CN105948350A - Recycling process and system for high-salt and high-concentration non-biodegradable organic matter-containing H acid wastewater - Google Patents
Recycling process and system for high-salt and high-concentration non-biodegradable organic matter-containing H acid wastewater Download PDFInfo
- Publication number
- CN105948350A CN105948350A CN201610268114.3A CN201610268114A CN105948350A CN 105948350 A CN105948350 A CN 105948350A CN 201610268114 A CN201610268114 A CN 201610268114A CN 105948350 A CN105948350 A CN 105948350A
- Authority
- CN
- China
- Prior art keywords
- acid
- boiling
- pelletize
- sodium sulfate
- waste water
- 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
Classifications
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F9/00—Multistage treatment of water, waste water or sewage
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
- C01D5/00—Sulfates or sulfites of sodium, potassium or alkali metals in general
- C01D5/16—Purification
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
- C02F2001/5218—Crystallization
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
Abstract
The invention discloses a recycling process and system for cyclic utilization of high-salt and high-concentration non-biodegradable organic matter-containing H acid wastewater and production of anhydrous sodium sulfate; the process for production of anhydrous sodium sulfate through solvent-out crystallization, waste acid cyclic utilization and high-temperature boiling granulation and oxidation is designed for the high-salt high-organic-matter H acid wastewater, so all components of the H acid wastewater are recycled with low cost, the production costs of H acid is reduced, zero emission of pollutants is achieved, and the method is the best way for H acid wastewater low-cost recycling, has demonstration significance for treatment of high-salt and high-concentration non-biodegradable organic matter wastewater, and has huge economic and social benefits.
Description
Technical field
The present invention relates to one and containing high salt high-concentration hardly-degradable Organic substance H-acid cycling utilization of wastewater and produce anhydrous
The process for reclaiming of sodium sulfate and system, belong to environmental resource field.
Background technology
Along with developing rapidly, respectively of the industries such as petrochemical industry, medicine, plastics, synthetic fibers, coking, printing and dyeing
Planting the waste water containing a large amount of high salt, the organic pollution of high concentration difficult for biological degradation to increase accordingly, they enter water
Body causes serious pollution to environment, annoyings the sound development of the industries such as petrochemical industry, coalification and medicine.According to
Statistics, the wastewater discharge of national petrochemical industry in 2015 is 42 billion cubic meters, only dye industry high salt difficulty fall
Solve organic wastewater and the most just have more than 20,000,000 tons.Process containing high-concentration hardly-degradable organic pollutant wastewater and be
The difficult problem that at present both at home and abroad sewage disposal circle is generally acknowledged, conventional physical chemistry and biochemical processing method is difficult to or cannot
Meeting the technology to this type of wastewater purification and economic requirement, domestic a lot of industrial undertakings actually fail it
In production process, this part divides waste water process up to standard, and serious environment pollution is healthy with the threat mankind's.Therefore
The Controlling research of hardly degraded organic substance has caused the great attention of domestic and international relevant expert, is current water prevention and cure of pollution
The focus of research and difficult point.
H-acid waste water contains the sulphuric acid of 15-20% sodium sulfate, 5-8%, and COD is up to 2000-40000mg/L, contains
There are the various substitutive derivatives of a large amount of naphthalene, there is strong bio-toxicity, it is extremely difficult to be biochemical, belong to typical case high salt, height
The waste water of concentration persistent organic pollutants.Current domestic H-acid yield is 130,000 tons, produces this waste water per year about
3000000 tons, mainly use extraction, adsorb, decolour, aoxidize, physics and the biochemical combination treatment technology such as concentration,
Processing cost is the highest, produces large amount of organic waste residue, the most thoroughly solves problem.
The present invention is that H-acid waste water devises dilution crystallization, and spent acid recycles, and high-boiling oxidation produces anhydrous
Sodium sulfate, makes H-acid waste water all the components all low cost resources, reduces H-acid production cost, it is achieved that dirty
Dye thing zero-emission, is the optimal path of current H-acid waste water low cost resource, to high salt, high-concentration hardly-degradable
The waste water of organic pollution processes demonstration meaning, and economic and social benefit is huge.
