CN112110423A - System and method for preparing acid from desulfurization waste liquid - Google Patents
System and method for preparing acid from desulfurization waste liquid Download PDFInfo
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- CN112110423A CN112110423A CN202011210936.9A CN202011210936A CN112110423A CN 112110423 A CN112110423 A CN 112110423A CN 202011210936 A CN202011210936 A CN 202011210936A CN 112110423 A CN112110423 A CN 112110423A
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- 238000000034 method Methods 0.000 title claims abstract description 70
- 239000002253 acid Substances 0.000 title claims abstract description 51
- 238000006477 desulfuration reaction Methods 0.000 title claims abstract description 39
- 230000023556 desulfurization Effects 0.000 title claims abstract description 39
- 239000007788 liquid Substances 0.000 title claims abstract description 33
- 239000002699 waste material Substances 0.000 title claims abstract description 32
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 claims abstract description 84
- 239000000706 filtrate Substances 0.000 claims abstract description 39
- 238000000746 purification Methods 0.000 claims abstract description 37
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims abstract description 35
- 239000011593 sulfur Substances 0.000 claims abstract description 35
- 229910052717 sulfur Inorganic materials 0.000 claims abstract description 35
- 238000006243 chemical reaction Methods 0.000 claims abstract description 31
- 238000010521 absorption reaction Methods 0.000 claims abstract description 25
- 238000011084 recovery Methods 0.000 claims abstract description 20
- 238000004537 pulping Methods 0.000 claims abstract description 12
- 238000002156 mixing Methods 0.000 claims abstract description 9
- 238000003860 storage Methods 0.000 claims abstract description 8
- 238000006386 neutralization reaction Methods 0.000 claims abstract description 7
- 239000007789 gas Substances 0.000 claims description 47
- 239000002918 waste heat Substances 0.000 claims description 24
- 238000005406 washing Methods 0.000 claims description 23
- 239000002002 slurry Substances 0.000 claims description 19
- 238000001816 cooling Methods 0.000 claims description 16
- 238000001035 drying Methods 0.000 claims description 13
- 238000004519 manufacturing process Methods 0.000 claims description 8
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 5
- 239000003054 catalyst Substances 0.000 claims description 4
- 150000003839 salts Chemical class 0.000 claims description 3
- 229910052720 vanadium Inorganic materials 0.000 claims description 3
- LEONUFNNVUYDNQ-UHFFFAOYSA-N vanadium atom Chemical compound [V] LEONUFNNVUYDNQ-UHFFFAOYSA-N 0.000 claims description 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 abstract description 12
- 238000004140 cleaning Methods 0.000 abstract description 8
- 229910021529 ammonia Inorganic materials 0.000 abstract description 6
- 238000002360 preparation method Methods 0.000 abstract description 5
- 239000002994 raw material Substances 0.000 abstract description 5
- 235000011149 sulphuric acid Nutrition 0.000 abstract 1
- 239000001117 sulphuric acid Substances 0.000 abstract 1
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 description 24
- 238000005507 spraying Methods 0.000 description 8
- 238000005516 engineering process Methods 0.000 description 5
- 239000006260 foam Substances 0.000 description 5
- 150000003863 ammonium salts Chemical class 0.000 description 4
- 239000000843 powder Substances 0.000 description 4
- 239000000571 coke Substances 0.000 description 3
- 230000007547 defect Effects 0.000 description 3
- SOIFLUNRINLCBN-UHFFFAOYSA-N ammonium thiocyanate Chemical compound [NH4+].[S-]C#N SOIFLUNRINLCBN-UHFFFAOYSA-N 0.000 description 2
- XYXNTHIYBIDHGM-UHFFFAOYSA-N ammonium thiosulfate Chemical compound [NH4+].[NH4+].[O-]S([O-])(=O)=S XYXNTHIYBIDHGM-UHFFFAOYSA-N 0.000 description 2
- 238000007599 discharging Methods 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 239000000047 product Substances 0.000 description 2
- 238000010306 acid treatment Methods 0.000 description 1
- 239000003513 alkali Substances 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 238000010924 continuous production Methods 0.000 description 1
- 239000000498 cooling water Substances 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000000428 dust Substances 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 230000007774 longterm Effects 0.000 description 1
- 239000003595 mist Substances 0.000 description 1
- 230000003472 neutralizing effect Effects 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 230000001502 supplementing effect Effects 0.000 description 1
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Classifications
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B17/00—Sulfur; Compounds thereof
- C01B17/69—Sulfur trioxide; Sulfuric acid
- C01B17/74—Preparation
- C01B17/76—Preparation by contact processes
- C01B17/80—Apparatus
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B17/00—Sulfur; Compounds thereof
