CN114349091B - Pyrolysis treatment process for desulfurization waste liquid - Google Patents
Pyrolysis treatment process for desulfurization waste liquid Download PDFInfo
- Publication number
- CN114349091B CN114349091B CN202111630979.7A CN202111630979A CN114349091B CN 114349091 B CN114349091 B CN 114349091B CN 202111630979 A CN202111630979 A CN 202111630979A CN 114349091 B CN114349091 B CN 114349091B
- Authority
- CN
- China
- Prior art keywords
- waste liquid
- desulfurization waste
- liquid
- pyrolysis
- desulfurization
- 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.)
- Active
Links
Classifications
-
- 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
-
- 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
-
- 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
-
- 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
- B01D53/1456—Removing acid components
- B01D53/1468—Removing hydrogen sulfide
-
- 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
- B01D53/1456—Removing acid components
- B01D53/1475—Removing carbon dioxide
-
- 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
- C02F1/025—Thermal hydrolysis
-
- 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
- C02F1/046—Treatment of water, waste water, or sewage by heating by distillation or evaporation under vacuum produced by a barometric column
-
- 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
- C02F1/048—Purification of waste water by evaporation
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K1/00—Purifying combustible gases containing carbon monoxide
- C10K1/002—Removal of contaminants
- C10K1/003—Removal of contaminants of acid contaminants, e.g. acid gas removal
- C10K1/004—Sulfur containing contaminants, e.g. hydrogen sulfide
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K1/00—Purifying combustible gases containing carbon monoxide
- C10K1/08—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors
- C10K1/10—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors with aqueous liquids
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/18—Nature of the water, waste water, sewage or sludge to be treated from the purification of gaseous effluents
-
- 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
- Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- General Chemical & Material Sciences (AREA)
- Water Supply & Treatment (AREA)
- Analytical Chemistry (AREA)
- Life Sciences & Earth Sciences (AREA)
- Environmental & Geological Engineering (AREA)
- Hydrology & Water Resources (AREA)
- Combustion & Propulsion (AREA)
- Physics & Mathematics (AREA)
- Thermal Sciences (AREA)
- Treating Waste Gases (AREA)
- Heat Treatment Of Water, Waste Water Or Sewage (AREA)
Abstract
The invention discloses a desulfurization waste liquid pyrolysis treatment process, which comprises the steps of concentrating desulfurization waste liquid, performing pyrolysis conversion by taking high-temperature superheated steam as a heat source, washing the converted tail gas by condensate obtained by evaporation of the desulfurization liquid or ammonia water obtained by ammonia evaporation, and then merging the tail gas into a VOC collection system, wherein liquid generated in the washing process enters a foam tank or a regeneration tower for sulfur recovery and then is used as the desulfurization liquid of coal gas. Compared with the prior art, the method has the outstanding advantages in terms of investment, running cost, secondary pollution generation, treatment and treatment effect, and has important significance for effective treatment of desulfurization waste liquid.
Description
Technical Field
The invention relates to a pyrolysis treatment process of desulfurization waste liquid, in particular to a wet oxidation H removal method by adopting an ammonia method aiming at coal gas 2 A treatment process of desulfurization waste liquid generated in the S process.
Background
The desulfurization waste liquid is a pollutant with great harm and contains a mixture of various toxic substances, and the mixture is listed in the national hazardous waste directory. Is the key point of environmental protection supervision, so how to effectively treat desulfurization waste liquid is a difficult problem to be solved by all enterprises adopting wet oxidation desulfurization process.
At present, the treatment process of the desulfurization waste liquid is mainly divided into three types, wherein one type is a salt extraction method represented by salt extraction, the other type is a conversion method represented by acid production, and the third type is a pyrolysis method represented by coal blending and coking.