Summary of the invention
The present invention seeks to for above-mentioned existing problems, it is provided that a kind of high-concentration hardly-degradable Organic substance Han high salt
H-acid waste water resource metallization processes and system, this technique has been realized with a low cost each in H-acid high salt height organic wastewater
Plant maximally utilizing of resource, decrease product direct production cost, significantly reduce waste water processing cost, real
Showed zero release of pollutant, made H waste water treatment and integral cost greatly reduce, for promote low cost solve high salt,
High-concentration hardly-degradable organic wastewater technical progress of industry has tremendous increase and demonstration effect, social benefit and economy
Remarkable benefit.
Technical scheme:
A kind of technique containing high salt high-concentration hardly-degradable Organic substance H-acid waste water resource gasifying device, step is as follows:
1) dilution crystallization
H-acid waste water is added in dilution crystallization still, at a temperature of 35-80 DEG C, uses venturi cyclically charging system
System, adds H-acid wastewater quality 10-40% dilution crystallization solvent, places 20-60 minutes, and sodium sulfate is brilliant
Body separates out, and step 3 is sent in separating sodium sulfate crystallization) high-boiling pelletize oxidation furnace device, waste acid liquor enters
Step 2) spent acid recycles workshop section；
2) spent acid recycles
Will be from step 1) containing a large amount of dissolved solvents and sulphuric acid, a small amount of sodium sulfate and a small amount of H-acid and other
Organic principle waste acid liquor, enters evaporating kettle and carries out solvent recovery, and recovered solvent returns step 1), 3-8wt%
Waste acid liquor be transported to the isolation workshop section of H-acid production system to reduce the addition of sulphuric acid in H-acid production technology
Amount；
3) high-boiling pelletize oxidation
Will be from step 1) containing large amount of organic and the sodium sulfate crystal of a small amount of moisture, it is delivered to high-boiling
Pelletize oxidation unit, under the conditions of 400-800 DEG C, the fluidized granulating oxidation 10-200 second is organic thoroughly to decompose
Thing, discharging sodium sulfate, unlap after wind cooling temperature lowering；Material-heat-exchanging wind is combustion-supporting as high-temperature oxydation system
Wind, reclaims heat and cools down material simultaneously；Tail gas 15wt% sodium hydroxide solution absorbs, and qualified discharge absorbs
Liquid is incorporated to step 2), whole high-temperature oxydation system energy consumption is mainly by Organic substance self calorific value, and system increases heat energy newly
Consumption is close to zero.
Described step 1) in dilution crystallization solvent be methanol, ethanol, butanol, toluene, ethylbenzene, acetone and two
The mixture of one or more arbitrary proportions in ethyl chloride.
A kind of realize the described system containing high salt high-concentration hardly-degradable Organic substance H-acid waste water resource metallization processes,
Including dissolved still, centrifuge, evaporating kettle, air cooling heat exchanger, exhaust gas processing device, burner, high-boiling
Pelletize oxidation unit, cyclone separator and Air cooler, dissolved still be provided with H-acid waterwater entrance, dissolved agent entrance,
Mixture export and recycling design entrance, the mixture export of dissolved still is connected with the import of centrifuge；Centrifuge
Liquid-phase outlet is connected to the import of evaporating kettle, and solid-phase outlet connects and high-boiling pelletize oxidation unit is enterprising
Mouthful；The recycling design outlet of evaporating kettle is connected with the recycling design entrance of dissolved still；High-boiling pelletize aoxidizes
The gaseous phase outlet of device is connected with cyclone separator, and the solid material of cyclone separator returns high-boiling pelletize oxidation
Device, the gas phase of cyclone separator is connected with exhaust gas processing device through air cooling heat exchanger, and exhaust gas processing device reclaims
Liquid phase return H-acid waterwater entrance, the treated qualified discharge of tail gas；The thing of high-boiling pelletize oxidation unit
Material outlet is packed after Air cooler is lowered the temperature, and gaseous phase outlet enters high-boiling pelletize oxidation after burner combustion
Device reclaims heat.
The working mechanism of the present invention:
This technique, initially with dilution crystallization, isolates major part sodium sulfate crystal and major part Organic substance, acid
After waste water abjection solvent, spent acid contains partly soluble H-acid, and reuse H-acid isolates workshop section, can reduce sulfur
Acid usage amount, can improve again H-acid yield, decreases the processing cost that spent acid alkali neutralizes simultaneously；Contain
The sodium sulfate of large amount of organic, sends into the high-boiling pelletize oxidation furnace of particular design, utilizes Organic substance self energy
Amount, thorough decomposing organic matter, produce anhydrous sodium sulfate simultaneously, make H-acid waste water all the components all low costs provide
Source, it is achieved that zero release of pollutant.
