CN103771646A - Method for processing wastewater generated during titanium-silicon molecular sieve production process - Google Patents
Method for processing wastewater generated during titanium-silicon molecular sieve production process Download PDFInfo
- Publication number
- CN103771646A CN103771646A CN201210395243.0A CN201210395243A CN103771646A CN 103771646 A CN103771646 A CN 103771646A CN 201210395243 A CN201210395243 A CN 201210395243A CN 103771646 A CN103771646 A CN 103771646A
- Authority
- CN
- China
- Prior art keywords
- hts
- value
- factory effluent
- treatment
- cod
- 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
- Activated Sludge Processes (AREA)
- Treatment Of Water By Oxidation Or Reduction (AREA)
Abstract
The invention discloses a method for processing wastewater generated during the titanium-silicon molecular sieve production process. The method comprises the following steps: adjusting the pH value of wastewater generated during the titanium-silicon molecular sieve production process to the alkaline region, evaporating the wastewater which has been adjusted the pH value, condensing the steam, adjusting the pH value of the condensed steam to a range of 6 to 9, carrying out a biochemical treatment on the condensed steam, and carrying out a burying treatment or a burning treatment on the residual condensed steam. The method for processing wastewater generated during the titanium-silicon molecular sieve production process can effectively process the wastewater generated during the titanium-silicon molecular sieve production process.
Description
Technical field
The present invention relates to a kind for the treatment of process of HTS factory effluent.
Background technology
HTS is a kind of high value added product, expensive.HTS synthetic and as the successful Application of organism catalyst for selective oxidation, is considered to a milestone in molecular sieve catalytic eighties field.Research Institute of Petro-Chemical Engineering adopts low temperature plastic, high temperature crystallization and resets the synthetic titanium-silicon molecular sieve catalysts of new technology such as modification the oxidizing reaction performance that has improved molecular sieve, has solved that HTS is syntheticly difficult to repetition, reactive behavior is difficult for stable problem.Adopt this technology Hunan Jianchang Petrochemical Co., Ltd to build up the HTS manufacture gasifying device of 200 tons/year, this molecular sieve catalyst has obtained application in the techniques such as cyclohexanone oxamidinating, has good economic benefit.
The waste water producing in the production process of HTS is larger with conventional molecular sieve factory effluent difference, and outstanding feature is that generation is low, organic content is high, and the partial organic substances containing in waste water is killed microorganism or inhibition effect, and biodegradability is poor.Simultaneously organonitrogen in waste water, ammonia nitrogen, silicone content are higher.In HTS factory effluent, directly discharge meeting brings great impact to existing biochemical treatment apparatus, and processing is separately comparatively desirable selection.
Report for the treatment process of molecular sieve catalytic agent production waste water in existing document has as follows:
CN1948191A disclose a kind of by waste water to producing harmful silica gel or silicon oxide, sodium salt and suspended substance removal, the ammonia and the clean water that in waste water, have recovery value are back to use to the catalyst production waste water treatment process in production technique.Method reuse water after treatment through this patent application can directly discharge or reuse, eliminate the environmental pollution that catalyst production waste water produces, water after treatment is back to use in production, reclaims the ammonia in ammonia nitrogen waste water simultaneously, produced good economic benefit and environmental benefit.But the core process of the method is to adopt membrane technique, removes mainly for inorganic pollutant in water, is not suitable for the processing of the waste water that organic pollutants concentration is higher, this technique is had relatively high expectations to the fineness of operational administrative simultaneously, and processing cost is higher.
CN1078872A discloses the recovery and treatment method of suspended substance in a kind of catalyst production waste water, and the method adopts millipore filtration technology, and the suspended substance in waste water reclaims the Catalyst Production process that is used under the state that does not add any medicament.In waste water after filtration, concentration of suspension can be down to below 200ppm by 1500-5000ppm.Adopt the method for this patent application can improve the production yield of catalyzer, reduce the suspended substance of catalyst production waste water treatment plant and process load, reduce the working cost of waste water treatment plant.But the method is mainly for the suspended substance in catalyst production waste water, adopt millipore filtration technology to remove, can not remove the dissolubility pollutant in water, thereby not be suitable for the processing of HTS factory effluent.
" biological treatment of Catalyst Production process ammonia-containing water " (Industrial Catalysis the 16th volume o. 11th in 2008, Gao Huijie, Li Yuansheng etc.) in reported with cultivate nitrifier to Catalyst Production process discharge ammonia-containing water process, continuous reaction apparatus adds after thalline, hydraulic detention time is 17.5h, and water outlet ammonia nitrogen can be lower than 10mgL
-1, ammonia nitrogen removal frank is 95%.Result shows, the bacterial classification of preservation is activity recovery after 2-7 days adapt to, can be by ammonia nitrogen concentration lower than 1500mgL
-1catalyst production waste water deamination to being less than 10mgL
-1.But this treatment process focuses on removing ammonia nitrogen in waste water, and in the factory effluent of oil refining molecular sieve catalyst, chemical oxygen demand (COD) (COD) is not high, and good biodegradability, can directly process by the method for biochemical treatment.And the COD of HTS factory effluent is higher, biodegradability is poor, can not directly adopt the method for biochemical treatment to process.Therefore, the treatment process of this molecular sieve catalytic agent production waste water not being suitable for is processed HTS factory effluent.
Summary of the invention
The object of the invention is the treatment process in order to overcome existing molecular sieve catalytic agent production waste water and be not suitable for the defect that HTS factory effluent is processed, a kind for the treatment of process of HTS factory effluent is provided.
The invention provides a kind for the treatment of process of HTS factory effluent, the method comprises: the pH value of described HTS factory effluent is adjusted to alkalescence, to regulate the waste water obtaining after pH value to evaporate, the pH value of the distillate that evaporation is obtained is adjusted to 6-9, then carry out biochemical treatment, the evaporation raffinate that evaporation is obtained carries out landfill disposal or burning disposal.
The treatment process of HTS factory effluent according to the present invention, after being adjusted to alkalescence, the pH value of HTS factory effluent evaporates, can significantly reduce the chemical oxygen demand (COD) (COD) of distillate, and significantly improve the ratio (B/C) of biochemical oxygen demand (BOD) (BOD) and chemical oxygen demand (COD) (COD), make distillate there is good biodegradability, thereby can effectively process distillate in follow-up biochemical treating processes; The evaporation raffinate obtaining for evaporation, follow-up landfill disposal and burning disposal process can realize effectively to be processed it, and because the volume of evaporation raffinate greatly reduces with respect to HTS factory effluent, therefore follow-up landfill disposal and burning disposal process can not cause higher processing load and processing cost.Therefore, the treatment process of HTS factory effluent according to the present invention can realize effectively to be processed described HTS factory effluent, thereby can avoid the impact of HTS factory effluent to conventional Sewage treatment systems.
Other features and advantages of the present invention are described in detail the embodiment part subsequently.
Embodiment
Below the specific embodiment of the present invention is elaborated.Should be understood that, embodiment described herein only, for description and interpretation the present invention, is not limited to the present invention.
The treatment process of HTS factory effluent according to the present invention comprises: the pH value of described HTS factory effluent is adjusted to alkalescence, to regulate the waste water obtaining after pH value to evaporate, the pH value of the distillate that evaporation is obtained is adjusted to 6-9, then carry out biochemical treatment, the evaporation raffinate that evaporation is obtained carries out landfill disposal or burning disposal.
In the present invention, described HTS factory effluent can be the waste water producing in conventional HTS production process.Conventionally, the organic content in described HTS factory effluent is higher, makes its COD higher, is generally greater than 15000mg/L, for example 21000-40000mg/L, and B/C is less than 0.1, for example 0.01-0.08, biodegradability is poor.Thereby biochemical processing method cannot directly be processed described HTS factory effluent.In addition, consider that biochemical processing method is the relatively low method of cost in numerous method of wastewater treatment.For this reason, the present inventor attempts HTS factory effluent to carry out pre-treatment to improve its biodegradability.Through after many trials, the present inventor is surprised to find that, then evaporates by the pH value of HTS factory effluent is adjusted to alkalescence, and the distillate that evaporation obtains has good biodegradability, thereby distillate can carry out biochemical treatment, thereby complete the present invention.
In described method of the present invention, in order as much as possible described HTS factory effluent to be evaporated, and guarantee that distillate meets the requirement of biochemical treatment, and preferably the pH value of described HTS factory effluent is adjusted to more than 10, be further preferably adjusted to 10.5-12.5.Regulating the reagent of pH value here, can be sodium carbonate and/or sodium hydroxide.
In described method of the present invention, the process that regulates the waste water obtaining after pH value to evaporate can be implemented in the evaporation unit of various routines.Under preferable case, in order to save energy consumption, described evaporative process is carried out in multiple-effect evaporator.Described multiple-effect evaporator can comprise 2-10 vaporizer, most preferably comprises 2-4 vaporizer.Compared with traditional evaporation unit, use and comprise that 2 single-effect evaporators of two vaporizers can save approximately 50% energy, and the number of vaporizer in multiple-effect evaporator is more, the energy consumption in evaporative process is lower, and the energy of saving is more.
In described method of the present invention, the volume of described distillate can be the 80-99% of the volume of described HTS factory effluent, is preferably 90-97%.
In described method of the present invention, the B/C of described distillate is higher, is generally more than 0.15, is preferably more than 0.3, more preferably 0.35-0.65.Described distillate can directly be carried out separately biochemical treatment, also can carry out biochemical treatment with after other waste water mixes.Described other waste water can be the waste water that can carry out biochemical treatment, as oil refining molecular sieve catalytic agent production waste water, can be also the waste water that can not carry out biochemical treatment, as HTS factory effluent.Carry out biochemical treatment after described distillate is mixed with the waste water (as HTS factory effluent) that can not carry out biochemical treatment time, need to guarantee that the COD of mixed waste water and B/C meet the requirement of biochemical processing method.
In described method of the present invention, before described distillate is carried out to biochemical treatment, preferably the pH value of described distillate is adjusted to 7-8.Regulating the reagent of pH value here, can be at least one in hydrochloric acid, sulfuric acid and nitric acid.
In described method of the present invention, the method of described biochemical treatment can be the various conventional biochemical processing methods that use in field of waste water treatment, for example, can be at least one in activated sludge process, Gas biological filter (BAF), biological contact oxidation process, membrane bioreactor, bio-disc system, trickling filter method and fluidized-bed reactor method.
Described activated sludge process can be the conventional activated sludge process using in this area, refer in the aeration tank of artificial oxygenation, utilize active sludge to remove the organism in sewage, then make mud separate with water, most of mud is back to aeration tank again, and the method that remainder mud is discharged.Described active sludge is the flock being formed by the organic and inorganic nitrogen solids coagulation in multiple aerobic microbiological and amphimicrobe (can contain a small amount of anaerobion) and sewage.The operational condition of described activated sludge process can comprise: temperature is 10-35 ℃, and mud age is 3-5d, and sludge loading is 0.2-0.4kgBOD
5/ (kgMLSSd), volume load is 0.3-0.6kgBOD
5/ (m
3d), suspended solids (MLSS) concentration is 1500-3000mg/L, and the treatment time is 4-20h, and reflux ratio is 0.25-0.5.In the present invention, BOD
5refer to 5 days biochemical oxygen demand (BOD)s.
Described Gas biological filter (BAF) can be the conventional Gas biological filter using in this area, refer to the granule filter material in the in-built raising specific surface area of bio-reactor, so that the carrier of microbial film growth to be provided, and lower to stream or upward flow to being divided into according to the various flows of sewage, sewage flows through filter material layer from top to bottom or from bottom to top, in the blast aeration of filter material layer bottom, air is reverse with sewage or contact in the same way, makes organism in sewage by carrying out with filling surface microbial film the method that biochemical reaction is removed.Described Gas biological filter can be for example TSA biological filter process.The operational condition of described Gas biological filter can comprise: temperature is 10-35 ℃, and volume load is 3-6kgCOD/ (m
3d), air water volume ratio is 1-20:1, and the treatment time is 2-10h.In the present invention, COD refers to chemical oxygen demand (COD).
Described biological contact oxidation process can be the conventional biological contact oxidation process using in this area, in biological contact oxidation pond, to load filler, utilization is adsorbed on microbial film on filler and the oxygen of ample supply, pass through biological oxidation, the pollutant oxidation such as the organic amine in described filtrate is decomposed, thereby reach the method for the object of purification.Described biological contact oxidation process can be for example anaerobic-aerobic-aerobic three grades of biological contact oxidation process (being tri-grades of biological contact oxidation process of A-O-O).The operational condition of described biological contact oxidation process can comprise: temperature is 10-35 ℃, and volume load is 0.1-1.8kgBOD
5/ (m
3d), the treatment time is 2-24h.
Described membrane bioreactor can be the method for carrying out biochemical treatment in conventional membrane bioreactor, and described membrane bioreactor is combined into by film separation unit and biological processing unit conventionally.The operational condition of described membrane bioreactor can comprise: temperature is 10-35 ℃, and volume load is 3-10kgCOD/ (m
3d), the treatment time is 1-10h.
Described bio-disc system can be the method for carrying out biochemical treatment in conventional blodisc.The operational condition of described bio-disc system can comprise: temperature is 10-35 ℃, and volume load is 0.2-2kgCOD/ (m
3d), the treatment time is 2-20h.
Described trickling filter method can be the method for carrying out biochemical treatment in conventional trickling filter.The operational condition of described trickling filter method can comprise: temperature is 10-35 ℃, and volume load is 0.1-1kg COD/ (m
3d), the treatment time is 2-20h.
Described fluidized-bed reactor method can be the method for carrying out biochemical treatment in conventional fluidized-bed reactor.The operational condition of described fluidized-bed reactor method can comprise: temperature is 10-35 ℃, and volume load is 3-15kg COD/ (m
3d), the treatment time is 1-5h.
In described method of the present invention, the COD of the evaporation raffinate after pervaporation is very high, and conventionally 80,000mg/L to 700, between 000mg/L, has obvious pungent smell.The present inventor is surprised to find that, in the time that the pH value of described evaporation raffinate is adjusted to below 8, this evaporation raffinate can become jelly shape material, and there is no obvious smell.Therefore, in the preferred case, before described evaporation raffinate is carried out to landfill disposal or burning disposal, the pH value of described evaporation raffinate is adjusted to below 8 to more preferably 6.5-7.5.Regulating the reagent of pH value here, can be at least one in hydrochloric acid, sulfuric acid and nitric acid.
In described method of the present invention, described burning disposal and landfill disposal are the conventional implementation method of refuse process field, do not repeat them here.
The invention will be further described with comparative example by the following examples.
In the following Examples and Comparative Examples, the COD of waste water and reuse water records according to GB11914-89 method; The BOD of waste water and reuse water records according to HJ 505-2009 method; The total nitrogen content (TN) of waste water and reuse water detects according to HJ 636-2012 method; The ammonia-nitrogen content of waste water and reuse water records according to HJ 535-2009 method.
Embodiment 1
The present embodiment is for illustrating the treatment process of described HTS factory effluent of the present invention.
The water sample of HTS factory effluent: COD is 31970mg/L, and B/C is that 0.1, TN is 960.7mg/L.
The pH value of above-mentioned HTS factory effluent is adjusted to 10.7, then adopts 2 single-effect evaporators to evaporate.The volume of distillate account for evaporation before described HTS factory effluent volume 92.0%, the COD of distillate is 2963mg/L, B/C is 0.72, ammonia-nitrogen content is 345.3mg/L, TN is 466.6mg/L; The COD of evaporation raffinate is 316800mg/L, and pH value is 11.8.
The pH value of distillate is adjusted to 8, then adopts tri-grades of biological contact oxidation process of A-O-O to regulating the distillate after pH value to process, treatment condition comprise: temperature is 30 ℃, and volume load is 0.5kgCOD/ (m
3d), the treatment time is 12h.The COD<60mg/L of the reuse water obtaining after processing, ammonia nitrogen <15mg/L, meets the discharging standards of GB8978-1996.
Evaporation raffinate is carried out to burning disposal.
Comparative example 1
By Fenton oxidation method, the wastewater sample of embodiment 1 is processed, the condition of processing comprises: pH value is 5, and the dosage of hydrogen peroxide is 6000ppm, and the dosage of ferrous sulfate is 12000ppm, and the reaction times is 2 hours.Learn by mensuration, the COD of the reuse water obtaining after processing is 29970mg/L, and BOD is 1199mg/L, and B/C is 0.04, because B/C is too little, thereby is not suitable for carrying out biochemical treatment.
Comparative example 2
By wet oxidation process, the wastewater sample of embodiment 1 is processed, the condition of processing comprises: temperature of reaction is 220 ℃, reaction pressure 3.5MPa, and the reaction times is 4 hours.Learn by mensuration, the COD of the reuse water obtaining after processing is 30180mg/L, and BOD is 1509mg/L, and B/C is 0.05, because B/C is too little, thereby is not suitable for carrying out biochemical treatment.
Embodiment 2
The present embodiment is for illustrating the treatment process of described HTS factory effluent of the present invention.
The water sample of HTS factory effluent: COD is 30800mg/L, and B/C is that 0.11, TN is 940.2mg/L.
The pH value of above-mentioned HTS factory effluent is adjusted to 11.5, then adopts 3 single-effect evaporators to evaporate.The volume of distillate account for evaporation before described HTS factory effluent volume 96.0%, the COD of distillate is 2875mg/L, B/C is 0.82, ammonia-nitrogen content is 324.3mg/L, TN is 448.9mg/L; The COD of evaporation raffinate is 303600mg/L, and pH value is 12.7.
The pH value of distillate is adjusted to 7, then adopts TSA filter tank method to regulating the distillate after pH value to process, treatment condition comprise: temperature is 25 ~ 35 ℃, and volume load is 3kgCOD/ (m
3d), air water volume ratio is 10:1, and the treatment time is 8 hours.The COD<60mg/L of the reuse water obtaining after processing, ammonia nitrogen <15mg/L, meets the discharging standards of GB8978-1996.
The pH value of evaporation raffinate is adjusted to 7, then produces after waste residue mixes and make landfill disposal according to the weight ratio of 1:2 and conventional molecular sieve.
Embodiment 3
The present embodiment is for illustrating the treatment process of described HTS factory effluent of the present invention.
The water sample of HTS factory effluent: COD is 24020mg/L, and B/C is that 0.08, TN is 980.0mg/L.
The pH value of above-mentioned HTS factory effluent is adjusted to 12.5, then adopts 3 single-effect evaporators to evaporate.The volume of distillate account for evaporation before described HTS factory effluent volume 95.4%, the COD of distillate is 3240mg/L, B/C is 0.70, ammonia-nitrogen content is 202.8mg/L, TN is 288.1mg/L; The COD of evaporation raffinate is 521300mg/L, and pH value is 13.9.
The pH value of distillate is adjusted to 7.5, then adopts tri-grades of biological contact oxidation process of A-O-O to regulating the distillate after pH value to process, treatment condition comprise: temperature is 25 ~ 35 ℃, and volume load is 0.6kgCOD/ (m
3d), the treatment time is 15 hours.The COD<60mg/L of the reuse water obtaining after processing, ammonia nitrogen <15mg/L, meets the discharging standards of GB8978-1996.
The pH value of evaporation raffinate is adjusted to 7, then produces after waste residue mixes and make landfill disposal according to the weight ratio of 1:2 and conventional molecular sieve.
As can be seen here, the treatment process of HTS factory effluent according to the present invention can realize described HTS factory effluent is effectively processed.
Claims (10)
1. the treatment process of a HTS factory effluent, the method comprises: the pH value of described HTS factory effluent is adjusted to alkalescence, to regulate the waste water obtaining after pH value to evaporate, the pH value of the distillate that evaporation is obtained is adjusted to 6-9, then carry out biochemical treatment, the evaporation raffinate that evaporation is obtained carries out landfill disposal or burning disposal.
2. method according to claim 1, wherein, is adjusted to the pH value of described HTS factory effluent more than 10.
3. method according to claim 2, wherein, is adjusted to 10.5-12.5 by the pH value of described HTS factory effluent.
4. according to the method described in any one in claim 1-3, wherein, described evaporative process is carried out in multiple-effect evaporator.
5. method according to claim 4, wherein, described multiple-effect evaporator comprises 2-4 vaporizer.
6. according to the method described in any one in claim 1-3, wherein, the volume of described distillate is the volume 80-99% of described HTS factory effluent.
7. method according to claim 1, wherein, the method for described biochemical treatment is at least one in activated sludge process, Gas biological filter, biological contact oxidation process, membrane bioreactor, bio-disc system, trickling filter method and fluidized-bed reactor method.
8. method according to claim 1, wherein, described method is adjusted to 6.5-7.5 by the pH value of described evaporation raffinate before being also included in described evaporation raffinate being carried out to landfill disposal.
9. method according to claim 1, wherein, the chemical oxygen demand (COD) of described HTS factory effluent is greater than 15000mg/L, and the ratio of biochemical oxygen demand (BOD) and chemical oxygen demand (COD) is less than 0.1.
10. method according to claim 9, wherein, the chemical oxygen demand (COD) of described HTS factory effluent is 21000-40000mg/L, the ratio of biochemical oxygen demand (BOD) and chemical oxygen demand (COD) is 0.01-0.08.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201210395243.0A CN103771646B (en) | 2012-10-17 | 2012-10-17 | A kind for the treatment of process of HTS factory effluent |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201210395243.0A CN103771646B (en) | 2012-10-17 | 2012-10-17 | A kind for the treatment of process of HTS factory effluent |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN103771646A true CN103771646A (en) | 2014-05-07 |
| CN103771646B CN103771646B (en) | 2015-11-11 |
Family
ID=50564484
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201210395243.0A Active CN103771646B (en) | 2012-10-17 | 2012-10-17 | A kind for the treatment of process of HTS factory effluent |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN103771646B (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114477653A (en) * | 2022-02-24 | 2022-05-13 | 陕西煤业化工技术研究院有限责任公司 | Method and system for treating wastewater in molecular sieve production process |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101151217A (en) * | 2005-03-29 | 2008-03-26 | 住友化学株式会社 | Method for treating waste water containing oxygen-containing compound having phenol hydroxy group or carbonyl group |
| CN101585620A (en) * | 2009-06-26 | 2009-11-25 | 河北建新化工股份有限公司 | Method for comprehensively treating high salt content organic industrial wastewater |
-
2012
- 2012-10-17 CN CN201210395243.0A patent/CN103771646B/en active Active
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101151217A (en) * | 2005-03-29 | 2008-03-26 | 住友化学株式会社 | Method for treating waste water containing oxygen-containing compound having phenol hydroxy group or carbonyl group |
| CN101585620A (en) * | 2009-06-26 | 2009-11-25 | 河北建新化工股份有限公司 | Method for comprehensively treating high salt content organic industrial wastewater |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114477653A (en) * | 2022-02-24 | 2022-05-13 | 陕西煤业化工技术研究院有限责任公司 | Method and system for treating wastewater in molecular sieve production process |
Also Published As
| Publication number | Publication date |
|---|---|
| CN103771646B (en) | 2015-11-11 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN103771650B (en) | A kind for the treatment of process of coal gasification waste water | |
| CN1321069C (en) | Method of purifying fischer-tropsch derived water | |
| JP4319981B2 (en) | Purification method of Fischer-Tropsch generated water | |
| CN103466893B (en) | Sewage recycling comprehensive treatment system | |
| CN101708935B (en) | Method for treating container washing wastewater | |
| CN110639358B (en) | Resource process for synchronously removing VOCs, sulfides and ammonia sulfur in waste gas by chemical coupling and biology | |
| CN105481168A (en) | Coal gasification sewage comprehensive treatment method | |
| CN106946420A (en) | A kind of integrated conduct method of high-concentration ammonia nitrogenous wastewater | |
| CN101376550B (en) | Method for processing process waste water of dimethyl ether preparation by dehydrating methyl alcohol | |
| CN104003581A (en) | Treatment process of high-concentration degradation-resistant organic wastewater | |
| Wijerathna et al. | Imperative assessment on the current status of rubber wastewater treatment: Research development and future perspectives | |
| CN108975616A (en) | Handle the system and method for biomass pyrolytic water | |
| CN111847796A (en) | System and method for treating leachate of waste incineration plant | |
| CN105565582A (en) | Method for treatment on sewage produced through preparation of hydrogen from coal | |
| CN110590062A (en) | Method for advanced treatment of salt-containing oil refining wastewater | |
| CN112028388B (en) | Method for treating wastewater containing DMF, pyridine and pyridine derivatives | |
| CN113213714A (en) | Raw material medicine wastewater treatment process | |
| CN208857099U (en) | The system for handling biomass pyrolytic water | |
| CN103771646B (en) | A kind for the treatment of process of HTS factory effluent | |
| CN109399856A (en) | A kind of semi-coke wastewater Zero discharge treatment method based on catalytic ozonation | |
| CN116655160A (en) | Integrated purification method for separation and reaction of aged garbage leachate | |
| CN103771649B (en) | Treatment method of 1,3-propanediol production wastewater | |
| CN107188368B (en) | Advanced treatment process for kitchen waste fermentation waste liquid | |
| CN206033470U (en) | High salt sewage treatment system | |
| CN212174737U (en) | Integrated treatment system for zero discharge of domestic garbage sewage |
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 |