The salt extraction method mainly adopts a certain technical means to effectively extract the ammonium thiosulfate and the ammonium thiocyanate in the desulfurization waste liquid, thereby achieving the dual purposes of saving resources and protecting the environment. At present, two methods, namely an evaporation crystallization method and a fractional crystallization method, are widely adopted in enterprises. The evaporation crystallization method is to extract mixed ammonium salt from desulfurization waste liquid by an evaporation crystallization method, and then return condensate obtained by evaporation to a desulfurization system so as to achieve the purpose of treating desulfurization waste liquid. Because the mixed ammonium salt has high toxicity and the limitation of market capacity such as ammonium thiocyanate, ammonium thiosulfate and the like, the mixed salt has no market, and the treatment and the utilization of the mixed salt are a new problem to be solved. The fractional crystallization method is to use ternary phase diagram theory and to recover ammonium thiocyanate and ammonium thiosulfate from the desulfurization waste liquid by fractional crystallization. The process comprises the steps of adding an acidification oxidation step before decoloring, decomposing and oxidizing ammonium thiosulfate in the desulfurization waste liquid, changing the original three components of the desulfurization waste liquid into a two-component solution containing only ammonium thiocyanate and ammonium sulfate, and extracting the ammonium thiocyanate and the ammonium sulfate from the desulfurization waste liquid through fractional crystallization. The optimization of the process realizes the purpose of extracting high-purity ammonium thiocyanate and ammonium sulfate from the desulfurization waste liquid. However, due to the problem of the market capacity of ammonium thiocyanate, the ammonium thiocyanate obtained in the desulfurization waste liquid cannot be sold. Meanwhile, the process also has the problems of large investment, high operation cost, secondary pollution and the like.
The first process in the conversion process is the acid making process. Because coked sulfur also has the problem of difficult sales, enterprises adopt a desulfurization waste liquid acid preparation process to treat desulfurization waste liquid and sulfur, and the process is to concentrate the desulfurization waste liquid containing sulfur, ammonium thiocyanate and ammonium thiosulfateAfter (or drying), the waste gas is burnt and decomposed in a combustion furnace together with combustion-supporting gas, and SO in the waste gas is utilized 2 Oxidation to SO 3 Then absorb SO with 95% sulfuric acid 3 98% concentrated sulfuric acid is produced and sent to an ammonium sulfate working section to be used as a raw material for producing ammonium sulfate.
The process technology can effectively treat the desulfurization waste liquid and obtain the sulfuric acid product, can be used as raw material supply of an ammonium sulfate working section, and has the greatest advantage of simultaneously treating two large pollutants of the desulfurization waste liquid and the sulfur mud. However, the process flow is complex, so that the problems of large investment, complex operation, high operation cost and the like exist. In the case of low current sulfuric acid markets, the massive application of this technology tends to exacerbate the sulfuric acid market overabundance. Meanwhile, the technology is adopted to generate dilute sulfuric acid and tail gas generated in the incineration process, which are newly added environmental protection problems.
The second process of the conversion method is to convert the desulfurization waste liquid into ammonium sulfate, and the method is to oxidize ammonium salt and sulfur in the desulfurization waste liquid into ammonium sulfate in an oxidation tower under the conditions of temperature 273-275 ℃ and pressure 7000-7500 kPa, and then send the ammonium sulfate into an ammonium sulfate working section for producing the ammonium sulfate. The method has the main problems of high requirements on equipment, large investment, high energy consumption for treating waste liquid and the like, so that the method has certain limitation on the use.
Some enterprises adopt a coal blending coking method to treat desulfurization waste liquid, the method comprises the steps of blending the waste liquid into furnace coal to carry out coking treatment, and heating and decomposing ammonium salt in the desulfurization waste liquid in the coke oven to obtain a final product NH 3 、H 2 S、CO 2 And N 2 Enters a subsequent coal-based purifying system along with raw gas, wherein only a small amount of H 2 S reacts with coke chemically, thereby achieving the purpose of treating desulfurization waste liquid. The method is widely used by coking enterprises, and some enterprises try to optimize and improve the method by means of uniform spraying, mixing by a mixer, spraying into a coal charging tower and the like, but the final treatment method is the same as that of direct dumping in a coal plant, and is basically indistinguishable. The method has the problems of influencing the moisture of the coal entering the furnace, influencing the coke quality, having poor working environment of workers and the like. Especially with the existingThe defect of the method for treating the desulfurization waste liquid is further developed when the large coal yard closed engineering is comprehensively implemented, and enterprises discard the method for treating the desulfurization waste liquid.