- C01B17/48—Sulfur dioxide; Sulfurous acid
- C01B17/50—Preparation of sulfur dioxide
- C01B17/501—Preparation of sulfur dioxide by reduction of sulfur compounds
- C01B17/504—Preparation of sulfur dioxide by reduction of sulfur compounds of ammonium sulfates
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B17/00—Sulfur; Compounds thereof
- C01B17/48—Sulfur dioxide; Sulfurous acid
- C01B17/50—Preparation of sulfur dioxide
- C01B17/54—Preparation of sulfur dioxide by burning elemental sulfur
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B17/00—Sulfur; Compounds thereof
- C01B17/48—Sulfur dioxide; Sulfurous acid
- C01B17/50—Preparation of sulfur dioxide
- C01B17/56—Separation; Purification
Abstract
The invention provides a system and a method for preparing acid from desulfurization waste liquid, and relates to the field of acid preparation. The system comprises a pretreatment unit, a concentration unit, a pulping unit, an incineration unit, a purification unit and a dry absorption conversion unit, wherein a dilute sulfuric acid outlet in the purification unit is connected with a filtrate storage tank in the pretreatment unit for storing the filtrate. The acid preparation method comprises the following steps: a pretreatment step of separating a desulfurization waste liquid from a desulfurization unit into a sulfur paste and a filtrate, a concentration step of concentrating the filtrate to obtain a concentrated solution, a pulp making step of mixing the sulfur paste and the concentrated solution to prepare a pulp, and a step of burning the pulp with SO2Incineration process of gas and SO2Cleaning process for cleaning gas and SO after cleaning2Preparation of concentrated sulfuric acid from gasAnd in the dry absorption conversion process, dilute sulfuric acid generated in the purification process is returned to the filtrate for neutralization. The method directly makes dilute sulphuric acid and ammonia contained in the filtrate generate neutralization reaction, and further obtains raw material SO by burning2And the sulfur recovery rate and the concentrated sulfuric acid yield are improved.
Description
Technical Field
The invention relates to the field of acid preparation, in particular to a system and a method for preparing acid from desulfurization waste liquid.
Background
At present, technologies for preparing industrial sulfuric acid by using desulfurization waste liquid and sulfur paste generated by a coke oven gas desulfurization system of a coke-oven plant as raw materials can be roughly divided into two types: the first type is that the sulfur foam is dried to be changed into mixture dry powder of sulfur, ammonium thiocyanate and ammonium thiosulfate, and then the mixture dry powder of the sulfur, the ammonium thiocyanate and the ammonium thiosulfate is sprayed into an incinerator to be combusted to prepare sulfur dioxide for producing sulfuric acid. The process has the following defects: firstly, the drying system is huge and the investment is high; secondly, the sulfur foam contains about 90% of water, and a large amount of energy is consumed for drying the sulfur foam, so that the energy consumption is high; thirdly, dry powder enters the incinerator, so that dry powder which is not completely combusted is easily generated and is further taken out of the incinerator to enter a subsequent waste heat recovery system, and the blockage of the waste heat recovery system is caused. Due to the defects, the process has high failure rate and cannot realize long-term continuous production.
And the second type is that a slurry spraying burning method process is adopted, sulfur paste obtained by centrifuging sulfur foam recovered in the desulfurization process through a centrifugal machine and part of concentrated desulfurization waste liquid are prepared into slurry containing about 50-60% of water, coke oven gas is used as fuel to burn and oxidize the sulfur slurry at high temperature, ammonium salt substances contained in the slurry can be decomposed and oxidized into furnace gas containing sulfur dioxide at high temperature, and then the furnace gas is subjected to purification, drying, conversion, absorption and other processes to prepare the industrial sulfuric acid. The method is adopted more abroad, the process is mature, and the method and the wet desulphurization are collectively called as an FRC process. Compared with the first type of process, the process does not need a huge drying system, has low failure rate and can be continuously operated for a long time. In addition, the process treats the sulfur foam and the desulfurization waste liquid together to prepare an industrial sulfuric acid product, no waste liquid treatment facility is needed, the process is continuous, the automation degree is high, and the sulfuric acid product with good quality can be produced. The process has the main defects that a large amount of moisture contained in the slurry is condensed in the purification process, and a large amount of dilute sulfuric acid is directly discharged and is not recycled, so that secondary pollution and resource waste are caused.
Disclosure of Invention
The invention aims to solve the technical problem of providing a system and a method for preparing acid from desulfurization waste liquid, and solving the problems that dilute sulfuric acid generated in a purification working section cannot be directly utilized to form secondary pollution, resource waste and the like when acid is prepared by adopting a slurry-spraying incineration process in the prior art.
In order to solve the technical problems, the technical scheme adopted by the invention is as follows:
a desulfurization waste liquid acid making system comprises a pretreatment unit for separating desulfurization waste liquid from a desulfurization unit into sulfur paste and filtrate, a concentration unit for concentrating the filtrate to obtain concentrated solution, a pulping unit for mixing the sulfur paste and the concentrated solution to prepare slurry, and a slurry incineration SO2Incineration unit of gas and for SO2Purification unit for washing gas and SO purified2A dry absorption conversion unit for preparing concentrated sulfuric acid from gas; a dilute sulfuric acid outlet in the purification unit is connected with a filtrate storage tank which is used for storing the filtrate in the pretreatment unit; dilute sulfuric acid produced by the purification unit is directly discharged to a filtrate storage tank in the pretreatment unit through a dilute acid return technology, and directly generates a neutralization reaction with ammonia in the filtrate to generate ammonium salt, and further obtains raw material SO required by the post-unit through incineration2The method improves the sulfur recovery rate and the yield of concentrated sulfuric acid, does not need to be discharged outside, does not form secondary pollution, completely stands by the device to treat the dilute sulfuric acid, and improves the resource utilization efficiency.
The purification unit comprises a washing tower, a cooling tower and a demister which are connected in sequence; and the washing tower and the cooling tower are sprayed and washed by circulating dilute acid.
The acid making system also comprises a waste heat recovery unit positioned between the incineration unit and the purification unit; the waste heat recovery unit comprises a waste heat boiler and an air preheater which are connected in sequence; the air preheater comprises a high-temperature air preheater and a low-temperature air preheater which are connected.
A centrifugal machine is arranged in the pretreatment unit, and an incinerator is arranged in the incineration unit; the temperature of the incinerator is 1050-1150 ℃.
The dry absorption conversion unit is internally provided with sequentially connected dry SO2Drying tower of (2), SO2Conversion to SO3Of SO, converting the SO3An absorption tower for converting the SO into concentrated sulfuric acid and an acid tank for storing the concentrated sulfuric acid, wherein the conversion tower is filled with the SO2Conversion to SO3The vanadium-based catalyst of (1).
The invention also provides a method for preparing acid from the desulfurization waste liquid, which comprises the following steps: a pretreatment step of separating a desulfurization waste liquid from a desulfurization unit into a sulfur paste and a filtrate, a concentration step of concentrating the filtrate to obtain a concentrated solution, a pulp making step of mixing the sulfur paste and the concentrated solution to prepare a pulp, and a step of burning the pulp with SO2Incineration process of gas and SO2Cleaning process for cleaning gas and SO after cleaning2A dry absorption conversion process for preparing concentrated sulfuric acid from gas; dilute sulfuric acid generated in the purification process is introduced into the filtrate for neutralization; dilute sulfuric acid produced in the purification process is directly discharged to a filtrate storage tank in the pretreatment process through a dilute acid recycling technology, is directly subjected to neutralization reaction with ammonia in the filtrate to generate ammonium salt, and is further incinerated to obtain raw material SO required by the subsequent process2The method improves the sulfur recovery rate and the yield of concentrated sulfuric acid, does not need to be discharged outside, does not form secondary pollution, completely stands by the device to treat the dilute sulfuric acid, and improves the resource utilization efficiency.
The salt content in the concentrated solution is 30-60% of the mass of the concentrated solution;
the mass ratio of the concentrated solution to the sulfur paste in the pulping process is 1: 1-4: 1.
The incineration temperature in the incineration procedure is 1000-1300 ℃.
In the purification step, SO is added2Gas passes through the washing tower, the cooling tower and the demister in sequence, and SO is generated in the washing and cooling processes2Small amount of SO contained in gas3Reacting with water to produce dilute sulfuric acid.
The mass concentration of the dilute sulfuric acid is 1-10%;
carrying out the purification workChronological SO2The flow velocity of the gas is 5-20 m/s.
The acid production method further includes a waste heat recovery step performed before the purification step: SO prepared in the burning process2The gas passes through the waste heat boiler and the air preheater in turn, and passes through SO of the waste heat boiler2The temperature of the gas is reduced to 450-650 ℃, and SO passes through an air preheater2The gas temperature is reduced to 280-350 ℃;
the air preheater comprises a high-temperature air preheater and a low-temperature air preheater which are connected, and SO2The gas passes through the high-temperature air preheater and the low-temperature air preheater in sequence.
When the dry absorption conversion process is carried out, wet SO after washing is firstly carried out2Introducing into a drying tower for drying, and collecting dried SO2Catalytic conversion to SO in a conversion column3Said SO3The concentrated sulfuric acid is generated by absorption in an absorption tower and then enters an acid tank.
The invention has the beneficial effects that:
(1) according to the method for preparing acid from desulfurization waste liquid, the dilute sulfuric acid generated in the purification process is directly discharged to the filtrate storage tank in the pretreatment process through the dilute acid blending technology without discharging, so that secondary pollution is not caused, the dilute sulfuric acid is completely treated by the device, and the resource utilization efficiency is improved;
(2) the invention provides a method for preparing acid from desulfurization waste liquid, which comprises the steps of neutralizing dilute sulfuric acid which cannot be treated in the original purification process with ammonia contained in filtrate to generate ammonium salt, and further incinerating to obtain raw material SO required by the subsequent process2The sulfur recovery rate and the yield of concentrated sulfuric acid are improved, and the yield of the concentrated sulfuric acid can be increased by 3-5%;
(3) the invention provides a method for preparing acid from desulfurization waste liquid, which utilizes ammonia contained in filtrate to neutralize dilute sulfuric acid without additionally supplementing alkali source;
(4) the waste heat recovery process effectively recycles the high-temperature SO obtained in the incineration process2Medium heat energy, reducing SO2The temperature is reduced, so that the damage to equipment in the purification process is reduced;
(5) the invention provides a method for preparing acid from desulfurization waste liquid, which has the advantages of simple process flow of the byproduct dilute acid treatment process in the purification process, only increased treatment capacity of a concentration unit, less investment, high sulfur recovery rate and environmental friendliness compared with the slurry spraying incineration process, and is easy to implement for the technical improvement of the put-into-production slurry spraying incineration process.
Drawings
FIG. 1: the invention discloses a process schematic diagram for preparing acid from desulfurization waste liquid.
Detailed Description
The invention is further described with reference to the following figures and specific embodiments.
Examples
As shown in FIG. 1, the desulfurization waste liquid acid production system comprises a pretreatment unit for separating desulfurization waste liquid from a desulfurization unit into sulfur paste and filtrate, a concentration unit for concentrating the filtrate to obtain a concentrated solution, a pulping unit for mixing the sulfur paste and the concentrated solution to prepare a slurry, and a SO incineration unit for incinerating the slurry2Incineration unit of gas, to SO2Cleaning unit for cleaning gas and SO cleaned by the same2The system comprises a dry absorption conversion unit for preparing concentrated sulfuric acid from gas and a waste heat recovery unit positioned between an incineration unit and a purification unit. The dilute sulfuric acid outlet in the purification unit is connected with a filtrate storage tank for storing filtrate in the pretreatment unit, a centrifugal machine for separating sulfur paste and filtrate is arranged in the pretreatment unit, and an incinerator is arranged in the incineration unit. Be equipped with the branch road of sending unnecessary filtrating back to desulfurization unit on the pipeline between pretreatment unit and the filtrating storage tank, further improve the utilization efficiency of filtrating.