Step 1 of the present invention) dilution crystallization, it is different from the two-way energy consumption of Conventional concentration or freezing and crystallizing, permissible
In acid condition, at a temperature of H-acid produces waste water nominal situation, low cost crystallizes out anhydrous slufuric acid at high proportion
Sodium crystal；Decrease step 3) system energy consumption, equipment difficult problem when simultaneously also not having acid waste water to concentrate.Literary composition
Solubilizer system is circulated, it is ensured that the granule of crystallization is bigger, it is simple to separate, beneficially step 3 in mound) energy-conservation
Process.
Step 2) principle of spent acid reuse energy saving, spent acid reuse, decrease and evaporate cost in a large number, with
Time compare other techniques and decrease in alkali and expense；H-acid has the dissolubility of 0.5-5% inside spent acid simultaneously,
Common-ion effect, reuse can improve yield, reduces system synthesis cost.
Step 3) energy-conservation principle is, step 1) transferring anhydrous sodium sulfate crystallization, COD is up to 200,000 mg/l
Left and right, and moisture only has about 10%, after this part calorific value of Organic substance self causes, enough Organic substances decompose also
Sodium sulfate, the energy reuse design of system tail gas and material, it is ensured that heat utilization rate reaches more than 90%.
The invention have the advantage that this dilution crystallization technique low-cost separation can go out major part sodium sulfate crystal and big portion
Dividing Organic substance, after acid waste water abjection solvent, useless reuse H-acid isolates workshop section, reduces sulphuric acid usage amount, again can
Improve H-acid yield, decrease the expense that spent acid alkali neutralizes simultaneously；Containing the sodium sulfate of large amount of organic,
Send into the high-boiling oxidation furnace of particular design, utilize Organic substance self-energy, thorough decomposing organic matter, simultaneously
Produce anhydrous sodium sulfate.This technique has been given overall consideration to and has been cleaned the energy-saving and emission-reduction produced, and optimizes the various resource of waste water
Path, makes salinity, Organic substance, spent acid, has each played maximum value, devise guarantee system simultaneously,
It is prone to industrializing implementation；The invention provides new danger to give up recycling economy thinking, change over pure consumption resource
" damage type " process waste water mode, turn waste into wealth, there is significant techno-economic effect and huge society
Benefit.
Accompanying drawing explanation
Fig. 1 is to realize the described system containing high salt high-concentration hardly-degradable Organic substance H-acid waste water resource metallization processes to show
It is intended to.
In figure: 1. dissolved still 2. centrifuge 3. evaporating kettle 4. air cooling heat exchanger 5. exhaust gas processing device 6.
Burner 7. high-boiling pelletize oxidation unit 8. cyclone separator 9. Air cooler.
Detailed description of the invention
Following example are for purposes of illustration only, be not intended that limitation of the present invention.
The work containing high salt high-concentration hardly-degradable Organic substance H-acid waste water resource gasifying device described in following example
The enforcement of skill is all implemented in following system.
A kind of high-concentration hardly-degradable Organic substance H-acid waste water reclaiming system Han high salt, as it is shown in figure 1, bag
Include dissolved still 1, centrifuge 2, evaporating kettle 3, air cooling heat exchanger 4, exhaust gas processing device 5, burner 6,
High-boiling pelletize oxidation unit 7, cyclone separator 8 and Air cooler 9, dissolved still 1 is provided with H-acid waste water and enters
Mouth, dissolved agent entrance, mixture export and recycling design entrance, the mixture export of dissolved still 1 and centrifuge
The import of 2 connects；Centrifuge 2 liquid-phase outlet is connected to the import of evaporating kettle 3, and solid-phase outlet connects high temperature
The import of fluidized granulating oxidation unit 7；The recycling design outlet of evaporating kettle 3 and the recycling design of dissolved still 1
Entrance connects；The gaseous phase outlet of high-boiling pelletize oxidation unit 7 is connected with cyclone separator 8, and whirlwind divides
Solid material from device 8 returns high-boiling pelletize oxidation unit 7, and the gas phase of cyclone separator 8 is through air-cooled heat exchange
Device 4 is connected with exhaust gas processing device 5, and the liquid phase that exhaust gas processing device 5 reclaims returns H-acid waterwater entrance, tail
The treated qualified discharge of gas；The material outlet of high-boiling pelletize oxidation unit 7 wraps after Air cooler 9 is lowered the temperature
Dress, gaseous phase outlet enters high-boiling pelletize oxidation unit 7 after burner 6 burns and reclaims heat.
