CN103172087A - Method for preparing sulfuric acid or ammonium sulfate from coal gas wet oxidative desulfurization sulfur pulp - Google Patents
Method for preparing sulfuric acid or ammonium sulfate from coal gas wet oxidative desulfurization sulfur pulp Download PDFInfo
- Publication number
- CN103172087A CN103172087A CN2012101452810A CN201210145281A CN103172087A CN 103172087 A CN103172087 A CN 103172087A CN 2012101452810 A CN2012101452810 A CN 2012101452810A CN 201210145281 A CN201210145281 A CN 201210145281A CN 103172087 A CN103172087 A CN 103172087A
- Authority
- CN
- China
- Prior art keywords
- sulphur
- gas
- ammonium
- slurry
- sulfuric acid
- 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
Images
Classifications
-
- 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
Landscapes
- Industrial Gases (AREA)
- Treating Waste Gases (AREA)
Abstract
The invention provides a method for preparing sulfuric acid or ammonium sulfate from coal gas wet oxidative desulfurization sulfur pulp. The method comprises the following steps of: (1) atomizing the coal gas wet oxidative desulfurization sulfur pulp through a nozzle by adopting compressed air, feeding the atomized pulp into a combustion furnace, combusting by using coal gas as an auxiliary fuel and air as an oxidant to obtain furnace gas containing sulfur dioxide; (2) cooling the furnace gas and removing dust; (3) introducing the furnace gas into a converter filled with a vanadium catalyst to obtain converted gas; and (4) feeding the converted gas into an absorption tower, contacting with ammonium sulfate barren solution to obtain ammonium sulfate pregnant solution, returning the ammonium sulfate pregnant solution to an ammonium sulfate system to prepare ammonium sulfate, or feeding the converted gas which is from the converter and contains sulfur trioxide into the absorption tower, and contacting concentrated sulfuric acid to obtain sulfuric acid. The method can be used for completely solving the influence of sulfur pulp and waste solution on the environment, has simple and reliable process flow and excellent economical benefit, can greatly improve the utilization value of impure sulfur, namely increasing the value of each ton of impure sulfur by over 50 percent, and can fulfill the requirements of energy saving and environmental friendliness.
Description
Technical field
The present invention relates to a kind of coal gas wet oxidation and desulfurization sulphur slurry of utilizing and be raw material, prepare sulfuric acid or prepare the method for sulphur ammonium.
Background technology
Traditional coal gas wet oxidation and desulfurization technique, multiplex ammoniacal liquor or diluted alkaline (sodium carbonate) are alkali source, absorb hydrogen sulfide and prussic acid in coal gas in thionizer, are then the sulphur slurry by air with Oxidation of Hydrogen Sulfide in regenerator column, and generate corresponding salt waste liquid.
At present, domestic sulphur slurry has two kinds of processing modes: a kind of is to adopt the molten sulphur of steam heating, and the generation sulphur content is 50～90% sulphur; Another kind is that to generate sulphur content with press filtration or centrifugation mode be 60 ~ 90% sulphur cream; Desulfurization waste liquor is allocated in coking coal.
But be the sulphur after molten sulphur or filter after sulphur cream be all the extremely low waste material of utility value, very easily form secondary pollution in storage and transportation, and desulfurization waste liquor is allocated into and is not only increased the coke oven thermal load in coking coal, returning coal measures commands to corrode and pollute, and obviously increased the sulphur content in the coke, reduced the total quality of coke.Therefore above-mentioned two kinds of processing modes can not satisfy the energy-conserving and environment-protective requirement, can not satisfy the requirement of production high quality coke.
Summary of the invention
The object of the present invention is to provide a kind of method of coal gas wet oxidation and desulfurization sulphur slurry sulfuric acid processed or sulphur ammonium processed, the defects that exists to overcome prior art.
Method of the present invention comprises the steps:
(1) with coal gas wet oxidation and desulfurization sulphur slurry by nozzle and after adopting the pressurized air atomizing, send in roasting kiln, take coal gas as auxiliary fuel, burn take air as oxygenant, obtain to contain the furnace gas of sulfurous gas;
Described coal gas wet oxidation and desulfurization sulphur slurry is a kind of product that derives from coke oven gas desulfurization, is a kind of prior art, as being prepared with reference to the method for the desulfurization such as existing coke-oven plant HPF or FRC;
Described coal gas wet oxidation and desulfurization sulphur slurry comprises following weight percent component:
Sulphur 10～30%
Described compressed-air actuated pressure is 0.4 ~ 0.7 MPa, and the particle diameter of the air atomizing sulphur slurry particle of delivery nozzle is 50～500 μ m, and the roasting kiln furnace temperature is 1000～1300 ℃, and the sulphur slurry with compressed-air actuated volume ratio is: 0.1 ~ 0.2 kg sulphur slurry/mark rice
3Pressurized air;
Above-mentioned " mark rice
3" refer to: the volume under 1 normal atmosphere, 0 ℃ of condition;
In the furnace gas that obtains, the volume content of sulfurous gas is 4～7 %, and the volume content of oxygen is 4～7 %, and the content of oxygen can be regulated by the intake of air;
The furnace gas that (2) will go out roasting kiln is cooled to 350～420 ℃, then sends into dust-removal system, removes the solid particulate in furnace gas, and after high-temperature dust removal, the gas-solid granule content is at 1～25 mg/Nm
3
(3) furnace gas after dedusting being sent into the convertor that is provided with vanadium catalyst, under the katalysis of vanadium catalyst, is sulphur trioxide with Sulphur Dioxide, and acquisition sulphur trioxide volume content is 2～10% reforming gas;
Described vanadium catalyst can adopt the commercial goods for existing matured product;
Invert point is 420～540 ℃; Air speed is 0.2～0.8 m/s;
Described air speed is defined as: the gas flow rate of unit time in void tower;
(4) sulphur ammonium processed or sulfuric acid processed
To go out the reforming gas that convertor contains sulphur trioxide and send into the absorption tower, contact with the sulphur ammonium lean solution of sending here from sulphur ammonium system, the oxynitride of the sulphur trioxide in the absorption reforming gas and a small amount of sulfurous gas and trace, obtain sulphur ammonium rich solution, send sulphur ammonium system back to and prepare the sulphur ammonium, tail gas is from the absorption tower top discharge;
Described sulphur ammonium system and the method for preparing the sulphur ammonium are prior art, can be referring to the method for " the coking chemistry product reclaims and processing ";
Described sulphur ammonium lean solution is the sulphur aqueous ammonium, and solution acidity is 3～6%, and described sulphur ammonium rich solution is all the sulphur aqueous ammonium, and solution acidity is 4～10%, and sulphur ammonium rich solution acidity is greater than sulphur ammonium lean solution acidity; The absorption tower service temperature is: 30～60 ℃, vapour-liquid ratio is 5～20 kg/m
3, described vapour-liquid ratio is defined as: spray liquid weight and absorption gas volume ratio;
Perhaps:
To go out the reforming gas that convertor contains sulphur trioxide and send into the absorption tower, be that 94～98% the vitriol oil contacts with weight concentration, sulphur trioxide in water absorption reforming gas in the vitriol oil and a small amount of sulfurous gas and the oxynitride of trace obtain sulfuric acid, and tail gas is from the absorption tower top discharge; The absorption tower service temperature is for being 30～60 ℃, and vapour-liquid ratio is 5～20kg/m
3
The method for preparing sulfuric acid is prior art, as can be referring to " sulfuric acid industry " 2007(2) method that provides of 13～21 documents.
The present invention also can adopt the more sulphur (sulphur and sulfosalt weight content are more than 40%) of impurity such as sulfosalt that contain of coal gas wet oxidation and desulfurization production to be raw material sulfuric acid processed or sulphur ammonium.Contain sulfosalt in the desulfurization waste liquor of sulfur melting kettle, also can be blended in sulphur slurry as raw material sulfuric acid processed or sulphur ammonium, desulfurization waste liquor and sulphur are starched and are allocated into by the part by weight of 1:1～5:1.
Unusual effect of the present invention is: 1, take coal gas wet oxidation method desulfurization sulfur slurry as raw material sulfuric acid processed or sulphur ammonium, efflux without waste liquid, the Sulphur Dioxide rate has thoroughly solved more than 99.6% the impact that sulphur slurry and waste liquid bring environment; 2, this process using the mode that absorbs of ammonium sulfate liquor, and cancelled traditional cooling, purification and dry link, technical process is simple and reliable; 3, this process using the mode that absorbs of ammonium sulfate liquor, effectively reduce sulphur trioxide, sulfurous gas, nitrogen oxide discharge capacity; 4, the present domestic coal gas desulfurization overwhelming majority adopts wet oxidation process, take coal gas wet-type desulfurization sulfur slurry as raw material, has very strong suitability and promotional value; 5, take coke-oven gas Wet-type oxidation sweetening sulphur slurry as raw material, can cancel the facility such as molten sulphur and sulphur cream in existing coal gas wet oxidation and desulfurization device, improve environment, improve coal gas desulfurization efficient; 6, form of nozzle is adopted in the roasting kiln charging, atomizes with pressurized air, and in desulfurization sulfur slurry and waste liquid, sulphur and sulfosalt can fully burn, and in raw material, the sulphur transformation efficiency is high, and the sulfuric acid yield is high; 7, can be to have the coal gas wet-type desulfurizer impure more sulphur of production and desulfurization waste liquor now as raw material production sulfuric acid or sulphur ammonium, wherein sulphur and sulfosalt content all can be used to sulfuric acid processed more than 40%, solve the outlet of coal gas desulfurization sulphur and waste liquid; 8, the ammonium sulfate liquor with sulphur ammonium system in this factory absorbs sulphur trioxide, and the ammonium sulfate liquor of high acidity returns sulphur ammonium system and produces the sulphur ammonium, forms the refuse H of three systems of desulfurization, relieving haperacidity, sulphur ammonium
2S, HCN, NH
3Finally be converted into the ammonium salts such as sulphur ammonium.
The economic benefit that the present invention produces is: 1, take coal gas wet oxidation and desulfurization sulphur slurry as raw material, 1 ton of sulphur slurry can be produced 1.4 tons of sulphur ammoniums, and 2 tons of about 2.5～3MPa steam have good economic benefit; 2, efflux without waste liquid due to desulfurization sulfur slurry sulfuric acid processed or sulphur ammonium, environmental benefit is very remarkable; 3, can be to have coal gas desulfurization sulphur and waste liquid now as raw material sulfuric acid processed or sulphur ammonium, wherein sulphur and sulfosalt content all can be used to sulfuric acid processed or sulphur ammonium more than 40%, greatly improved the utility value of impure sulphur, impure sulphur per ton is worth and can increases more than 50%, meets the energy-saving and environmental protection requirement.
Description of drawings
Fig. 1 is schema of the present invention.
Fig. 2 is the nozzle arrangements schematic diagram.
Fig. 3 is the converter structure schematic diagram.
Concrete embodiment
Referring to Fig. 1, method of the present invention comprises the steps:
(1) with coal gas wet oxidation and desulfurization sulphur slurry by nozzle 101, and after adopting the pressurized air atomizing, send in roasting kiln 1, take coal gas as fuel, burn take air as oxygenant, obtain to contain the furnace gas of sulfurous gas;
The furnace gas that (2) will go out roasting kiln 1 is cooled to 350～420 ℃, then sends into dust-removal system 3 dedustings, as remove the solid particulate in furnace gas through the high-temperature dry-type dust-removal system;
Described high-temperature dry-type dust-removal system is a kind of prior art, as the system of " environment protection " 2008 VOL404 reported in literature;
Preferably, reclaim heat by waste heat boiler 2, be cooled to 350～420 ℃, and produce 0.8～4.0MPa steam;
(3) furnace gas after dedusting being sent into the convertor 4 that is provided with vanadium catalyst, under the vanadium catalyst katalysis, is sulphur trioxide with Sulphur Dioxide;
Preferably, the furnace gas after dedusting is sent into the convertor 4 that is provided with vanadium catalyst by gas blower;
(4) will go out the reforming gas that convertor 4 contains sulphur trioxide and send into absorption tower 5, contact with the sulphur ammonium lean solution of sending here from sulphur ammonium system, the oxynitride of the sulphur trioxide in the absorption reforming gas and a small amount of sulfurous gas and trace, obtain sulphur ammonium rich solution, send sulphur ammonium system back to, for the preparation of the sulphur ammonium, tail gas is from the absorption tower top discharge;
Perhaps:
To go out the reforming gas that convertor 4 contains sulphur trioxide and send into absorption tower 5, and contact with the vitriol oil, the water in the vitriol oil absorbs sulphur trioxide and a small amount of sulfurous gas and the oxynitride of trace in reforming gas, obtains sulfuric acid, and tail gas is from the absorption tower top discharge;
Referring to Fig. 2, described nozzle 101 comprises coaxial pipe core 20 and outer tube 30, one end of pipe core 20 is sulphur slurry entrance 201, the other end is air atomizing sulphur slurry outlet 202, one end of outer tube 30 is compressed air inlet 301, and the sulphur slurry enters described nozzle 101 by the sulphur slurry entrance 201 of pipe core 20, and pressurized air enters described nozzle 101 by compressed air inlet 301, air atomizing sulphur slurry outlet 202 through described nozzle 101 enters roasting kiln 1 after atomizing;
Pipe core 20: outer tube 30=1: 4～20;
As Fig. 3, said convertor 4 comprises a section 41 of overlapping successively conversion, transforms two section 42 and transform three section 43;
SO in tail gas
2Content≤300 ppm, tail gas rear discharging up to standard.
Transforming one section inlet temperature is 420～460 ℃, and transforming the one section outlet temperature is 540～580 ℃;
Transforming two sections inlet temperatures is 420～450 ℃, and transforming the second stage exit temperature is 460～500 ℃;
Transforming three sections inlet temperatures is 420～440 ℃, and transforming three sections temperature outs is 420～440 ℃.
Embodiment 1
Adopt flow process, the nozzle of Fig. 2 and the convertor of Fig. 3 of Fig. 1, preparation sulphur ammonium.
The basic technology condition is as follows:
Coal gas wet oxidation and desulfurization sulphur slurry is comprised of the component of following weight percent: sulphur 10%, sulfosalt 20%, water 70%;
Compressed-air actuated pressure is 0.4 MPa, and the particle diameter of the particle of the atomized sulfur slurry of delivery nozzle is 50 μ m, and the roasting kiln furnace temperature is 1000 ℃, and the sulphur slurry with compressed-air actuated volume ratio is: 0.1 kg sulphur slurry/mark rice
3Pressurized air;
Pipe core 20: outer tube 30=1: 4;
In the furnace gas that obtains, the volume content of sulfurous gas is 4%, and the volume content of oxygen is 4%;
Go out the furnace gas of roasting kiln, reclaim heat by waste heat boiler 2, be cooled to 350 ℃, and produce 2.5MPa steam; After high-temperature dust removal, the gas-solid granule content is at 1 mg/Nm
3
Being provided with the vanadium catalyst convertor comprises a section 41 of conversion, transforms two section 42 and transform three section 43;
Transform 460 ℃ of one section inlet temperatures, transform 580 ℃ of one section outlet temperature;
Transform 450 ℃ of two sections inlet temperatures, temperature out is 500 ℃;
Transform 440 ℃ of three sections inlet temperatures, transform 440 ℃ of three sections temperature outs.
Air speed is 0.8 m/s;
The catalyzer that vanadium catalyst adopts Xiangfan Jingxin Catalyst Co., Ltd. to produce.
In sulphur ammonium lean solution, solution acidity is about 4%, and in sulphur ammonium rich solution, solution acidity is about 5%, and the absorption tower service temperature is 60 ℃, and vapour-liquid ratio is 5 kg/m
3
The sulphur ammonium rich solution that obtains, preparation sulphur ammonium in sulphur ammonium system.
SO in tail gas
2Content≤300 ppm, treated rear discharging up to standard.
Adopt above-mentioned method, 1 ton of sulphur slurry can be produced 1 ton of sulphur ammonium, approximately 2 tons of 2.5MPa steam.
Adopt flow process, the nozzle of Fig. 2 and the convertor of Fig. 3 of Fig. 1, preparation sulphur ammonium.
The basic technology condition is as follows:
The component of coal gas wet oxidation and desulfurization sulphur slurry is: sulphur 30%, sulfosalt 40%, water 30%
Compressed-air actuated pressure is 0.7 MPa, and the particle diameter of the particle of the atomized sulfur slurry of delivery nozzle is 500 μ m, and the roasting kiln furnace temperature is 1300 ℃, and the sulphur slurry with compressed-air actuated volume ratio is: 0.2 kg sulphur slurry/mark rice
3Pressurized air;
Pipe core: outer tube 30=1: 20;
In the furnace gas that obtains, the volume content of sulfurous gas is 7%, and the volume content of oxygen is 7%;
Go out the furnace gas of roasting kiln, reclaim heat by waste heat boiler 2, be cooled to 420 ℃, and produce 2.5MPa steam;
After high-temperature dust removal, the gas-solid granule content is at 25 mg/Nm
3
Being provided with the vanadium catalyst convertor comprises a section 41 of conversion, transforms two section 42 and transform three section 43;
Transform 420 ℃ of one section inlet temperatures, transform 540 ℃ of one section outlet temperature;
Transform 420 ℃ of two sections inlet temperatures, temperature out is 460 ℃;
Transform 420 ℃ of three sections inlet temperatures, transform 430 ℃ of three sections temperature outs.
Air speed is 0.2 m/s;
The catalyzer that vanadium catalyst adopts Xiangfan Jingxin Catalyst Co., Ltd. to produce.
In sulphur ammonium lean solution, solution acidity is about 5%, and in sulphur ammonium rich solution, solution acidity is about 10%, and the absorption tower service temperature is 30 ℃, and vapour-liquid ratio is 20 kg/m
3
The sulphur ammonium rich solution that obtains, preparation sulphur ammonium in sulphur ammonium system;
SO in tail gas
2Content≤300 ppm, treated rear discharging up to standard.
Adopt above-mentioned method, 1 ton of sulphur slurry can be produced 1.8 tons of sulphur ammoniums, 2 tons of about 2.5MPa steam.
Adopt flow process, the nozzle of Fig. 2 and the convertor of Fig. 3 of Fig. 1, preparation sulfuric acid.
To go out the reforming gas that convertor contains sulphur trioxide and send into the absorption tower, be that 95% the vitriol oil contacts with weight concentration, sulphur trioxide in water absorption reforming gas in the vitriol oil and a small amount of sulfurous gas and the oxynitride of trace, the acquisition weight concentration is 98% sulfuric acid, and other is identical with embodiment 1.
The absorption tower service temperature is 50 ℃, and vapour-liquid ratio is 5 kg/m
3
Adopt above-mentioned method, it is 98% sulfuric acid that 1 ton of sulphur slurry can be produced 1 ton of weight concentration, 2 tons of about 3MPa steam.
Claims (10)
1. the method for coal gas wet oxidation and desulfurization sulphur slurry sulfuric acid processed or sulphur ammonium processed, is characterized in that, comprises the steps:
(1) with coal gas wet oxidation and desulfurization sulphur slurry by nozzle and after adopting the pressurized air atomizing, send in roasting kiln, take coal gas as auxiliary fuel, burn take air as oxygenant, obtain to contain the furnace gas of sulfurous gas;
(2) will go out that the furnace gas of roasting kiln is cooling, dedusting;
(3) furnace gas after dedusting being sent into the convertor that is provided with vanadium catalyst, under the katalysis of vanadium catalyst, is sulphur trioxide with Sulphur Dioxide, obtains reforming gas;
(4) will go out the reforming gas that convertor contains sulphur trioxide and send into the absorption tower, and contact with the sulphur ammonium lean solution of sending here from sulphur ammonium system, and obtain sulphur ammonium rich solution, and send sulphur ammonium system back to and prepare the sulphur ammonium, tail gas is from the absorption tower top discharge;
Perhaps: will go out the reforming gas that convertor contains sulphur trioxide and send into the absorption tower, and contact with the vitriol oil, and obtain sulfuric acid, tail gas is from the absorption tower top discharge.
2. method according to claim 1, it is characterized in that, described compressed-air actuated pressure is 0.4 ~ 0.7 MPa, the particle diameter of the air atomizing sulphur slurry particle of delivery nozzle is 50～500 μ m, the roasting kiln furnace temperature is 1000～1300 ℃, and the sulphur slurry with compressed-air actuated volume ratio is: 0.1 ~ 0.2 kg sulphur slurry/mark rice
3Pressurized air.
3. method according to claim 1, is characterized in that, the furnace gas that will go out roasting kiln is cooled to 350～420 ℃, then dedusting, and after dedusting, the gas-solid granule content is at 1～25 mg/Nm
3
4. method according to claim 3, is characterized in that, reclaims heat by waste heat boiler (2), is cooled to 350～420 ℃, and produces 0.8～4.0MPa steam.
5. method according to claim 1, is characterized in that, in step (3), invert point is 420～540 ℃; Air speed is 0.2～0.8 m/s.
6. method according to claim 1, is characterized in that, said convertor (4) comprises overlapping successively conversion one section (41), conversion two sections (42) and transforms three sections (43);
Transforming one section inlet temperature is 420～460 ℃, and transforming the one section outlet temperature is 540～580 ℃; Transforming two sections inlet temperatures is 420～450 ℃, and transforming the second stage exit temperature is 460～500 ℃; Transforming three sections inlet temperatures is 420～440 ℃, and transforming three sections temperature outs is 420～440 ℃.
7. method according to claim 1, is characterized in that, described sulphur ammonium lean solution is the sulphur aqueous ammonium, and solution acidity is 3～6%, and described sulphur ammonium rich solution is all the sulphur aqueous ammonium, and solution acidity is 4～10%, and sulphur ammonium rich solution acidity is greater than sulphur ammonium lean solution acidity; The absorption tower service temperature is: 30～60 ℃, vapour-liquid ratio is 5～20 kg/m
3
8. according to claim 1～7 described methods of any one, is characterized in that, described coal gas wet oxidation and desulfurization sulphur slurry comprises following weight percent component: sulphur 10～30%, sulfosalt 20～40%, water 30 ~ 70%.
9. method according to claim 8, it is characterized in that, described nozzle (101) comprises coaxial pipe core (20) and outer tube (30), one end of pipe core (20) is sulphur slurry entrance (201), the other end is air atomizing sulphur slurry outlet (202), and an end of outer tube (30) is compressed air inlet (301).
10. method according to claim 8, is characterized in that, nozzle (101) exit, and pipe core (20) with the ratio of the cross-sectional area of outer tube (30) is: pipe core 20: outer tube 30=1: 4～20.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2012101452810A CN103172087A (en) | 2011-12-26 | 2012-05-11 | Method for preparing sulfuric acid or ammonium sulfate from coal gas wet oxidative desulfurization sulfur pulp |
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201110440764.9 | 2011-12-26 | ||
| CN201110440764 | 2011-12-26 | ||
| CN2012101452810A CN103172087A (en) | 2011-12-26 | 2012-05-11 | Method for preparing sulfuric acid or ammonium sulfate from coal gas wet oxidative desulfurization sulfur pulp |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN103172087A true CN103172087A (en) | 2013-06-26 |
Family
ID=48632370
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2012101452810A Pending CN103172087A (en) | 2011-12-26 | 2012-05-11 | Method for preparing sulfuric acid or ammonium sulfate from coal gas wet oxidative desulfurization sulfur pulp |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN103172087A (en) |
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106430116A (en) * | 2016-08-24 | 2017-02-22 | 金能科技股份有限公司 | Method for preparing sulfuric acid by utilizing sulfur-containing waste liquid generated during gas wet type oxidation process |
| CN107055572A (en) * | 2017-05-17 | 2017-08-18 | 北京华元昊峰科技有限公司 | The cleaning procedure and system of a kind of acetylene spent acid disposal |
| CN107934989A (en) * | 2017-12-15 | 2018-04-20 | 中冶焦耐(大连)工程技术有限公司 | Utilize the system of desulfurization regeneration tail gas drying sulphur ammonium |
| CN108046292A (en) * | 2017-12-15 | 2018-05-18 | 中冶焦耐(大连)工程技术有限公司 | Utilize the technique of desulfurization regeneration tail gas drying sulphur ammonium |
| CN109852434A (en) * | 2019-02-20 | 2019-06-07 | 宁波科新化工工程技术有限公司 | A kind of method of coke-oven-gas desulfurization and decyanation concentration relieving haperacidity |
| CN111017884A (en) * | 2019-12-21 | 2020-04-17 | 山东绿知源环保工程有限公司 | Method for preparing industrial sulfuric acid from desulfurization waste liquid by slurry spraying method |
| WO2022172864A1 (en) * | 2021-02-10 | 2022-08-18 | 日本管機工業株式会社 | Apparatus for producing dilute sulfuric acid and method for producing dilute sulfuric acid |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101092577A (en) * | 2007-04-16 | 2007-12-26 | 中冶焦耐工程技术有限公司 | Technique and equipment for preparing sulfuric acid by using sulfur and waste liquid generated from coal gas wet type oxidation sweetening technique |
| CN101519193A (en) * | 2008-02-25 | 2009-09-02 | 宁波科新煤化工设备有限公司 | Acid preparing method by coal gas wet oxidation and desulfurization |
-
2012
- 2012-05-11 CN CN2012101452810A patent/CN103172087A/en active Pending
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101092577A (en) * | 2007-04-16 | 2007-12-26 | 中冶焦耐工程技术有限公司 | Technique and equipment for preparing sulfuric acid by using sulfur and waste liquid generated from coal gas wet type oxidation sweetening technique |
| CN101519193A (en) * | 2008-02-25 | 2009-09-02 | 宁波科新煤化工设备有限公司 | Acid preparing method by coal gas wet oxidation and desulfurization |
Cited By (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106430116A (en) * | 2016-08-24 | 2017-02-22 | 金能科技股份有限公司 | Method for preparing sulfuric acid by utilizing sulfur-containing waste liquid generated during gas wet type oxidation process |
| CN106430116B (en) * | 2016-08-24 | 2019-01-04 | 金能科技股份有限公司 | A method of the sulphur-bearing waste solution extracting sulfuric acid generated using coal gas wet oxidation method |
| CN107055572A (en) * | 2017-05-17 | 2017-08-18 | 北京华元昊峰科技有限公司 | The cleaning procedure and system of a kind of acetylene spent acid disposal |
| CN107934989A (en) * | 2017-12-15 | 2018-04-20 | 中冶焦耐(大连)工程技术有限公司 | Utilize the system of desulfurization regeneration tail gas drying sulphur ammonium |
| CN108046292A (en) * | 2017-12-15 | 2018-05-18 | 中冶焦耐(大连)工程技术有限公司 | Utilize the technique of desulfurization regeneration tail gas drying sulphur ammonium |
| CN108046292B (en) * | 2017-12-15 | 2023-04-11 | 中冶焦耐(大连)工程技术有限公司 | Process for drying ammonium sulfate by using desulfurization regeneration tail gas |
| CN107934989B (en) * | 2017-12-15 | 2023-08-01 | 中冶焦耐(大连)工程技术有限公司 | System for drying ammonium sulfate by utilizing desulfurization regeneration tail gas |
| CN109852434A (en) * | 2019-02-20 | 2019-06-07 | 宁波科新化工工程技术有限公司 | A kind of method of coke-oven-gas desulfurization and decyanation concentration relieving haperacidity |
| CN111017884A (en) * | 2019-12-21 | 2020-04-17 | 山东绿知源环保工程有限公司 | Method for preparing industrial sulfuric acid from desulfurization waste liquid by slurry spraying method |
| WO2022172864A1 (en) * | 2021-02-10 | 2022-08-18 | 日本管機工業株式会社 | Apparatus for producing dilute sulfuric acid and method for producing dilute sulfuric acid |
| WO2022172354A1 (en) * | 2021-02-10 | 2022-08-18 | 日本管機工業株式会社 | Dilute sulfuric acid production device and dilute sulfuric acid production method |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101519193B (en) | Acid preparing method by coal gas wet oxidation and desulfurization | |
| CN103172087A (en) | Method for preparing sulfuric acid or ammonium sulfate from coal gas wet oxidative desulfurization sulfur pulp | |
| CN102303883B (en) | Method for preparing calcium oxide and sulfur by double-atmosphere fluidized roasting of desulfurated gypsum | |
| CN101643809B (en) | Sponge iron production technology by coal gasification | |
| CN102367169B (en) | Method for preparation of sulfuric acid and combined production of fine flour iron through calcination of coal-derived pyrite in presence of oxygen-rich air | |
| WO2020135135A1 (en) | Process and device for processing low-purity sulfur and auxiliary salt waste liquid produced by desulfurization of coke oven gas | |
| CN102698585B (en) | Method for recyling carbon dioxide in boiler flue gas | |
| CN102997697A (en) | Sinter waste-heat utilization process based on purification of sintering flue gas | |
| CN104803819B (en) | A kind of method and system utilizing fine coal preparing ethylene | |
| CN103072957A (en) | Technology for preparing sulfuric acid | |
| CN108176194A (en) | A kind of processing unit and processing method containing sulphur simple substance and compound tail gas | |
| CN111847381B (en) | Method and device for preparing hydrogen from industrial waste gas | |
| CN108128757B (en) | A kind of technique of flue gas during smelting sulphur | |
| CN105129800A (en) | Process and system of preparing calcium carbide and ethylene through oxygen/coal injection | |
| CN207468199U (en) | For the device of sulphur recovery and alkylation spent acid Combined Treatment clean manufacturing | |
| CN108862207A (en) | A kind of sour gas wet process acid-making process combined with semidry method tail gas desulfurization | |
| CN101774550A (en) | Novel production method of sulfuric acid | |
| CN108298507B (en) | Method and device for treating sulfur-containing flue gas generated by calcining petroleum coke by using pyrite acid making device | |
| CN108217606B (en) | Utilize the cross-flow moving bed device of carbon-based material reduction and desulfurization resolution gas Recovered sulphur | |
| CN103043625A (en) | Method for preparing sulfuric acid by blending combustion of sulfur waste and ferrous sulfate waste | |
| CN206924611U (en) | A kind of sulfur-containing tail gas processing system | |
| CN102277205B (en) | Method for extracting salt from coke oven gas by desulfuration and decyanation | |
| CN212222701U (en) | Device for recovering desulfurization and denitrification waste liquid by extraction method | |
| CN102976285B (en) | Method for preparing sulfuric acid from desulfurized gypsum in secondary lead smelting process as raw material | |
| CN107311117A (en) | Sulphur recovery and alkylation spent acid Combined Treatment process for cleanly preparing and device |
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: 20130626 |