The purification unit comprises a washing tower, a cooling tower and a demister which are connected in sequence, wherein the washing tower and the cooling tower are sprayed and washed by circulating dilute acid. The waste heat recovery unit comprises a waste heat boiler and an air preheater which are sequentially connected, and the air preheater comprises a high-temperature air preheater and a low-temperature air preheater which are connected. The dry absorption conversion unit is internally provided with sequentially connected dry SO2Drying tower of (2), SO2Conversion to SO3Conversion tower for converting SO3An absorption tower for converting the SO into concentrated sulfuric acid and an acid tank for storing the concentrated sulfuric acid, wherein the conversion tower is filled with the SO2Conversion to SO3The vanadium-based catalyst of (1).
The method for preparing the acid from the desulfurization waste liquid in the acid preparation system comprises the following steps:
(1) separating the desulfurization waste liquid from the desulfurization unit into sulfur paste and filtrate; (2) concentrating the filtrate through a concentration process to obtain a concentrated solution; (3) mixing the sulfur paste and the concentrated solution through a pulping process to prepare a slurry; (4) incinerating the slurry to obtain SO2A gas; (5) to SO obtained by incineration2The gas is subjected to heat recovery through a waste heat recovery process; (6) SO after waste heat recovery2Washing the gas through a purification process; (7) purifying the SO2The gas is made into concentrated sulfuric acid through a dry absorption conversion process.
The desulfurization waste liquid is separated into sulfur paste and filtrate through a centrifugal machine, the separated filtrate is partially used for preparing concentrated solution, and redundant filtrate is sent back to a desulfurization system for use. The salt content of the concentrated solution obtained in the concentration procedure is 30-60% of the mass of the concentrated solution, the mass ratio of the concentrated solution to the sulfur paste in the pulping procedure is 1: 1-4: 1, and the incineration temperature of an incinerator in the incineration procedure is 1000-1300 ℃.
When the pulping process is carried out, the sulfur paste and the concentrated solution are stirred and mixed by a stirrer equipped in a pulping tank, and the pulping temperature is controlled to be 40-80 ℃ by an internal heating coil.
When the waste heat recovery process is carried out, SO prepared in the incineration process is used2The gas passes through the waste heat boiler, the high-temperature air preheater and the low-temperature air preheater in sequence, and passes through SO of the waste heat boiler2The gas temperature is reduced to 450-650 ℃, and the waste heat boiler utilizes high-temperature SO2The heat of the gas generates 3-4 MPaG steam, and the steam passes through SO of the low-temperature air preheater2The gas temperature is reduced to 280-350 ℃.
In the purification step, SO is added2The gas passes through a washing tower, a cooling tower and an electric demister in sequence, the dynamic wave washing tower and the cooling tower are washed by adopting the circulating spraying of the dilute acid, and the circulating dilute acid is cooled by utilizing the cooling water through a heat exchanger. Spraying circulating dilute acid and atomizing SO in dynamic wave washing tower2By intimate contact with atomized dilute acid, by adiabatic evaporation, SO2Humidifying, cooling and primary washing and purifying. Wet SO discharged from outlet of dynamic wave washing tower2After gas-liquid separation, the gas-liquid separated gas enters a cooling tower, is in countercurrent contact with cooling circulating diluted acid sprayed on the top of the tower, is washed and purified to remove impurities and steam in the gas-liquid separated gas, and then enters an electric demister to remove acid mist and dust. SO during washing and cooling2Small amount of SO contained in gas3Reacting with water to generate dilute sulfuric acid with the mass concentration of 1-10%, and feeding the dilute sulfuric acid into the filtrate for neutralization with ammonia contained in the filtrate by blending back, SO during the purification process2The flow velocity of the gas is 5-20 m/s.
When the dry absorption conversion process is carried out, wet SO after washing is firstly carried out2Introducing into a drying tower for drying, and collecting dried SO2Conversion to SO in a conversion column over a catalyst3Absorbing SO with 98% concentrated sulfuric acid sprayed from the top of the absorption tower3，SO3The concentrated sulfuric acid is generated by absorption in an absorption tower and then enters an acid tank.
Taking a 2 ten thousand tons/year coke oven gas desulfurization waste liquid acid making device as an example, adopting the traditional slurry spraying incineration method process, and discharging 2400kg/h (3-5% wtH) of dilute sulfuric acid at the purification section2SO4). After the dilute acid blending technology is introduced into the traditional slurry spraying incineration process, the dilute sulfuric acid discharged from the purification section is treated in the system, no waste liquid is discharged from the whole system, and the yield of concentrated sulfuric acid is increased by 3-5%.
Claims (10)
1. The system for preparing acid from the desulfurization waste liquid is characterized by comprising a pretreatment unit for separating the desulfurization waste liquid from a desulfurization unit into sulfur paste and filtrate, a concentration unit for concentrating the filtrate to obtain concentrated solution, a pulping unit for mixing the sulfur paste and the concentrated solution to prepare slurry, and a slurry incineration SO2Incineration unit of gas and for SO2Purification unit for washing gas and SO purified2A dry absorption conversion unit for preparing concentrated sulfuric acid from gas; and a dilute sulfuric acid outlet in the purification unit is connected with a filtrate storage tank which is used for storing the filtrate in the pretreatment unit.
2. The acid making system according to claim 1, wherein the purification unit comprises a washing tower, a cooling tower and a demister connected in sequence; and the washing tower and the cooling tower are sprayed and washed by circulating dilute acid.
3. The acid making system according to claim 1 or 2, further comprising a waste heat recovery unit located between the incineration unit and the purification unit; the waste heat recovery unit comprises a waste heat boiler and an air preheater which are connected in sequence; the air preheater comprises a high-temperature air preheater and a low-temperature air preheater which are connected.
4. The acid making system according to claim 1, wherein a centrifuge is provided in the pretreatment unit, and an incinerator is provided in the incineration unit; the temperature of the incinerator is 1000-1300 ℃.
5. The acid making system according to claim 1, wherein the dry absorption conversion unit is internally provided with sequentially connected dry SO2Drying tower of (2), SO2Conversion to SO3Of SO, converting the SO3An absorption tower for converting the SO into concentrated sulfuric acid and an acid tank for storing the concentrated sulfuric acid, wherein the conversion tower is filled with the SO2Conversion to SO3The vanadium-based catalyst of (1).
6. A method for producing acid from desulfurization waste liquid, which is performed in the acid production system according to any one of claims 1 to 5, characterized by comprising:
a pretreatment step of separating the desulfurization waste liquid from the desulfurization unit into a sulfur paste and a filtrate;
a concentration step of concentrating the filtrate to obtain a concentrated solution;
a pulping process, wherein the sulfur paste and the concentrated solution are mixed to prepare slurry;
a burning step of burning the slurry into SO2A gas;
a purification step of subjecting the SO2Washing the gas;
dry absorption and conversion process, the purified SO is2Preparing concentrated sulfuric acid from the gas;
the dilute sulfuric acid produced in the purification step is passed to the filtrate for neutralization.
7. The acid making method according to claim 1, wherein the salt content in the concentrated solution is 30-60% of the mass of the concentrated solution;
preferably, the mass ratio of the concentrated solution to the sulfur paste in the pulping process is 1: 1-4: 1;
preferably, the incineration temperature in the incineration process is 1000 to 1300 ℃.
8. The acid production method according to claim 1, wherein SO is added during the purification step2Gas passes through the washing tower, the cooling tower and the demister in sequence, and SO is generated in the washing and cooling processes2SO contained in gas3Reacting with water to generate dilute sulfuric acid;
preferably, the mass concentration of the dilute sulfuric acid is 1-10%;
preferably, in the purification step, SO is added2The flow velocity of the gas is 5-20 m/s.
9. The acid production method according to any one of claims 6 to 8, further comprising a waste heat recovery process performed before the purification process: SO prepared in the burning process2The gas passes through the waste heat boiler and the air preheater in turn, and passes through SO of the waste heat boiler2The temperature of the gas is reduced to 450-650 ℃, and SO passes through an air preheater2The gas temperature is reduced to 280-350 ℃;
preferably, the air preheater comprises a high-temperature air preheater and a low-temperature air preheater which are connected, and SO2The gas passes through the high-temperature air preheater and the low-temperature air preheater in sequence.
10. The method according to claim 6, wherein the dry absorption conversion step is performed by first washing wet SO2Introducing into a drying tower for drying, and collecting dried SO2Catalytic conversion to SO in a conversion column3Said SO3The concentrated sulfuric acid is generated by absorption in an absorption tower and then enters an acid tank.
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114590946A (en) * | 2022-03-24 | 2022-06-07 | 安徽益硫环境科技有限公司 | Drying method of sulfur foam and desulfurization waste liquid |
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