In conclusion, the main salts in the desulfurization waste liquid generated in the wet oxidation desulfurization process by the ammonia method are (NH) 4 ) 2 S 2 O 3 ，NH 4 SCN and (NH) 4 ) 2 SO 4 However, the salt has poor thermal stability, and no economical and effective desulfurization waste liquid treatment method exists at present.
Disclosure of Invention
In order to solve the problems, the invention provides a pyrolysis treatment process for desulfurization waste liquid, which can effectively solve the problems of large investment, high operation cost, serious secondary pollution and the like in the existing treatment process.
Aiming at the characteristics of poor thermal stability of pollutants in ammonia desulfurization waste liquid, the invention firstly concentrates the desulfurization waste liquid, then uses high-temperature superheated steam as a heat source to carry out pyrolysis conversion, and the converted tail gas is used as a desulfurizing liquid of coal gas after being subjected to washing treatment of condensate obtained by evaporating the desulfurizing liquid or ammonia water obtained by evaporating ammonia and then is merged into a VOC collecting system, and liquid generated in the washing process enters a foam tank or a regeneration tower to carry out sulfur recovery. The process is simple in process, flexible in operation, free of secondary pollution, and has outstanding advantages in investment, running cost, secondary pollution generation and treatment effect compared with the prior art.
The invention provides a pyrolysis treatment process of desulfurization waste liquid, which comprises the following steps:
(1) The desulfurization waste liquid is firstly evaporated and concentrated in a concentrating kettle or an evaporator, saturated steam with the pressure of 0.2-0.5MPa or waste heat of tail gas generated by pyrolysis of the desulfurization waste liquid is used as a heat source in the evaporation process, the salt content in the concentrated liquid after concentration is controlled to be 400-600g/L, and condensate generated in the concentration process is fed into a washing tower for washing and purifying the tail gas. In order to improve the evaporation efficiency, the concentration process is carried out under vacuum condition, and the vacuum degree is 0.05-0.09MPa.
(2) Spraying the concentrated desulfurization waste liquid into a pyrolysis furnace in a form of mist or liquid drops for pyrolysis, wherein the mass ratio of the superheated steam to the desulfurization waste liquid is 0.5-1 in the pyrolysis process, the superheated steam with the temperature of 500-800 ℃ is used as a heat source, a steam superheat pipe is arranged at the upper part of the pyrolysis furnace in the process, a nozzle for the desulfurization waste liquid is arranged at the middle part of the pyrolysis furnace, and a high-temperature-resistant filler layer and a superheated steam distributor are arranged at the bottom of the pyrolysis furnace; the superheated steam is produced with saturated steam of 0.2-0.5MPa as material and through preheating the steam to 200-400 deg.c in the steam superheating pipe, introducing into the steam heating furnace, superheating the steam to 500-800 deg.c in the gas, electric heating or afterheat of the enterprise, and introducing into the pyrolyzing furnace.
(3) The gas generated after the pyrolysis of the desulfurization waste liquid is subjected to primary cooling through a steam superheating pipe, the cooled gas is introduced into the evaporator or the concentrating kettle in the step (1) for secondary cooling, and meanwhile, the heat supply in the desulfurization waste liquid concentrating process is realized. The gas-water mixture discharged from the evaporator or the concentrating kettle is introduced into the middle lower part of a washing tower, the washing tower is in the form of an air spraying tower or a packing tower, the washing liquid used in the washing process is condensate obtained by evaporating and concentrating the desulfurization waste liquid, the washing liquid is pumped from the middle lower part of the washing tower for recycling, part of liquid is periodically pumped from the bottom of the washing tower and is introduced into a regeneration tower or a foam tank of a desulfurization section, and the tail gas at the top of the washing tower is introduced into a VOC tail gas purification system of the desulfurization section of an enterprise.
