CN105883859A - Waste salt treatment method - Google Patents
Waste salt treatment method Download PDFInfo
- Publication number
- CN105883859A CN105883859A CN201610430258.4A CN201610430258A CN105883859A CN 105883859 A CN105883859 A CN 105883859A CN 201610430258 A CN201610430258 A CN 201610430258A CN 105883859 A CN105883859 A CN 105883859A
- Authority
- CN
- China
- Prior art keywords
- abraum salt
- roasting
- processing method
- salt
- hya
- 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.)
- Pending
Links
Classifications
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
- C01D3/00—Halides of sodium, potassium or alkali metals in general
- C01D3/14—Purification
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D45/00—Separating dispersed particles from gases or vapours by gravity, inertia, or centrifugal forces
- B01D45/12—Separating dispersed particles from gases or vapours by gravity, inertia, or centrifugal forces by centrifugal forces
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/18—Absorbing units; Liquid distributors therefor
-
- 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
- C02F1/28—Treatment of water, waste water, or sewage by sorption
-
- 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
- C02F1/42—Treatment of water, waste water, or sewage by ion-exchange
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Organic Chemistry (AREA)
- Water Supply & Treatment (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Life Sciences & Earth Sciences (AREA)
- Hydrology & Water Resources (AREA)
- Environmental & Geological Engineering (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- General Chemical & Material Sciences (AREA)
- Analytical Chemistry (AREA)
- Materials Engineering (AREA)
- Inorganic Chemistry (AREA)
- Solid-Sorbent Or Filter-Aiding Compositions (AREA)
- Water Treatment By Sorption (AREA)
Abstract
The invention relates to a waste salt treatment method, and belongs to the technical field of treatment of water or wastewater or sewage or sludge. Waste salt to be treated is roasted for 0.5 h to 4 h at 300 DEG C to 600 DEG C, wherein tail gas generated in the roasting process enters a gas purification device to be purified and then exhausted; water is added to a roasted product, beating is conducted, and a treated fluid of which the salt concentration ranges from 15% to 25% is formed; the treated fluid is subjected to macroporous resin absorption and then drained. The waste salt treatment method is applied to industrial waste salt treatment and has the advantages of being low in energy consumption, easy and convenient to operate, good in treatment effect and the like.
Description
Technical field
The present invention relates to a kind of abraum salt processing method, belong to the processing technology field of water, waste water, sewage or mud.
Background technology
Containing Organic substance in industrial waste salt, common processing method is: burning method, multistage washing method, landfill method,
Forge the method for firing building material, dissolve the method for reconcentration crystallization after adsorbing, etc..
The disclosure of the invention refinement treatment side of a kind of by-product Nacl such as Application No. 201510851364.5
Method, it " obtains pure by the method for " dissolving-absorption-spray drying-middle temperature calcination-dissolving-Ultrafiltration-Concentration "
White salt crystals.Long flow path and twice dissolving of need.
In the invention of Application No. 201510077657.2, amino phenylate, paranitrophenol are produced waste water and inhale
The solid salt that attached evaporative crystallization obtains obtains high-quality volume chlorination by " high-temperature calcination-dissolving-evaporative crystallization "
Sodium；A kind of technique processing abraum salt of the disclosure of the invention of Application No. 201510428826.2, uses " melted
Remove impurity-condensation " way organics removal, obtain high-quality salt；Application No. 201410220949.2
Invention remove the Organic substance in Nacl by " high-temperature catalytic-middle temperature be catalyzed " method, obtain clean having
Machine thing.Three kinds of temperature required height of method, power consumption height.
Based on this, make the application.
Summary of the invention
In order to overcome the drawbacks described above in the presence of existing industrial waste salt processing procedure, the application provides a kind of flow process
Simply, the abraum salt processing method that energy consumption is relatively low.
For achieving the above object, the technical scheme that the application takes is as follows:
A kind of abraum salt processing method, pending abraum salt employing steps of processing: (1) roasting: by pending
Abraum salt is roasting 0.5-4 hour at 300-600 DEG C, and wherein tail gas produced by roasting enters gas cleaning plant
Discharging after purifying, it is standby that calcining matter is down to room temperature；(2) water-soluble；Add water making beating by calcining matter, forms salt
Mass concentration is the treatment fluid of 20%；(3) resin absorption: by step (2) gained treatment fluid through macroporous resin
Discharge after absorption.
Further, as preferably:
Described tail gas clean-up technique is: the waste gas that abraum salt roasting is volatilized enters cyclone dust collection by flue
Device, the superfine material carried in dust-precipitator exhaust gas recycling, waste gas enters absorption tower by induced-draft fan and processes.
Described treatment fluid temperature is 20-50 DEG C, and this temperature is slightly above room temperature, can be effectively improved salt in water
Dissolubility so that it is maximum to the greatest extent is converted into soluble salt solutions, while convenient absorption, also reduces in ejection
Solids content.
Described macroporous resin uses macroporous adsorbent resin or macroporous anion exchange resin.It is furthermore preferred that described is big
Hole resin can be selected for HYA-103, HYA-105, HYA-106, HYA-107, HYA-110 (Xi'an vast space resin
Science and Technology Ltd.) in any one.
Use technical scheme, by pending abraum salt (the abraum salt such as chlorination produced with Fine Chemical
Sodium salt is main source) high-temperature roasting at 300-600 DEG C, the tail gas that high-temperature roasting produces enters gas purification
Device is discharged after carrying out gas purification process；And the calcining matter use water after high-temperature roasting processes is pulled an oar, and it is made to flow
Crossing macropore resin absorbing column, going out post liquid can be expelled directly out.Compared with usual manner, the operation principle of the application
And have the beneficial effect that:
(1) technological process is short, easy to operate.In the application, the process of abraum salt has only to two steps and can complete,
Pending abraum salt first passes through high-temperature roasting, is waste gas and solubility by most organic compound combustion decomposition and inversion
Salt and a small amount of small organic molecule, waste gas purification therein can be discharged, and soluble-salt forms saline solution, warp
Macroporous resin adsorption removes Organic substance therein further, and treatment fluid colourity, TOC after macroporous resin adsorption are (total
Organic carbon) and the clearance of TN (total nitrogen) all can reach more than 99%, reach enter ion film caustic soda sodium chloride
Requirement, can direct plunge into subsequent processing processing.
(2) organic removal rate is high, and emission pollutes few.Organic substance in abraum salt is the largest source of solid waste,
The application passes through high-temperature roasting and absorption, and the Organic substance of the overwhelming majority is converted into waste gas and soluble-salt, waste gas
Can discharge after purification, remaining a small amount of small organic molecule is the most directly the most permissible by macroporous resin column absorption
Removing, when being put into subsequent processing, organic substance residues amount therein is the lowest, can meet use completely
Demand.
(3) energy consumption is low, can effectively reduce post processing cost.The application only requires the expenditure of energy at firing stage,
And the temperature of firing stage belongs to middle temperature, conventional equipment can be supplied, it is not necessary to uses large-scale firing equipment, and water
Molten and absorption is all by mean of the physical property of calcining matter and realizes dissolving and absorption, it is not necessary to carry out the confession of external energy
Should, and the whole course of processing need not increase catalyst or activating agent, energy and supplies consumption little, processing and
Post processing low cost, universality is high.
Detailed description of the invention
Embodiment 1
The pending abraum salt of the present embodiment is lemon yellow, chloride containing sodium salt 87.38%, Organic substance 2.62%,
Aqueous 10%, the TOC of the saturated solution after dissolving is about 15000mg/L.Above-mentioned abraum salt is according to following operation
Process:
(1) roasting: take sodium chloride abraum salt, puts in incinerator, is warming up to 500 DEG C, keeps temperature calcination 3h,
Obtaining calcining matter, the tail gas that roasting produces enters gas cleaning plant.
After coming out of the stove, calcining matter shows canescence.
(2) water-soluble: the calcining matter of step (1) is made into the saline solution of 20%, saline solution temperature T meets:
30≤T ＜ 50；Record the TOC of this saline solution be 83.94mg/L, TN be 56.1mg/L.
(3) resin absorption: the saline solution that step (2) obtains crosses macroporous resin column (Xi'an vast space resin science and technology
Company limited produces, lower same), adsorb, after absorption, obtain treatment fluid, the TOC recording treatment fluid is
5.05mg/L, TN are 0.5mg/L
Embodiment 2
The pending abraum salt of the present embodiment is: use the sodium hydroxide of 80-90% containing highly concentrated Organic substance strongly acid wastewater
Solution neutralizes, and after reaction, has NaCl float to separate out, directly filters, and the sodium chloride abraum salt obtained is as waiting to locate
Reason abraum salt, in bronzing, chloride containing sodium salt 89.70%, Organic substance 2.70%, aqueous 7.60%, after dissolving
The TOC of saturated solution is about 13580mg/L.Above-mentioned abraum salt processes according to following operation:
(1) roasting: take sodium chloride abraum salt, puts in incinerator, is warming up to 400 DEG C, keeps temperature calcination 3h,
Obtaining calcining matter, record calcining matter after coming out of the stove and show canescence, the tail gas that roasting produces enters gas cleaning plant.
It is (2) water-soluble: the calcining matter of step (1) to be put in clear water according to 1:4, obtains saline solution,
Concentration of salt solution 20%, saline solution temperature T meets: 30≤T ＜ 50；The TOC recording saline solution is
62.98mg/L, TN are 33.6mg/L.
(3) resin absorption: the saline solution that step (2) obtains crosses macroporous resin column, adsorbs, after absorption
Obtain treatment fluid, record the TOC for the treatment of fluid be 3.05mg/L, TN be 0.8mg/L
Embodiment 3
The present embodiment pending abraum salt gray, chloride containing sodium salt 90%, Organic substance 1.02%, aqueous 8.98%,
The TOC of the saturated solution after dissolving is about 8000mg/L.Above-mentioned abraum salt processes according to following operation:
(1) roasting: take sodium chloride abraum salt, puts in incinerator, is warming up to 300 DEG C, keeps temperature calcination 2h,
Obtaining calcining matter, record the calcining matter after coming out of the stove and show canescence, the tail gas that roasting produces enters gas cleaning plant.
(2) water-soluble: the calcining matter of step (1) is put in clear water according to 1:4, concentration of salt solution 20%,
Saline solution temperature T meets: 30≤T ＜ 50；Obtaining saline solution, the TOC recording saline solution is 30.89mg/L,
TN is 23.5mg/L.
(3) resin absorption: the saline solution that step (2) obtains crosses macroporous resin column, adsorbs, after absorption
Obtain treatment fluid, record the TOC for the treatment of fluid be 4.08mg/L, TN be 0.3mg/L.
The result of embodiment 1-3 is compareed, referring specifically to shown in table 1.
Effect comparison table before and after the process of table 1 different modes
Wherein, sodium chloride, organic unit are % (mass percent), TOC and TN unit is
mg/L。
By the comparison of table 1 it can be seen that use the technical scheme of the application, the organic removal rate of abraum salt is high
Reaching more than 99%, after process, TOC, TN are down to 5%, less than 1.0% respectively, can be directly entered ion
Film process of caustic soda carries out post processing processing.
Embodiment 4-9
In pending abraum salt, chloride containing sodium salt 89.70%, Organic substance 2.70%, aqueous 7.60%.
Roasting time is 3 hours；Concentration of salt solution 20%, saline solution temperature T meets: 30≤T ＜ 50；
Sintering temperature is respectively 200 DEG C, 250 DEG C, 300 DEG C, 350 DEG C, 400 DEG C, 500 DEG C and 600 DEG C, to most preferably
Sintering temperature is tested, and result is referring specifically to table 2.
Treatment effect synopsis during different sintering temperature under table 2 the same terms
Wherein, TOC and TN unit is mg/L.
From table 2 it can be seen that along with the rising of sintering temperature, in the saline solution that calcining matter is formed TOC and
TN reduces more and more significant, time between especially 300-400 DEG C, reduces especially pronounced, but when temperature exceedes
When 400 DEG C, this growth gradually slows down, and when sintering temperature is increased to 600 DEG C by 500 DEG C, its amplification reduces not
Obvious again, therefore, comprehensive energy consumption cost mates with the optimal for the treatment of effect, and sintering temperature is chosen as 300-600 DEG C,
And be optimal with 300-400 DEG C.
Embodiment 10-13
In pending abraum salt, chloride containing sodium salt 89.70%, Organic substance 2.70%, aqueous 7.60%.
Sintering temperature is 400 DEG C；Concentration of salt solution 20%, saline solution temperature T meets: 30≤T ＜ 50；Roasting
The burning time is respectively 0.5h, 2.0h, 3.0h, 4.0h and 5.0h, tests optimal roasting time, place
Reason result is referring specifically to table 3.
The treatment effect synopsis of different roasting time under table 3 the same terms
Wherein, TOC and TN unit is mg/L.
From table 3 it can be seen that under identical sintering temperature, along with the prolongation of roasting time, content of organics by
Gradually reducing, in the solution after saline solution and process, TOC, TN reduce notable, when the time reaches 3.0-4.0h,
This reduction reaches maximum, continues to extend roasting time, reduces no longer obvious, due to salt Organic substance after burning
Seldom, can't there is being charred phenomenon to content in purer salt, and the longest energy consumption cost of roasting time is the highest,
It is unfavorable for post processing.Therefore, comprehensive energy consumption cost mates with the optimal for the treatment of effect, and roasting time may select
0.5-4 hour, preferably 2-3 hour.
Embodiment 14-17
In pending abraum salt, chloride containing sodium salt 89.70%, Organic substance 2.70%, aqueous 7.60%.
Sintering temperature is 400 DEG C, roasting time 3h；Saline solution temperature T meets: 30≤T ＜ 50；Water-soluble
To concentration of salt solution be respectively 10%, 15%, 20%, 25% and 30%, respectively as embodiment 14-17,
Result shows, the dissolubility of comprehensive salt, reduces the total amount of saline solution, reduces processing cost, works as salinity
When being 20%, process before TOC62.98mg/L, TN 33.6mg/L, after process TOC be down to 3.05mg/L,
TN is down to 0.8mg/L.
Embodiment 18-21
In pending abraum salt, chloride containing sodium salt 89.70%, Organic substance 2.70%, aqueous 7.60%.
Sintering temperature is 400 DEG C, roasting time 3h；Concentration of salt solution 20%；The water-soluble saline solution temperature obtained
Degree T is respectively 10≤T ＜ 15,15≤T ＜ 20,20≤T ＜ 30,30≤T ＜ 50 and 50≤T ＜ 60, right
Optimal saline solution temperature is tested, and result is referring specifically to table 4.
Treatment effect synopsis during various salts temperature under table 4 the same terms
Wherein, TOC and TN unit is mg/L.
From table 4, it can be seen that with adsorption column interact should be the small organic molecule in saline solution,
When saline solution temperature is too high, resin column occurs that desorption effect, absorption organic matter efficiency decline.
Comparative example 1
With patent 201310220509.2 as a comparison case 1, waste salt dregs uses thermal decomposition method to carry out innoxious place
Reason, heating flue-gas temperature is 500-1000 DEG C, and residence time of material is 4-10 hour, the Organic substance in abraum salt
Objectionable impurities is thermally decomposed into volatile tail gas, and tail gas is taken out of by the hot-air being passed through bottom pyrolysis oven, through offgas duct
Coming back to air stove calcine, tail gas supplements fresh air, air stove when introducing air stove and calcining
After the flue gas produced completes heating, reclaiming thermal source recycling through waste heat boiler, flue gas is high idle discharge after water film dedusting
Put；Sodium chloride after process as preparing the raw material of industry salt of chlor-alkali or soda, as cement building material additive,
The snow melting agent of snow sky road uses, and the sodium sulfate after process is used for preparing sodium sulfide as industrial anhydrous Matrii Sulfas Exsiccatus.
Comparative example 2
With patent 201410003693.X as a comparison case 2, waste water enters stripping tower and carries out dichloromethane air stripping,
Steam enters heated waste water in stripping tower, and after bottom stripping tower, waste water enters acidizing device process, waste water enters
Resin absorption device, the time of staying is 5～60min, the content of organics 5～50mg/L of the waste water after absorption,
Enter back into absorbent charcoal adsorber, add after alkali liquor adjusts pH value and carry out Secondary Organic thing absorption, during stop
Between be 10～60min, outlet wastewater through organic matter content be 1～20mg/L, send into sewage-treatment plant.
The cost synopsis of table 5 different disposal scheme
The application has only to roasting and water-soluble absorption two step in processing procedure, and sintering temperature is at 300-500 DEG C
, documents 1 then needs to carry out repeatedly thermal degradation and could realize, and its temperature must reach
The high-temperature region of 500-1000 DEG C just can carry out thermal degradation, and energy consumption is huge, and heat treatment cost is high；Though documents 2
So also use resin absorption, but its pretreatment such as air stripping to be carried out and acid-base neutralization, after resin absorption
Also needing to carry out activated carbon adsorption, adsorption effect is the best.
Above content is that the preferred implementation combining the invention is entered one to what provided technical scheme made
Step describes in detail, it is impossible to assert that the invention is embodied as being confined to these explanations above-mentioned, for the present invention
For creating person of an ordinary skill in the technical field, without departing from the concept of the premise of the invention, also
Some simple deduction or replace can be made, all should be considered as belonging to the protection domain of the invention.
Claims (7)
1. an abraum salt processing method, it is characterised in that pending abraum salt employing steps of processing:
(1) roasting: by pending abraum salt roasting 0.5-4 hour at 300-600 DEG C, wherein tail gas produced by roasting enters after gas cleaning plant purifies and discharges, and it is standby that calcining matter is down to room temperature；
(2) water-soluble；Add water making beating by calcining matter, forms the treatment fluid that salinity is 15-25%；
(3) resin absorption: step (2) gained treatment fluid is discharged after macroporous resin adsorption.
2. a kind of abraum salt processing method as claimed in claim 1, it is characterized in that: described purification technique is: the waste gas that abraum salt roasting is volatilized enters rotoclone collector by flue, the superfine material carried in dust-precipitator exhaust gas recycling, waste gas enters absorption tower by induced-draft fan and processes.
3. a kind of abraum salt processing method as claimed in claim 1, it is characterised in that: described sintering temperature is 300-400 DEG C.
4. a kind of abraum salt processing method as claimed in claim 1, it is characterised in that: described roasting time is 2-3 hour.
5. a kind of abraum salt processing method as claimed in claim 1, it is characterised in that: described treatment fluid temperature is 20-50 DEG C.
6. a kind of abraum salt processing method as claimed in claim 1, it is characterised in that: described macroporous resin uses macroporous adsorbent resin or macroporous anion exchange resin.
7. a kind of abraum salt processing method as claimed in claim 1, it is characterised in that: described macroporous resin selects HYA-103, any one in HYA-105, HYA-106, HYA-107, HYA-110.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610430258.4A CN105883859A (en) | 2016-06-16 | 2016-06-16 | Waste salt treatment method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610430258.4A CN105883859A (en) | 2016-06-16 | 2016-06-16 | Waste salt treatment method |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN105883859A true CN105883859A (en) | 2016-08-24 |
Family
ID=56730870
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201610430258.4A Pending CN105883859A (en) | 2016-06-16 | 2016-06-16 | Waste salt treatment method |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN105883859A (en) |
Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106495190A (en) * | 2016-09-12 | 2017-03-15 | 天津科技大学 | A kind of calcining of abraum salt containing lithium recovery method |
| CN106989403A (en) * | 2017-03-30 | 2017-07-28 | 大丰跃龙化学有限公司 | The processing method of abraum salt in cyclopropanecarboxylic acid wastewater treatment |
| CN107128951A (en) * | 2017-06-22 | 2017-09-05 | 南京诚朴环保科技有限公司 | A kind of method of organic matter in removing inorganic salts |
| CN111112296A (en) * | 2019-12-27 | 2020-05-08 | 洛南环亚源铜业有限公司 | Resource utilization treatment method for industrial waste salt |
| CN111272946A (en) * | 2020-03-30 | 2020-06-12 | 合肥工业大学 | Device and method for measuring content of organic carbon in industrial waste salt |
| CN111471432A (en) * | 2020-04-03 | 2020-07-31 | 安徽科安废盐资源化有限公司 | Method for preparing snow-melting agent by using industrial waste miscellaneous salt |
| CN113048489A (en) * | 2021-03-16 | 2021-06-29 | 上海蓄科环境工程有限公司 | Method and system for purifying and recycling industrial salt from waste salt containing organic matters |
| CN113149035A (en) * | 2020-12-29 | 2021-07-23 | 中国科学院生态环境研究中心 | Method for treating waste sodium chloride salt |
| CN114605018A (en) * | 2022-02-04 | 2022-06-10 | 重庆大学 | Method for treating phosphorus-containing fluorine-containing high-salt organic wastewater and recycling salt |
Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105502437A (en) * | 2015-11-26 | 2016-04-20 | 山东潍坊润丰化工股份有限公司 | Resourceful treatment technology of by-product industrial salt |
-
2016
- 2016-06-16 CN CN201610430258.4A patent/CN105883859A/en active Pending
Patent Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105502437A (en) * | 2015-11-26 | 2016-04-20 | 山东潍坊润丰化工股份有限公司 | Resourceful treatment technology of by-product industrial salt |
Cited By (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106495190A (en) * | 2016-09-12 | 2017-03-15 | 天津科技大学 | A kind of calcining of abraum salt containing lithium recovery method |
| CN106495190B (en) * | 2016-09-12 | 2018-03-09 | 天津科技大学 | A kind of calcining of abraum salt containing lithium recovery method |
| CN106989403A (en) * | 2017-03-30 | 2017-07-28 | 大丰跃龙化学有限公司 | The processing method of abraum salt in cyclopropanecarboxylic acid wastewater treatment |
| CN107128951A (en) * | 2017-06-22 | 2017-09-05 | 南京诚朴环保科技有限公司 | A kind of method of organic matter in removing inorganic salts |
| CN107128951B (en) * | 2017-06-22 | 2019-07-12 | 南京诚朴环保科技有限公司 | A kind of method of organic matter in removing inorganic salts |
| CN111112296A (en) * | 2019-12-27 | 2020-05-08 | 洛南环亚源铜业有限公司 | Resource utilization treatment method for industrial waste salt |
| CN111272946A (en) * | 2020-03-30 | 2020-06-12 | 合肥工业大学 | Device and method for measuring content of organic carbon in industrial waste salt |
| CN111471432A (en) * | 2020-04-03 | 2020-07-31 | 安徽科安废盐资源化有限公司 | Method for preparing snow-melting agent by using industrial waste miscellaneous salt |
| CN113149035A (en) * | 2020-12-29 | 2021-07-23 | 中国科学院生态环境研究中心 | Method for treating waste sodium chloride salt |
| CN113048489A (en) * | 2021-03-16 | 2021-06-29 | 上海蓄科环境工程有限公司 | Method and system for purifying and recycling industrial salt from waste salt containing organic matters |
| CN114605018A (en) * | 2022-02-04 | 2022-06-10 | 重庆大学 | Method for treating phosphorus-containing fluorine-containing high-salt organic wastewater and recycling salt |
| CN114605018B (en) * | 2022-02-04 | 2024-02-02 | 重庆大学 | Method for treating phosphorus-containing fluorine-containing high-salt organic wastewater and recovering salt |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN105883859A (en) | Waste salt treatment method | |
| CA2952395C (en) | Process and device for desulfurization-denitration of flue gas | |
| CN101455974B (en) | Tail-gas comprehensive utilization method in mercuric chloride catalyst production | |
| WO2009024014A1 (en) | Method for removing ammonia from coking waste water | |
| CN113145608A (en) | System and process for treating incineration fly ash through thermal desorption and carbon neutralization | |
| CN101745309B (en) | Flue gas desulfurization (FGD) and comprehensive utilization method for flyash pudding blast furnace slag | |
| KR20120099810A (en) | Waste to energy by way of hydrothermal decomposition and resource recycling | |
| CN105016530A (en) | Comprehensive treatment process of waste water high in concentration and high in salinity | |
| CN109500061B (en) | Method for combined utilization of incineration fly ash and bypass ash | |
| CN109647152B (en) | Method and device for purifying waste gas containing chlorine or/and sulfur | |
| CN114162837A (en) | Waste salt recycling treatment system and treatment method thereof | |
| CN113955889A (en) | Resource recovery process of fly ash washing liquid | |
| CN102441322A (en) | Method for desulfurizing flue gas and by-producing flocculant | |
| CN113754162B (en) | Method and system for recycling chloride salt through crystallization of acidic washing wastewater | |
| CN113877944A (en) | Method for treating dioxin in fly ash | |
| CN112775145A (en) | Efficient secondary washing process for household garbage incineration fly ash | |
| CN105417816A (en) | Continuous treatment method for dye industry acid wastewater | |
| CN215391554U (en) | Waste salt resourceful treatment system | |
| CN105565564A (en) | Dimethylamine waste water treatment method capable of recovering dimethyl formamide (DMF) | |
| CN115138668B (en) | Fly ash treatment method | |
| CN113754167B (en) | Method for recovering ammonia from coking wastewater | |
| CN115572004A (en) | System and method for removing heavy metals from fly ash washing liquid by coupling flue gas purification with waste incineration plant | |
| JP2020148373A (en) | PFCs-CONTAINING EXHAUST GAS TREATMENT DEVICE AND METHOD | |
| CN1225303C (en) | Method for controlling flue gas contaiing SO2 with NaCl and producing high concentratino SO2 | |
| CN212403835U (en) | Treatment system for purifying acid-making wastewater by using active coke flue gas |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| RJ01 | Rejection of invention patent application after publication | ||
| RJ01 | Rejection of invention patent application after publication |
Application publication date: 20160824 |