CN103803753A - Comprehensive recovery treatment method for H acid industrial waste water - Google Patents
Comprehensive recovery treatment method for H acid industrial waste water Download PDFInfo
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- CN103803753A CN103803753A CN201410073751.6A CN201410073751A CN103803753A CN 103803753 A CN103803753 A CN 103803753A CN 201410073751 A CN201410073751 A CN 201410073751A CN 103803753 A CN103803753 A CN 103803753A
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- 238000000034 method Methods 0.000 title claims abstract description 50
- 238000011084 recovery Methods 0.000 title claims abstract description 21
- APRRQJCCBSJQOQ-UHFFFAOYSA-N 4-amino-5-hydroxynaphthalene-2,7-disulfonic acid Chemical compound OS(=O)(=O)C1=CC(O)=C2C(N)=CC(S(O)(=O)=O)=CC2=C1 APRRQJCCBSJQOQ-UHFFFAOYSA-N 0.000 title claims abstract 20
- 239000010842 industrial wastewater Substances 0.000 title abstract description 5
- 238000000605 extraction Methods 0.000 claims abstract description 110
- 239000002351 wastewater Substances 0.000 claims abstract description 64
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 50
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims abstract description 45
- 238000001704 evaporation Methods 0.000 claims abstract description 19
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- 239000012528 membrane Substances 0.000 claims abstract description 16
- 239000003513 alkali Substances 0.000 claims abstract description 15
- 238000004519 manufacturing process Methods 0.000 claims abstract description 13
- PMZURENOXWZQFD-UHFFFAOYSA-L Sodium Sulfate Chemical compound [Na+].[Na+].[O-]S([O-])(=O)=O PMZURENOXWZQFD-UHFFFAOYSA-L 0.000 claims abstract description 10
- 238000000926 separation method Methods 0.000 claims abstract description 10
- 229910052938 sodium sulfate Inorganic materials 0.000 claims abstract description 10
- 235000011152 sodium sulphate Nutrition 0.000 claims abstract description 10
- 238000004064 recycling Methods 0.000 claims abstract description 5
- 239000003795 chemical substances by application Substances 0.000 claims description 44
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 claims description 5
- 239000002253 acid Substances 0.000 claims description 5
- 238000000108 ultra-filtration Methods 0.000 claims description 5
- 230000000536 complexating effect Effects 0.000 claims description 4
- 239000003350 kerosene Substances 0.000 claims description 4
- 235000011149 sulphuric acid Nutrition 0.000 claims description 4
- 239000001117 sulphuric acid Substances 0.000 claims description 4
- 150000003512 tertiary amines Chemical class 0.000 claims description 4
- 238000005374 membrane filtration Methods 0.000 claims description 3
- 239000012452 mother liquor Substances 0.000 claims description 2
- 238000005204 segregation Methods 0.000 claims description 2
- 239000000126 substance Substances 0.000 abstract description 15
- 238000005516 engineering process Methods 0.000 abstract description 9
- 239000007788 liquid Substances 0.000 abstract description 8
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- 229920006395 saturated elastomer Polymers 0.000 abstract description 5
- 239000002585 base Substances 0.000 abstract 2
- 230000001105 regulatory effect Effects 0.000 abstract 2
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 abstract 1
- 238000010668 complexation reaction Methods 0.000 abstract 1
- 238000001914 filtration Methods 0.000 abstract 1
- 230000004927 fusion Effects 0.000 abstract 1
- 229910052760 oxygen Inorganic materials 0.000 abstract 1
- 239000001301 oxygen Substances 0.000 abstract 1
- QPILZZVXGUNELN-UHFFFAOYSA-M sodium;4-amino-5-hydroxynaphthalene-2,7-disulfonate;hydron Chemical compound [Na+].OS(=O)(=O)C1=CC(O)=C2C(N)=CC(S([O-])(=O)=O)=CC2=C1 QPILZZVXGUNELN-UHFFFAOYSA-M 0.000 description 46
- 235000011121 sodium hydroxide Nutrition 0.000 description 15
- 239000002904 solvent Substances 0.000 description 11
- 230000008569 process Effects 0.000 description 10
- 229940056729 sodium sulfate anhydrous Drugs 0.000 description 9
- 238000010521 absorption reaction Methods 0.000 description 8
- 229960003010 sodium sulfate Drugs 0.000 description 8
- 229910017053 inorganic salt Inorganic materials 0.000 description 6
- 238000012545 processing Methods 0.000 description 6
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- 230000000694 effects Effects 0.000 description 5
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- 150000003839 salts Chemical class 0.000 description 5
- 238000004065 wastewater treatment Methods 0.000 description 5
- 239000006227 byproduct Substances 0.000 description 4
- 238000004821 distillation Methods 0.000 description 4