The invention has the beneficial effects that:
the invention provides a pyrolysis treatment process of desulfurization waste liquid, which takes superheated steam as a heat source, and NH generated after pyrolysis of the desulfurization waste liquid 3 、H 2 S、CO 2 And N 2 The tail gas after washing enters a VOC tail gas collecting system for further treatment and then is discharged after reaching the standard, and the liquid generated in the washing process enters a foam tank or a regeneration tower for sulfur recovery and then is used as a desulfurizing liquid of coal gas. Compared with the prior art, the method has the outstanding advantages in terms of investment, running cost, secondary pollution generation, treatment and treatment effect, and has important significance for effective treatment of desulfurization waste liquid.
Drawings
FIG. 1 is a diagram of a pyrolysis treatment process for desulfurization waste liquid.
Detailed Description
The present invention is further illustrated by, but not limited to, the following examples.
Referring to fig. 1, the pyrolysis treatment process of the desulfurization waste liquid provided by the invention comprises the following steps:
(1) The desulfurization waste liquid is firstly evaporated and concentrated in a concentrating kettle or an evaporator, saturated steam with the pressure of 0.2-0.5MPa or waste heat of tail gas generated by pyrolysis of the desulfurization waste liquid is used as a heat source in the evaporation process, the salt content in the concentrated liquid after concentration is controlled at 400-600g/L, and condensate liquid generated in the concentration process is fed into a washing tower for washing and purifying the tail gas. In order to improve the evaporation efficiency, the concentration process is carried out under vacuum condition, and the vacuum degree is 0.05-0.09MPa.
(2) Spraying the concentrated desulfurization waste liquid into a pyrolysis furnace in a form of mist or liquid drops for pyrolysis, wherein the mass ratio of the superheated steam to the desulfurization waste liquid in the pyrolysis process is 0.5-1, the superheated steam with the temperature of 500-800 ℃ is used as a heat source, a steam superheat pipe is arranged at the upper part of the pyrolysis furnace in the process, a nozzle for the desulfurization waste liquid is arranged at the middle part of the pyrolysis furnace, and a high-temperature-resistant filler layer and a superheated steam distributor are arranged at the bottom of the pyrolysis furnace; the superheated steam is produced with saturated steam of 0.2-0.5MPa as material and through preheating the steam to 200-400 deg.c in the steam superheating pipe, introducing into the steam heating furnace, superheating the steam to 500-800 deg.c in the gas, electric heating or afterheat of the enterprise, and introducing into the pyrolyzing furnace.
(3) The generated gas after the desulfurization waste liquid is pyrolyzed by the pyrolysis furnace is initially cooled by a steam superheating pipe, the cooled gas is introduced into the evaporator or the concentrating kettle in the step (1) for secondary cooling, and meanwhile, the heat supply in the desulfurization waste liquid concentrating process is realized. The gas-water mixture discharged from the evaporator or the concentrating kettle is introduced into the middle lower part of a washing tower, the washing tower is in the form of an air spraying tower or a packing tower, the washing liquid used in the washing process is condensate obtained by evaporating and concentrating the desulfurization waste liquid, the washing liquid is pumped from the middle lower part of the washing tower for recycling, part of liquid is periodically pumped from the bottom of the washing tower and is introduced into a regeneration tower or a foam tank of a desulfurization section, and the tail gas at the top of the washing tower is introduced into a VOC tail gas purification system of the desulfurization section of an enterprise.