Embodiment 1:
A kind of technique containing high salt high-concentration hardly-degradable Organic substance H-acid waste water resource gasifying device, step is as follows:
1) dilution crystallization
H-acid waste water is added in dilution crystallization still, at a temperature of 35 DEG C, uses with venturi cyclically charging system
System, adds H-acid wastewater quality 40% dilution crystallization etoh solvent, places 20 minutes, sodium sulfate crystal
Separate out, separating sodium sulfate crystallization feeding 3) high-boiling pelletize oxidation furnace system, waste acid liquor enters step 2)
Spent acid recycles workshop section.
2) spent acid recycles
From step 1) containing a large amount of dissolved solvents and sulphuric acid, a small amount of sodium sulfate and a small amount of H-acid and other have
Machine composition waste acid liquor, enters evaporating kettle and carries out solvent recovery, and recovered temperature is 80 DEG C；Recovered solvent returns
Return step 1), the waste acid liquor of 5wt% is transported to the isolation workshop section of H-acid production system, it is possible to reduce H-acid is raw
The addition 15% of sulphuric acid in production. art.
3) high-boiling pelletize oxidation
From step 1) containing large amount of organic and the sodium sulfate crystal of a small amount of moisture, it is delivered to high-boiling and makes
Grain oxidative system；Under the conditions of 700 DEG C, fluidized granulating aoxidizes 40 seconds, organic matter decomposition rate 99.8%, discharging
Sodium sulfate, unlap after wind cooling temperature lowering；Material-heat-exchanging wind, as the combustion air of high-temperature oxydation system, reclaims
Heat cools down material simultaneously；Tail gas absorbs with 15% sodium hydroxide solution, qualified discharge, and absorbing liquid is incorporated to step
2).Whole high-temperature oxydation system energy consumption increases thermal energy consumption newly mainly by Organic substance self calorific value, waste water system per ton
It is 7 kilograms of mark coals.All achieving resource through above step H-acid waste water all the components, waste water per ton is combined
Close cost of disposal close to null element.
Embodiment 2:
A kind of technique containing high salt high-concentration hardly-degradable Organic substance H-acid waste water resource gasifying device, step is as follows:
1) dilution crystallization
H-acid waste water is added in dilution crystallization still, at a temperature of 45 DEG C, uses with venturi cyclically charging system
System, adds H-acid wastewater quality 30% dilution crystallization solvent methanol, places 60 minutes, sodium sulfate crystal
Separate out, separating sodium sulfate crystallization feeding 3) high-boiling pelletize oxidation furnace system, waste acid liquor enters step 2)
Spent acid recycles workshop section.
2) spent acid recycles
From step 1) containing a large amount of dissolved solvents and sulphuric acid, a small amount of sodium sulfate and a small amount of H-acid and other have
Machine composition waste acid liquor, enters evaporating kettle and carries out solvent recovery, and recovered temperature is 60 DEG C；Recovered solvent returns
Return step 1), the waste acid liquor of 6wt% is transported to the isolation workshop section of H-acid production system, it is possible to reduce H-acid is raw
The addition 16% of sulphuric acid in production. art.
3) high-boiling pelletize oxidation
From step 1) containing large amount of organic and the sodium sulfate crystal of a small amount of moisture, it is delivered to high-boiling and makes
Grain oxidative system；Under the conditions of 600 DEG C, fluidized granulating aoxidizes 120 seconds, and organic matter decomposition rate 99.7% goes out
Material sodium sulfate, unlap after wind cooling temperature lowering；Material-heat-exchanging wind, as the combustion air of high-temperature oxydation system, returns
Receive heat and cool down material simultaneously；Tail gas absorbs with 15% sodium hydroxide solution, qualified discharge, and absorbing liquid is incorporated to step
Rapid 2).Whole high-temperature oxydation system energy consumption increases heat energy newly mainly by Organic substance self calorific value, waste water system per ton
Consumption is 8 kilograms of mark coals.Resource is all achieved through above step H-acid waste water all the components, per ton useless
Water joint disposal cost is close to null element.
Embodiment 3:
A kind of technique containing high salt high-concentration hardly-degradable Organic substance H-acid waste water resource gasifying device, step is as follows:
1) dilution crystallization
H-acid waste water is added in dilution crystallization still, at a temperature of 50 DEG C, uses with venturi cyclically charging system
System, adds H-acid wastewater quality 15% dilution crystallization etoh solvent, places 100 minutes, sodium sulfate crystal
Separate out, separating sodium sulfate crystallization feeding 3) high-boiling pelletize oxidation furnace system, waste acid liquor enters step 2)
Spent acid recycles workshop section.
2) spent acid recycles
From step 1) containing a large amount of dissolved solvents and sulphuric acid, a small amount of sodium sulfate and a small amount of H-acid and other have
Machine composition waste acid liquor, enters evaporating kettle and carries out solvent recovery, and recovered temperature is 80 DEG C；Recovered solvent returns
Return step 1), the waste acid liquor of 4wt% is transported to the isolation workshop section of H-acid production system, it is possible to reduce H-acid is raw
The addition 13% of sulphuric acid in production. art.
3) high-boiling pelletize oxidation
From step 1) containing large amount of organic and the sodium sulfate crystal of a small amount of moisture, it is delivered to high-boiling and makes
Grain oxidative system；Under the conditions of 500 DEG C, fluidized granulating aoxidizes 160 seconds, and organic matter decomposition rate 99.8% goes out
Material sodium sulfate, unlap after wind cooling temperature lowering；Material-heat-exchanging wind, as the combustion air of high-temperature oxydation system, returns
Receive heat and cool down material simultaneously；Tail gas absorbs with 15% sodium hydroxide solution, qualified discharge, and absorbing liquid is incorporated to step
Rapid 2).Whole high-temperature oxydation system energy consumption increases heat energy newly mainly by Organic substance self calorific value, waste water system per ton
Consumption is 7 kilograms of mark coals.Resource is all achieved through above step H-acid waste water all the components, per ton useless
Water joint disposal cost is close to null element.
Claims (3)
1. the technique containing high salt high-concentration hardly-degradable Organic substance H-acid waste water resource gasifying device, its feature
It is that step is as follows:
1) dilution crystallization
H-acid waste water is added in dilution crystallization still, at a temperature of 35-80 DEG C, uses venturi cyclically charging system
System, adds H-acid wastewater quality 10-40% dilution crystallization solvent, places 20-60 minutes, and sodium sulfate is brilliant
Body separates out, and step 3 is sent in separating sodium sulfate crystallization) high-boiling pelletize oxidation furnace device, waste acid liquor enters
Step 2) spent acid recycles workshop section；
2) spent acid recycles
Will be from step 1) containing a large amount of dissolved solvents and sulphuric acid, a small amount of sodium sulfate and a small amount of H-acid and other
Organic principle waste acid liquor, enters evaporating kettle and carries out solvent recovery, and recovered solvent returns step 1), 3-8wt%
Waste acid liquor be transported to the isolation workshop section of H-acid production system to reduce the addition of sulphuric acid in H-acid production technology
Amount；
3) high-boiling pelletize oxidation
Will be from step 1) containing large amount of organic and the sodium sulfate crystal of a small amount of moisture, it is delivered to high-boiling
Pelletize oxidation unit, under the conditions of 400-800 DEG C, the fluidized granulating oxidation 10-200 second is organic thoroughly to decompose
Thing, discharging sodium sulfate, unlap after wind cooling temperature lowering；Material-heat-exchanging wind is combustion-supporting as high-temperature oxydation system
Wind, reclaims heat and cools down material simultaneously；Tail gas 15wt% sodium hydroxide solution absorbs, and qualified discharge absorbs
Liquid is incorporated to step 2), whole high-temperature oxydation system energy consumption is mainly by Organic substance self calorific value, and system increases heat energy newly
Consumption is close to zero.
The most according to claim 1 containing high salt high-concentration hardly-degradable Organic substance H-acid waste water resource gasifying device
Technique, it is characterised in that: described step 1) in dilution crystallization solvent be methanol, ethanol, butanol, toluene,
The mixture of one or more arbitrary proportions in ethylbenzene, acetone and dichloroethanes.
3. one kind realizes the high-concentration hardly-degradable Organic substance H-acid waste water reclaiming Han high salt described in claim 1
The system of technique, it is characterised in that: include dissolved still, centrifuge, evaporating kettle, air cooling heat exchanger, tail gas
Processing means, burner, high-boiling pelletize oxidation unit, cyclone separator and Air cooler, dissolved still is provided with
H-acid waterwater entrance, dissolved agent entrance, mixture export and recycling design entrance, the mixture export of dissolved still
It is connected with the import of centrifuge；Centrifuge liquid-phase outlet is connected to the import of evaporating kettle, solid-phase outlet connect and
High-boiling pelletize oxidation unit upper inlet；The recycling design outlet of evaporating kettle enters with the recycling design of dissolved still
Mouth connects；The gaseous phase outlet of high-boiling pelletize oxidation unit is connected with cyclone separator, cyclone separator
Gu material returns high-boiling pelletize oxidation unit, the gas phase of cyclone separator is through air cooling heat exchanger and vent gas treatment
Device connects, and the liquid phase that exhaust gas processing device reclaims returns H-acid waterwater entrance, the treated qualified discharge of tail gas；
The material outlet of high-boiling pelletize oxidation unit is packed after Air cooler is lowered the temperature, and gaseous phase outlet fires through burner
Enter high-boiling pelletize oxidation unit after burning and reclaim heat.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610268114.3A CN105948350B (en) | 2016-04-26 | 2016-04-26 | H acid waste water reclaiming technique and system containing high-concentration hardly-degradable organic matter with high salt |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610268114.3A CN105948350B (en) | 2016-04-26 | 2016-04-26 | H acid waste water reclaiming technique and system containing high-concentration hardly-degradable organic matter with high salt |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN105948350A true CN105948350A (en) | 2016-09-21 |
| CN105948350B CN105948350B (en) | 2019-04-05 |
Family
ID=56915607
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201610268114.3A Active CN105948350B (en) | 2016-04-26 | 2016-04-26 | H acid waste water reclaiming technique and system containing high-concentration hardly-degradable organic matter with high salt |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN105948350B (en) |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106669386A (en) * | 2016-12-14 | 2017-05-17 | 江苏瑞升华能源科技有限公司 | Spray oxidization granulation technique and device |
| CN108950235A (en) * | 2018-07-19 | 2018-12-07 | 芜湖青悠静谧环保科技有限公司 | A kind of recovery method of the pre- desulphurization mother solution of lead plaster |
| CN112079366A (en) * | 2020-08-10 | 2020-12-15 | 暨南大学 | Method for separating and recovering sodium nitrate and sodium sulfate from low-temperature flue gas oxidation denitration absorption liquid |
| CN112174375A (en) * | 2020-09-28 | 2021-01-05 | 北京石油化工学院 | Method for extracting sodium sulfate from phenol-containing wastewater |
| CN113024005A (en) * | 2021-03-30 | 2021-06-25 | 常州时升环境工程科技有限公司 | Resource treatment process for hardly-degradable salt-containing organic wastewater |
Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103803753A (en) * | 2014-02-28 | 2014-05-21 | 南京大学盐城环保技术与工程研究院 | Comprehensive recovery treatment method for H acid industrial waste water |
| CN103979730A (en) * | 2014-06-05 | 2014-08-13 | 华东理工大学 | Method for purifying penicillin production waste liquid and recycling sodium sulfate |
| CN104086017A (en) * | 2014-06-13 | 2014-10-08 | 通辽市龙盛化工有限公司 | Treatment method of H acid separation waste water |
| CN104326614A (en) * | 2014-11-12 | 2015-02-04 | 中蓝连海设计研究院 | Comprehensive treatment method of H acid production wastewater |
| 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 |
| CN105130079A (en) * | 2015-09-09 | 2015-12-09 | 江西玛德精细化学工业有限公司 | Treatment process combining H acid mother solution and T acid mother solution |
| 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 |
| CN105384292A (en) * | 2015-11-13 | 2016-03-09 | 中蓝连海设计研究院 | H acid production industrial waste water treatment method |
-
2016
- 2016-04-26 CN CN201610268114.3A patent/CN105948350B/en active Active
Patent Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103803753A (en) * | 2014-02-28 | 2014-05-21 | 南京大学盐城环保技术与工程研究院 | Comprehensive recovery treatment method for H acid industrial waste water |
| CN103979730A (en) * | 2014-06-05 | 2014-08-13 | 华东理工大学 | Method for purifying penicillin production waste liquid and recycling sodium sulfate |
| CN104086017A (en) * | 2014-06-13 | 2014-10-08 | 通辽市龙盛化工有限公司 | Treatment method of H acid separation waste water |
| CN104326614A (en) * | 2014-11-12 | 2015-02-04 | 中蓝连海设计研究院 | Comprehensive treatment method of H acid production wastewater |
| 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 |
| CN105130079A (en) * | 2015-09-09 | 2015-12-09 | 江西玛德精细化学工业有限公司 | Treatment process combining H acid mother solution and T acid mother solution |
| 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 |
| CN105384292A (en) * | 2015-11-13 | 2016-03-09 | 中蓝连海设计研究院 | H acid production industrial waste water treatment method |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106669386A (en) * | 2016-12-14 | 2017-05-17 | 江苏瑞升华能源科技有限公司 | Spray oxidization granulation technique and device |
| CN108950235A (en) * | 2018-07-19 | 2018-12-07 | 芜湖青悠静谧环保科技有限公司 | A kind of recovery method of the pre- desulphurization mother solution of lead plaster |
| CN112079366A (en) * | 2020-08-10 | 2020-12-15 | 暨南大学 | Method for separating and recovering sodium nitrate and sodium sulfate from low-temperature flue gas oxidation denitration absorption liquid |
| CN112174375A (en) * | 2020-09-28 | 2021-01-05 | 北京石油化工学院 | Method for extracting sodium sulfate from phenol-containing wastewater |
| CN113024005A (en) * | 2021-03-30 | 2021-06-25 | 常州时升环境工程科技有限公司 | Resource treatment process for hardly-degradable salt-containing organic wastewater |
Also Published As
| Publication number | Publication date |
|---|---|
| CN105948350B (en) | 2019-04-05 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN105948350A (en) | Recycling process and system for high-salt and high-concentration non-biodegradable organic matter-containing H acid wastewater | |
| CN107185948B (en) | Industrial waste salt system and method | |
| CN108358407B (en) | PTA oxidation residue and sludge comprehensive utilization system and method | |
| CN109867296A (en) | A kind of industrial chlorinations sodium waste salt dregs refining methd | |
| CN113149038A (en) | Resource utilization method for treating industrial mixed waste salt by using sulfuric acid | |
| CN101372381B (en) | 3,3'-dichlorobenzidine hydrochloride waste water reclaiming method and apparatus thereof | |
| CN109019634B (en) | Chemical waste salt refining and resource utilization system and method | |
| CN105967415A (en) | 2-naphthol high-salt and high-concentration organic matter wastewater recycling process and system | |
| CN109879507A (en) | A kind of technique and device of coking high-salt wastewater resource utilization | |
| WO2014194790A1 (en) | Method for extracting two secondary salts from desulfurized salt-containing waste liquid of coke oven gas | |
| CN106976896A (en) | A kind of utilization waste sulfuric acid from alkylation produces the method and system of epsom salt | |
| CN114535264A (en) | Recycling treatment method for industrial waste salt | |
| WO2014194791A1 (en) | Method for processing sulphur paste as by-product from coke oven coal gas desulphuration | |
| CN112222156A (en) | Method for removing organic matters in industrial waste salt | |
| CN112794289A (en) | Sulfur purification system and purification process thereof | |
| CN114685020B (en) | Sludge anaerobic digestion combined desiccation carbonization system and method | |
| CN214437765U (en) | Equipment for separating sodium and potassium salts in high-temperature melting flue gas of waste incineration fly ash | |
| CN212404016U (en) | Waste salt vacuum cracking system | |
| CN114249336A (en) | Process for preparing industrial sodium carbonate by using chemical tail gas waste salt | |
| CN112691509A (en) | Equipment and method for separating sodium and potassium salts in high-temperature molten flue gas of waste incineration fly ash | |
| CN110204168B (en) | Resource treatment method and device for tannery sludge | |
| CN108502903B (en) | Gasification detoxification system and method for pre-concentrated salt residue fluidized bed | |
| CN102351149A (en) | System for recovering and removing chlorine from hydrogen chloride | |
| CN107597795B (en) | System and method for recycling and treating household garbage incineration fly ash | |
| CN220976601U (en) | Solid danger salt waste regenerating unit |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |