisocyanuric acid production process | |
| CN104876243A (en) | Cleaning method of biurea mother liquid | |
| CN101786643B (en) | Method for comprehensively utilizing byproduct salt and alkali waste in production of hydrazine hydrate by urea process | |
| CN219517849U (en) | Valuable byproduct resource recycling system in foaming agent production | |
| CN219518808U (en) | Green chlorine hydrogen internal consumption absorption system in foaming agent production |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20121031 Termination date: 20141117 |
|
| EXPY | Termination of patent right or utility model |