The process flow of the invention is illustrated by the following specific examples:
example 1:
the salt content collected from the gas desulfurization section of a coking enterprise is 256g/L (NH) 4 SCN 162g/L，(NH 4 ) 2 S 2 O 3 74g/L,(NH 4 ) 2 SO 4 20 g/L), concentrating 100L of the desulfurization waste liquid in an evaporation kettle, generating 56L of condensate in the concentration process, increasing the salt content in the concentrate to 581g/L, spraying the concentrate into a pyrolysis furnace through an ejector within one hour, introducing superheated steam with the temperature of 760 ℃ and the flow of 60Kg/h into the pyrolysis furnace from the bottom, directly exchanging heat between the superheated steam and the sprayed desulfurization waste liquid, discharging a gaseous mixture formed by pyrolysis of the desulfurization waste liquid from the top of the pyrolysis furnace, sequentially passing through a steam preheater, the evaporation kettle and a washing tower in the discharging process, and circularly washing the inside of the washing tower by using condensate generated in the evaporation process. Saturated steam of 0.2MPa is preheated to 350 ℃ by a steam preheater, then enters a steam heating furnace to be heated to 760 ℃ and enters from the bottom of the pyrolysis furnace. Finally, the washing liquid in the washing tower is filtered and then analyzed, 7.6kg of elemental sulfur is produced in the filtering process, and NH in the liquid 4 SCN 10.13g/L，(NH 4 ) 2 S 2 O 3 1.05g/L,(NH 4 ) 2 SO 4 1.88g/L。
Example 2:
the salt content collected from the gas desulfurization section of a coking enterprise is 256g/L (NH) 4 SCN 162g/L，(NH 4 ) 2 S 2 O 3 74g/L,(NH 4 ) 2 SO 4 20 g/L), concentrating 100L of the desulfurization waste liquid in an evaporation kettle, generating 42L of condensate in the concentration process, increasing the salt content in the concentrate to 441g/L, spraying the concentrate into a pyrolysis furnace through an ejector within one hour, introducing superheated steam with the temperature of 560 ℃ and the flow of 80Kg/h into the pyrolysis furnace from the bottom, directly exchanging heat between the superheated steam and the sprayed desulfurization waste liquid, discharging a gaseous mixture formed by pyrolysis of the desulfurization waste liquid from the top of the pyrolysis furnace, sequentially passing through a steam preheater, the evaporation kettle and a washing tower in the discharging process, and discharging the gaseous mixture in the washing towerThe condensate generated in the evaporation process is used for circulation washing. Saturated steam of 0.2MPa is preheated to 280 ℃ by a steam preheater, then enters a steam heating furnace to be heated to 660 ℃ and enters from the bottom of the pyrolysis furnace. Finally, the washing liquid in the washing tower is filtered and then analyzed, 6.9kg of elemental sulfur is produced in the filtering process, and NH in the liquid 4 SCN 13.50g/L，(NH 4 ) 2 S 2 O 3 4.18g/L，(NH 4 ) 2 SO 4 2.22g/L。
Claims (4)
1. A desulfurization waste liquid pyrolysis treatment process is characterized in that: is aimed at adopting ammonia wet oxidation to remove H 2 The treatment process of the desulfurization waste liquid generated in the S process comprises the steps of concentrating the desulfurization waste liquid, then using high-temperature superheated steam as a heat source to carry out pyrolysis conversion on the desulfurization waste liquid, washing the converted tail gas by condensate obtained by evaporation of the desulfurization liquid or ammonia water obtained by evaporation of ammonia, and then merging the tail gas into a VOC collection system, wherein the liquid generated in the washing process enters a foam tank or a regeneration tower to carry out sulfur recovery and then is used as the desulfurization liquid of coal gas;
the desulfurization waste liquid pyrolysis treatment process comprises the following steps:
(1) The desulfurization waste liquid is firstly evaporated and concentrated in a concentrating kettle or an evaporator, saturated steam with the pressure of 0.2-0.5MPa or waste heat of tail gas generated by pyrolysis of the desulfurization waste liquid is used as a heat source in the evaporation process, the salt content in the concentrated liquid after concentration is controlled to be 400-600g/L, and condensate liquid generated in the concentration process is fed into a washing tower for washing and purifying the tail gas;
(2) Spraying the concentrated desulfurization waste liquid into a pyrolysis furnace in the form of liquid drops for pyrolysis, wherein superheated steam is used as a heat source in the pyrolysis process, the mass ratio of the superheated steam to the desulfurization waste liquid is 0.5-1, and the temperature is 500-800 ℃;
the superheated steam takes saturated steam of 0.2-0.5MPa of enterprises as raw materials, a steam superheating pipe preheats the steam to 200-400 ℃, then a steam heating furnace is introduced, and the steam is superheated to 500-800 ℃ by gas, electric heating or enterprise waste heat and then introduced into a pyrolysis furnace;
(3) The gas generated after the pyrolysis of the desulfurization waste liquid is subjected to primary cooling through a steam superheating pipe, and the cooled gas is introduced into an evaporator or a concentrating kettle for secondary cooling, so that the heat supply in the desulfurization waste liquid concentrating process is realized; the gas-water mixture discharged from the evaporator or the concentrating kettle is introduced into the middle lower part of the washing tower, the washing liquid used in the washing process is condensate obtained by evaporating and concentrating the desulfurization waste liquid, the washing liquid is pumped from the middle lower part of the washing tower for recycling, part of liquid is periodically pumped from the bottom of the washing tower and is introduced into a regeneration tower or a foam tank of the desulfurization section, and the tail gas at the top of the washing tower is introduced into a VOC tail gas purification system of the desulfurization section of an enterprise.
2. The desulfurization waste liquid pyrolysis treatment process according to claim 1, wherein: in the step (1), the concentration process is carried out under vacuum condition, and the vacuum degree is 0.05-0.09MPa.
3. The desulfurization waste liquid pyrolysis treatment process according to claim 1, wherein: in the step (2), a steam superheating pipe is arranged at the upper part of the pyrolysis furnace, a nozzle for desulfurizing waste liquid is arranged at the middle part of the pyrolysis furnace, and a high-temperature-resistant filler layer and a superheated steam distributor are arranged at the bottom of the pyrolysis furnace.
4. The desulfurization waste liquid pyrolysis treatment process according to claim 1, wherein: in the step (3), the washing tower is an air-jet tower or a packed tower.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202111630979.7A CN114349091B (en) | 2021-12-29 | 2021-12-29 | Pyrolysis treatment process for desulfurization waste liquid |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202111630979.7A CN114349091B (en) | 2021-12-29 | 2021-12-29 | Pyrolysis treatment process for desulfurization waste liquid |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN114349091A CN114349091A (en) | 2022-04-15 |
| CN114349091B true CN114349091B (en) | 2023-10-13 |
Family
ID=81104194
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202111630979.7A Active CN114349091B (en) | 2021-12-29 | 2021-12-29 | Pyrolysis treatment process for desulfurization waste liquid |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN114349091B (en) |
Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| IE921844A1 (en) * | 1992-06-08 | 1993-12-15 | Mason James A | Method and apparatus for treating water and/or wastewater |
| CN102503031A (en) * | 2011-11-08 | 2012-06-20 | 太原理工大学 | Treatment technique of coking desulfurization liquid waste |
| CN105236647A (en) * | 2015-09-25 | 2016-01-13 | 太原理工大学 | Method used for pyrolyzing wet oxidation desulfurization mixed waste liquid in partial oxidation environment |
| CN205965449U (en) * | 2016-08-10 | 2017-02-22 | 中冶华天工程技术有限公司 | Coking desulfurization liquid waste processing system |
| CN108217690A (en) * | 2018-03-14 | 2018-06-29 | 湖南华菱涟源钢铁有限公司 | Process for extracting secondary salt from desulfurization waste liquid |
| CN110921953A (en) * | 2019-12-06 | 2020-03-27 | 太原理工大学 | Resource treatment process and device for coking desulfurization waste liquid |
| CN112125319A (en) * | 2020-09-01 | 2020-12-25 | 太原理工大学 | Process for recovering all components of desulfurization waste liquid |
| CN113028408A (en) * | 2021-03-30 | 2021-06-25 | 威尔能环保科技(苏州)有限公司 | Process and device for treating solid waste by high-temperature steam pyrolysis |
-
2021
- 2021-12-29 CN CN202111630979.7A patent/CN114349091B/en active Active
Patent Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| IE921844A1 (en) * | 1992-06-08 | 1993-12-15 | Mason James A | Method and apparatus for treating water and/or wastewater |
| CN102503031A (en) * | 2011-11-08 | 2012-06-20 | 太原理工大学 | Treatment technique of coking desulfurization liquid waste |
| CN105236647A (en) * | 2015-09-25 | 2016-01-13 | 太原理工大学 | Method used for pyrolyzing wet oxidation desulfurization mixed waste liquid in partial oxidation environment |
| CN205965449U (en) * | 2016-08-10 | 2017-02-22 | 中冶华天工程技术有限公司 | Coking desulfurization liquid waste processing system |
| CN108217690A (en) * | 2018-03-14 | 2018-06-29 | 湖南华菱涟源钢铁有限公司 | Process for extracting secondary salt from desulfurization waste liquid |
| CN110921953A (en) * | 2019-12-06 | 2020-03-27 | 太原理工大学 | Resource treatment process and device for coking desulfurization waste liquid |