- 238000002156 mixing Methods 0.000 description 4
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- 229920005989 resin Polymers 0.000 description 4
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- 238000005406 washing Methods 0.000 description 3
- 239000002699 waste material Substances 0.000 description 3
- LSNNMFCWUKXFEE-UHFFFAOYSA-M Bisulfite Chemical compound OS([O-])=O LSNNMFCWUKXFEE-UHFFFAOYSA-M 0.000 description 2
- 150000007513 acids Chemical class 0.000 description 2
- 238000003763 carbonization Methods 0.000 description 2
- 239000003610 charcoal Substances 0.000 description 2
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- 239000012141 concentrate Substances 0.000 description 2
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- 238000005265 energy consumption Methods 0.000 description 2
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- -1 naphthene sulfonic acid class Chemical class 0.000 description 2
- 239000010815 organic waste Substances 0.000 description 2
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- 244000025254 Cannabis sativa Species 0.000 description 1
- UFWIBTONFRDIAS-UHFFFAOYSA-N Naphthalene Chemical compound C1=CC=CC2=CC=CC=C21 UFWIBTONFRDIAS-UHFFFAOYSA-N 0.000 description 1
- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 description 1
- 230000002378 acidificating effect Effects 0.000 description 1
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- WBZKQQHYRPRKNJ-UHFFFAOYSA-L disulfite Chemical compound [O-]S(=O)S([O-])(=O)=O WBZKQQHYRPRKNJ-UHFFFAOYSA-L 0.000 description 1
- 238000004043 dyeing Methods 0.000 description 1
- 239000000284 extract Substances 0.000 description 1
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- 239000000446 fuel Substances 0.000 description 1
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- 238000003199 nucleic acid amplification method Methods 0.000 description 1
- 239000005416 organic matter Substances 0.000 description 1
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- 239000000047 product Substances 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 230000000717 retained effect Effects 0.000 description 1
- RSIJVJUOQBWMIM-UHFFFAOYSA-L sodium sulfate decahydrate Chemical compound O.O.O.O.O.O.O.O.O.O.[Na+].[Na+].[O-]S([O-])(=O)=O RSIJVJUOQBWMIM-UHFFFAOYSA-L 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
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Landscapes
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
The invention discloses a comprehensive recovery treatment method for H acid industrial waste water, belonging to the field of an industrial waste water recovery treatment method. The comprehensive recovery treatment method comprises the steps of (1) after the pH value of H acid industrial waste water is regulated to 10-1.5, extracting by adopting a complexation extraction method so as to separate organic matters from waste water, filtering extraction water through a membrane so as to reduce the loss of an extractant, carrying out back extraction on the extractant by utilizing a 13% sodium hydroxide solution, wherein the ratio of the back-extraction oil to base is 4:1, and the recycling of the extractant and the enrichment of organic matters in the waste water can be realized; (2) after the back-extraction base liquid is saturated, directly recycling the back-extraction liquid into alkali fusion workshop section in H acid production, and further carrying out H acid production; (3) regulating the pH value of the extraction water to 6-9, concentrating and evaporating the extraction water by using MVR (Mechanical Vapor Recompression) technology, and recycling to obtain sodium sulfate. By combination use of extraction technology, membrane separation technology and MVR technology, the running cost can be saved, and the COD (Chemical Oxygen Demand) value of the evaporation water can achieve the administration standard of a sewage treatment plant in a chemical industrial park.
Description
Technical field
The invention belongs to trade effluent recovery and treatment method field, more particularly, relate to a kind of comprehensive recovery and treatment method of H acid trade effluent.
Background technology
H acid is one of important dyestuff intermediate, and in its production process, producing a large amount of naphthene sulfonic acid is class waste water.This COD value of waste water is high, colourity dark, pH=2, belongs to the organic waste water of high density, high acidity, high salinity and high chroma, can not adopt the traditional method such as biochemistry and materialization processing.How wherein organism and inorganic salt are separated, and are the difficult points in H acid waste water treatment always.
At present there are absorption method, method of enrichment, carbonization and burning method, membrane separation process, cold method, electrolytic process, chemical oxidization method, have extraction process etc. for the treatment process of this type of dye intermediate wastewater.Absorption method is divided charcoal absorption and resin absorption, and charcoal absorption is applicable to the wastewater treatment that concentration is lower, and resin absorption is to utilize resin absorption organism; Method of enrichment is suitable for processing high density, high salinity organic waste water, and shortcoming is that energy consumption is high; Carbonization and burning method are applicable to the extra high waste water of concentration, but investment is expensive, higher to fuel mass and burn operation conditional request; Membrane separation process is simple to operate, but effect is not ideal enough, and fenestra easily stops up; Electrolytic process is applicable to process the waste water of COD0.01～1g/L, and shortcoming is that power consumption is large, and metal polar plate loss is serious; The conventional ozone oxidation of chemical oxidization method and H
2o
2oxidation, Ozonation is applicable to the waste water treatment that concentration is lower, H
2o
2oxidation style is directly used in the waste liquid that concentration is high, and when processing, expense is high; Extraction process is relatively suitable for processing that toxicity is large, concentration is high, the waste water of difficult for biological degradation, selects suitable extraction agent, and treatment effect is better.So, improvement for high density, high acidity waste water can be joined together extraction and chemical treatment, can obtain good regulation effect, but abstraction technique can only be removed the organism in waste water, inorganic salt a large amount of in waste water are still still deposited, and chemical industrial park enterprise wastewater all enters the adapter of garden sewage work at present, high-salt wastewater can not enter the treatment system of garden sewage work, simultaneously direct discharge also can cause the waste of a large amount of inorganic salt, therefore, this waste water does not obtain optimum handling method always.
Deng Bing, Wang Xiangyun has inquired into complexing abstraction and has processed naphthene sulfonic acid class waste water in the research of naphthene sulfonic acid class waste water complexometric extraction, COD is still higher in the method extraction water outlet, extracting operation excess Temperature can strengthen extraction agent solubleness in water, not installing membrane separation unit additional makes extraction agent loss quantitative change large, the alkali lye of back extraction simultaneously can not be reused, cause alkali charge excessive too much with strip liquor, increase running cost, easily cause secondary pollution, and extraction water outlet need to be through processing discharge again, the a large amount of sodium sulfate that dissolve in extraction water outlet directly discharge, to environment.During what Chen Jinlong, Zhang Weiming etc. reclaimed in the purification of H acid producing waste water and resource utilize method, adopt DN-910 complexing polymeric adsorbent to realize the separating and recovering of H acid wastewater through organic matter, adsorb the reuse of water saturation metabisulfite solution to H acid, T acidleach cake washing process.Resin absorption technique complicated operation, needs very professional technician's guarantee adsorption and desorption effect.At present H acid production process does not use saturated sulphuric acid soln to carry out filter cake washing through updating, and the method do not carry out further following the tracks of and processing to washing water outlet, and the final treatment process of inorganic salt in H acid waste water is not described.
Summary of the invention
1. technical problem
Higher for the extraction water outlet COD value existing in prior art H acid Industrial Wastewater Treatment, extraction agent loss amount is large, back extraction alkali lye is too much, the problem that high-salt wastewater directly discharges, the invention provides a kind of comprehensive recovery and treatment method of H acid trade effluent, the method can realize water outlet COD value and reach chemical industrial park sewage work adapter standard, extraction agent loss amount is lower than 5/10000ths (extracting 5 tons of extraction agents of 10000 tons of waste water losses), in waste water, organism is back to use in production, and by MVR technique by-product Sodium sulfate anhydrous.min(99) (Disodium sulfate decahydrate), realize the complete qualified discharge of waste water.
2. technical scheme
A comprehensive recovery and treatment method for H acid trade effluent, the steps include:
(1) H acid trade effluent regulates behind pH value to 1.0～1.5, adopt complexing abstraction to extract, organism is separated from waste water, extraction water outlet reduces extraction agent through membrane filtration and runs off, extraction agent utilizes 13%(mass ratio) sodium hydroxide solution carries out back extraction, back extraction oil alkali is than 4:1(volume ratio), realize organic enrichment in the recycling utilization of extraction agent and waste water;
This is that organism is transferred in extraction agent, when waste water ph is effect of extracting the best between 1.0～1.5 due to how sulphonic acids generation complex reaction in acidic conditions extraction agent and H acid waste water; After extraction agent adds liquid caustic soda, pH value becomes alkalescence, how sulphonic acids generation decomplexing reacts extraction agent with H acid waste water, organism is transferred in strip liquor again, the sodium hydroxide solution (mass ratio) of employing 13% is as strip liquor, back extraction oil alkali is than 4:1, can guarantee that strip liquor reuses 20 times and reach capacity later; Extraction water outlet can realize extraction agent after ultrafiltration membrance filter, and water outlet is effective separates with extraction, and extraction agent turnover rate is controlled in 5/10000ths;
(2), after back extraction alkali lye reaches capacity, the alkaline melt workshop section of strip liquor direct reuse in producing to H acid, proceeds the production of H acid;
(3) regulate pH value to 6～9 of extraction water outlet, then by MVR technique, extraction water outlet is carried out to concentration and evaporation, reclaim and obtain sodium sulfate.
Extraction water outlet is limpid bright, there are a large amount of inorganic salt, still do not meet chemical industrial park and take over standard, and cause the waste of a large amount of inorganic salt, after adjusting pH value, by MVR technique, extraction water outlet is carried out to concentration and evaporation, recovery obtains sodium sulfate can sell acquisition economic worth outward as by-product, and evaporation water outlet reaches garden adapter standard and can directly discharge.
MVR is the energy that re-uses it self secondary steam of producing, thereby reduces a power-saving technology of the demand of the energy to external world, at present because its energy-efficient being widely used in solid-liquid separation process.
Preferably, the acid used of the acid of the H in described step (1) trade effluent adjusting pH value is industrial sulphuric acid.
Preferably, the extraction process service temperature in described step (1) is 30～40 ℃.
Preferably, the extraction agent in described step (1) is that trialkyl tertiary amine and sulfonated kerosene mix according to mass ratio 1:2.
Preferably, the membrane separation process in described step (1) adopts ultrafiltration membrance filter, and operational condition is 25～35 ℃ of temperature, pressure 0.3～0.5MPa.
Preferably, described H acid trade effluent is the H acid mother liquor that the finishing operation segregation workshop section of H acid production process produces, and H acid content is more than 3000mg/L.
Preferably, in described step (3), MVR technique is continuous operation, and evaporation concentration is than the volume ratio for 1:1～2:3(distillation amount and vinasse).
In H acid producing waste water, sodium sulfate is realized resource utilization recovery after " extraction+membrane sepn+MVR " processes, and in H acid producing waste water, organism is realized resource utilization recovery after " concentrate+reuse of extraction+back extraction is to alkaline melt workshop section " processed.
3. beneficial effect
Than prior art, the invention has the advantages that:
(1) extraction process is to utilize the extraction agent that is insoluble in water contact with waste water, makes sulfonic acid substance and extraction agent in waste water carry out physics or chemical combination, realizes organic phase transition, then passes through the chemical property of adjusting extraction agent, realizes organic transfer enrichment.MVR is the abbreviation of function of mechanical steam recompression technology (mechanical vapor recompression).Mvr is the energy that re-uses it self secondary steam of producing, thereby reduces a power-saving technology of the demand of the energy to external world.The present invention adopts extraction and MVR combination process to realize the resource utilization of H acid waste water; The present invention can be applied in H acid producing waste water industry amplification preferably, is a kind of novel process that industrialization demand, practicality are very strong that meets;
(2) the present invention employing is as aminated compounds extraction agent (trialkyl tertiary amine and sulfonated kerosene mix according to mass ratio 1:2), H acid waste water is extracted, the organism of realizing in waste water separates with water, carry out back extraction by alkali lye again and realize organism and separate with extraction agent, extraction agent recycle.Saturated strip liquor is back to use to the alkaline melt workshop section in production, realizes the recovery of H acid, make the organism in waste water be recycled utilization, reduce to greatest extent organic discharge, realize resource utilization;
(3) to have realized extraction water outlet organic content low in the present invention, contains a large amount of sodium sulfate in water outlet, after evaporation concentration, the sodium sulfate of the technical grade of purifying out can beyond sell, when bringing economic interests for enterprise, realize discharged wastewater met the national standard;
(4) the extracting process easy handling the present invention relates to, adopts membrane separation technique to reduce to greatest extent extraction agent loss and has saved running cost, and evaporation concentration adopts MVR technology, and capacity usage ratio is high, and operation simple-to-maintain is convenient;
(5) the present invention is simple to operate, running cost is low, energy consumption is low, and the H acid of recovery, Sodium sulfate anhydrous.min(99) can be sold and bring economic interests, reduces scale wastewater treatment burden.
Accompanying drawing explanation
Fig. 1 is the process flow sheet of embodiment 1.
Embodiment
Below in conjunction with accompanying drawing and specific embodiment, technical scheme of the present invention is described further.
Embodiment 1
As shown in arrow points in Fig. 1, extraction agent is stored in solvent tank 1, H acid producing waste water is stored in waste water tank, waste water tank is with heating function, when operation, waste water tank can remain on 30～40 ℃ by H acid wastewater temperature, volume pump is promoted to waste water and extraction agent in static mixer 1, waste water enters gun barrel 1 after fully mixing therein with extraction agent, while operation continuously, extraction agent is from flowing in solvent tank 2, extraction water outlet enters membrane separation unit, after membrane sepn, water outlet enters wastewater disposal basin, extraction agent after membrane sepn enters solvent tank 2, alkali lye in extraction agent in solvent tank 2 and reextraction flow container is promoted in static mixer 2 through volume pump, after fully mixing, mixed solution enters in gun barrel 2, after layering, extraction agent flows in solvent tank 1 and continues to use, saturated strip liquor enters in saturated back extraction flow container, then reuse to H acid produce in alkaline melt workshop section, continue the production of H acid.Regulate extraction water outlet pH value to 6～9 that store in wastewater disposal basin, pump in MVR vaporizer through lift pump, after evaporative crystallization, water outlet enters official website, garden, and by-product is sodium sulfate.
This example is processed the H acid waste water of certain printing and dyeing mill, and this waste water quality is in Table 1-1.
Table 1-1
| Project | pH | COD（mg/L） | H acid content (mg/L) | Total salt quantity (mg/L) |
| H acid waste water | 2～3 | 22000 | 3900 | 310000 |
This H acid producing waste water is stored in the waste water tank of 5t, volume pump pumps into 50% industrial sulphuric acid solution wherein, automatically regulate pH value to 1.0 through online pH meter, water temperature in waste water tank is remained on 30 ℃ by heating system, 1t trialkyl tertiary amine and 2t sulfonated kerosene are added in 5t solvent tank 1, two volume pumps pump into the solution in waste water tank and solvent tank 1 in static mixer 1 with 4L/min, after mixing in 5min, enter in gun barrel 1, after separating, extraction agent enters in solvent tank 1, extracting water temp is 28 ℃, pump into (employing ultra-filtration membrane) in membrane separation unit through pump, pressure reaches 0.4MPa, after membrane sepn, water outlet enters wastewater disposal basin, isolated extraction agent enters in solvent tank 2, the liquid caustic soda that is 13% by massfraction adds in 5t back extraction flow container, in solvent tank 2, the liquid caustic soda of extraction agent and back extraction flow container pumps in static mixer 2 with 4L/min and 1L/min respectively through volume pump, after mixing 5min, enter in gun barrel 2, after layering, extraction agent flows in solvent tank 1 and continues to use, back extraction alkali lye enters saturated back extraction flow container kind, enters H acid and produce alkaline melt workshop section continuation H acid production after having stored.Extraction water outlet enters in wastewater disposal basin after membrane filtration, enters MVR multi-effect evaporation system, passes into steam start vaporizer, and evaporation concentration is than being 1:1, and waste water obtains by-product sodium sulfate crystal after MVR multiple-effect evaporation is concentrated, and water outlet enters garden pipe network.Evaporation concentration effluent quality is in Table 1-2.
Table 1-2
| Project | pH | COD（mg/L） | H acid content (mg/L) | Total salt quantity (mg/L) |
| Distillation water outlet | 7.5 | 280 | — | 570 |
Known after extraction, MVR multiple-effect evaporation concentrate by table 1-2, water outlet reaches chemical industrial park sewage work completely and takes over standard.Adapter standard in chemical industrial park is in Table 1-3.
Table 1-3
| Sequence number | Project | Sewage is taken over standard |
| 1 | pH | 6-9 |
| 2 | COD | ≤500/L |
| 3 | Salinity | ≤5000mg/l |
After MVR multiple-effect evaporation is concentrated, the Sodium sulfate anhydrous.min(99) of system can reach the standard of acceptable end product completely.The quality and technical index that table 1-4 is Sodium sulfate anhydrous.min(99):
Table 1-4
Embodiment 2
The present embodiment is processed the H acid waste water of certain printworks, and this waste water quality is in Table 2-1.
Table 2-1
| Project | pH | COD（mg/L） | H acid content (mg/L) | Total salt quantity (mg/L) |
| H acid waste water | 2～3 | 20000 | 4000 | 330000 |
(1) extraction
Get the H acid waste water of 500mL, add 0.5mL industrial sulphuric acid that pH value is adjusted to 1.5, heating in water bath to 40 ℃, adds 500mL extraction agent, and waste water is evenly mixed with extraction agent, after oscillation extraction 5min, stratification 5min, lower floor extracts water temp and is reduced to 34 ℃, and extraction water outlet is held back extracting and enriching agent after ultra-filtration membrane filters under 0.5MPa, then extraction water outlet is transferred in 1000mL distilling flask, lower floor's extraction agent is retained in separating funnel.Extraction effluent quality is in Table 2-2:
Table 2-2
| Project | pH | COD（mg/L） | H acid content (mg/L) | Total salt quantity (mg/L) |
| Extraction water outlet | 3 | 300 | 12 | 330000 |
(2) back extraction
The sodium hydroxide solution that is 13% by the mass concentration configuring, heating in water bath to 35 ℃, join in separating funnel extraction agent is carried out to back extraction, oil alkali than 4:1, after oscillation extraction 5min, stratification 20min, after layering, extraction agent continues to use, alkali lye is proceeded back extraction, after alkali lye back extraction 20 times, gets back to alkaline melt workshop section in production, reclaims H acid product.
(3) evaporation concentration and Sodium sulfate anhydrous.min(99) are produced
In test, add 0.4g sodium hydroxide to regulate pH to 7.5 above-mentioned 500mL extraction water outlet, flask is placed in heating jacket, connect water distilling apparatus, evaporation concentration under the condition stirring, distill out (distillation effluent quality is in Table 2-3) after 150mL liquid, raffinate is transferred in 3 100mL furnace potes while hot, furnace pot is placed in to moisture eliminator, 105 ℃ of dry 4h, obtain content at 95.0% above Sodium sulfate anhydrous.min(99) (Sodium sulfate anhydrous.min(99) specific targets are in Table 1-4).
Table 2-3
| Project | pH | COD（mg/L） | H acid content (mg/L) | Total salt quantity (mg/L) |
| Distillation water outlet | 7.3 | 180 | — | 430 |
"-" represents lower than detection limit, known after extraction, evaporation concentration by table 2-3, and water outlet reaches chemical industrial park sewage work completely and takes over standard.Adapter standard in chemical industrial park is in Table 1-3.
The Sodium sulfate anhydrous.min(99) that present method is produced can reach the standard of acceptable end product completely.Sodium sulfate anhydrous.min(99) technology quality index is in Table 1-4.
Claims (7)
1. a comprehensive recovery and treatment method for H acid trade effluent, the steps include:
(1) H acid trade effluent regulates behind pH value to 1.0～1.5, adopt complexing abstraction to extract, organism is separated from waste water, extraction water outlet reduces extraction agent through membrane filtration and runs off, extraction agent utilizes 13% sodium hydroxide solution to carry out back extraction, back extraction oil alkali is than 4:1, realizes organic enrichment in the recycling utilization of extraction agent and waste water;
(2), after back extraction alkali lye reaches capacity, the alkaline melt workshop section of strip liquor direct reuse in producing to H acid, proceeds the production of H acid;
(3) regulate pH value to 6～9 of extraction water outlet, then by MVR technique, extraction water outlet is carried out to concentration and evaporation, reclaim and obtain sodium sulfate.
2. the comprehensive recovery and treatment method of a kind of H acid trade effluent according to claim 1, is characterized in that, it is industrial sulphuric acid that the H acid trade effluent in described step (1) regulates the acid used of pH value.
3. the comprehensive recovery and treatment method of a kind of H acid trade effluent according to claim 1, is characterized in that, the extraction process service temperature in described step (1) is 30～40 ℃.
4. the comprehensive recovery and treatment method of a kind of H acid trade effluent according to claim 1, is characterized in that, the extraction agent in described step (1) is that trialkyl tertiary amine and sulfonated kerosene mix according to mass ratio 1:2.
5. the comprehensive recovery and treatment method of a kind of H acid trade effluent according to claim 1 and 2, is characterized in that, the membrane separation process in described step (1) adopts ultrafiltration membrance filter, and operational condition is 25～35 ℃ of temperature, pressure 0.3～0.5MPa.
6. the comprehensive recovery and treatment method of a kind of H acid trade effluent according to claim 1 and 2, is characterized in that, described H acid trade effluent is the H acid mother liquor that the finishing operation segregation workshop section of H acid production process produces, and H acid content is more than 3000mg/L.
7. the comprehensive recovery and treatment method of a kind of H acid trade effluent according to claim 6, is characterized in that, in described step (3), MVR technique is continuous operation, and evaporation concentration is than being 1:1～2:3.
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Cited By (17)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
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| CN108178419A (en) * | 2017-11-27 | 2018-06-19 | 江苏力禾颜料有限公司 | Waste water treatment system prepared by H acid monosodium salt |
| CN109748830A (en) * | 2019-01-09 | 2019-05-14 | 江苏吉华化工有限公司 | A kind of processing solution and processing method for H acid mother liquor |
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| CN104030509B (en) * | 2014-06-18 | 2016-01-13 | 泰兴锦汇化工有限公司 | A kind for the treatment of process of color-forming intermediate H acids factory effluent |
| CN105129894A (en) * | 2015-09-09 | 2015-12-09 | 江西玛德精细化学工业有限公司 | High efficiency extraction method of T-acid mother liquor |
| CN105129893A (en) * | 2015-09-09 | 2015-12-09 | 江西玛德精细化学工业有限公司 | High efficiency extractant and extraction method of H-acid mother liquor |
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| CN105906122A (en) * | 2016-05-23 | 2016-08-31 | 江苏瑞升华能源科技有限公司 | Treatment technology of high-organic matter high-salt wastewater and treatment device thereof |
| CN106186147A (en) * | 2016-07-26 | 2016-12-07 | 北京惠宇乐邦环保科技有限公司 | A kind of recovery and treatment method of high concentration waste organic acid |
| CN106186147B (en) * | 2016-07-26 | 2020-05-19 | 北京惠宇乐邦环保科技有限公司 | Recovery treatment method of high-concentration organic acid wastewater |
| CN107021538A (en) * | 2017-03-28 | 2017-08-08 | 刘奎东 | A kind of efficient extraction decolouring system of reactive dyeing raffinate |
| CN107021538B (en) * | 2017-03-28 | 2020-10-30 | 新疆神邦环境工程有限公司 | High-efficient extraction decoloration system of reactive dye dyeing raffinate |
| CN107235594A (en) * | 2017-07-05 | 2017-10-10 | 山东如意科技集团有限公司 | A kind of utilization process and system of reactive dyeing raffinate |
| CN107352677A (en) * | 2017-07-05 | 2017-11-17 | 山东如意科技集团有限公司 | The decoloration process and decolouring system of a kind of reactive dyeing raffinate |
| CN108178406A (en) * | 2017-11-27 | 2018-06-19 | 江苏力禾颜料有限公司 | The technique for reducing H acid monosodium salt waste water COD content |
| CN108178419A (en) * | 2017-11-27 | 2018-06-19 | 江苏力禾颜料有限公司 | Waste water treatment system prepared by H acid monosodium salt |
| WO2019109565A1 (en) * | 2017-12-08 | 2019-06-13 | 荆门市熊兴化工有限公司 | Extraction method and extractant for denitration process in h acid production process |
| CN109748830A (en) * | 2019-01-09 | 2019-05-14 | 江苏吉华化工有限公司 | A kind of processing solution and processing method for H acid mother liquor |
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