| CN112125319A (en) * | 2020-09-01 | 2020-12-25 | 太原理工大学 | Process for recovering all components of desulfurization waste liquid |
| CN113028408A (en) * | 2021-03-30 | 2021-06-25 | 威尔能环保科技(苏州)有限公司 | Process and device for treating solid waste by high-temperature steam pyrolysis |
Non-Patent Citations (1)
| Title |
|---|
| HPF焦化脱硫废液资源化处理技术开发;李国强等;《工业水处理》;20130920;第33卷(第9期);第10-15页 * |
Also Published As
| Publication number | Publication date |
|---|---|
| CN114349091A (en) | 2022-04-15 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN109052335B (en) | Method for preparing liquid sulfur dioxide and sulfuric acid by reducing waste sulfuric acid with sulfur gas | |
| CN102229806B (en) | Green circular economy technology with coal coking as the main part | |
| CN103521060B (en) | Method for desulfurization of sulfur recovery tail gas by using boiler flue gas ammonia method | |
| CN103274367B (en) | Method for extracting two secondary salts from desulfurized salt-containing waste liquid of coke oven gas | |
| CN105214478A (en) | The integral process of a kind of coke oven flue exhuast gas desulfurization denitration and waste heat recovery | |
| CN202063875U (en) | Green circulation economy type coal coking process device | |
| CN105236647B (en) | Method used for pyrolyzing wet oxidation desulfurization mixed waste liquid in partial oxidation environment | |
| CN106082137B (en) | A kind of system and technique for comprehensively utilizing coking low-quality sulfur and doctor solution secondary salt | |
| CN103264991B (en) | Method for processing sulfur paste as coke oven gas desulfuration by-product | |
| CN114620692B (en) | Process for preparing sulfuric acid by coking desulfurization foam sulfur melting and desulfurization waste liquid melting method salt extraction and mixed firing | |
| CN201658945U (en) | Sintering flue gas purification system based on heat pipe waste heat recovery technology | |
| CN109607575A (en) | A method of sodium pyrosulfite is produced using coking desulfurization waste liquor and thick sulphur | |
| CN113979411A (en) | Process for preparing acid from coking desulfurization waste salt and crude sulfur | |
| CN111760457A (en) | Method and equipment for regenerating waste salt generated in flue gas desulfurization | |
| CN111071995A (en) | Method for preparing industrial sulfuric acid by using sulfur-containing waste liquid | |
| CN110332552B (en) | Resourceful treatment system and method for chlorine-sulfur-containing organic waste liquid | |
| CN114349091B (en) | Pyrolysis treatment process for desulfurization waste liquid | |
| WO2023226473A1 (en) | Cooperative utilization system for coal gangue power generation and co2 mineralization and working method | |
| CN210523361U (en) | Waste salt resourceful treatment processing system | |
| CN114349090B (en) | Coking desulfurization waste liquid harmless treatment process | |
| CN110683520B (en) | Process for preparing sulfuric acid by regenerating low-concentration dilute waste sulfuric acid | |
| CN107311117B (en) | Clean production process and device for combined treatment of sulfur recovery and alkylated waste acid | |
| CN104353351A (en) | Industrial preparation method for preparing sodium hydrogen carbonate for smoke purification from waste alkali | |
| CN212492410U (en) | Flue gas desulfurization waste salt regeneration equipment | |
| CN112342392B (en) | Method for respectively recovering titanium, tungsten and vanadium from waste denitration catalyst |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |