CN108862207A - A kind of sour gas wet process acid-making process combined with semidry method tail gas desulfurization - Google Patents
A kind of sour gas wet process acid-making process combined with semidry method tail gas desulfurization Download PDFInfo
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- CN108862207A CN108862207A CN201810813786.7A CN201810813786A CN108862207A CN 108862207 A CN108862207 A CN 108862207A CN 201810813786 A CN201810813786 A CN 201810813786A CN 108862207 A CN108862207 A CN 108862207A
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- 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
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D46/00—Filters or filtering processes specially modified for separating dispersed particles from gases or vapours
- B01D46/02—Particle separators, e.g. dust precipitators, having hollow filters made of flexible material
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- 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
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/48—Sulfur compounds
- B01D53/50—Sulfur oxides
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- 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
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/81—Solid phase processes
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/40—Alkaline earth metal or magnesium compounds
- B01D2251/404—Alkaline earth metal or magnesium compounds of calcium
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/60—Inorganic bases or salts
- B01D2251/604—Hydroxides
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- 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
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- 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
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Abstract
The present invention relates to a kind of sour gas wet process acid-making process combined with semidry method tail gas desulfurization, sour gas and fuel gas enter sour gas burning furnace, process gas after burning enters SO 2 converter after the heat exchange of sour gas waste heat boiler, the process gas that SO 2 converter comes out enters condensation of sulfuric acid device, the sulfuric acid and the cold acid-mixed of circulation of condensation of sulfuric acid device bottom outflow enter sulfuric acid mixing channel after closing, it is cooling as product sulfuric acid submitting battery limit (BL) through sulfuric acid water cooler again, after tail is mixed with the part hot-air that condensation of sulfuric acid device comes out out at the top of condensation of sulfuric acid device, it forms relieving haperacidity tail gas and enters the venturi section of circulating fluidized bed desulfurization tower lower part, it is come into full contact with the calcium hydroxide in tower, tail gas containing calcium hydroxide powder enters in sack cleaner, cleaning of off-gas smoke evacuation chimney after desulfurization air-introduced machine.The present invention for the first time combines semi-dry desulphurization with wet process acid-making process, the SO in removing tail gas2While realize SO3（Sulfuric acid mist）97%-100% removal efficiency realizes the qualified discharge of tail gas.
Description
Technical field
The present invention relates to sour gas acid-making process technical field, and in particular to a kind of to combine with semidry method tail gas desulfurization
Sour gas wet process acid-making process.
Background technique
Sour gas wet process relieving haperacidity is one extensive kind and produces applied to coal chemical industry, coking, oil-refining chemical, viscose rayon, is coloured
The industries such as metal smelt processing sour gas and the process system for recycling high-concentration sulfuric acid, relative to dry method relieving haperacidity, with work
Skill process is simple, and occupied area is small, and heat utilization ratio is high, can by-product high-quality steam the advantages that.But it is catalyzed by sulfur dioxide
The limitation of reforming catalyst performance, the conversion ratio to sulfur dioxide are up to 99.0-99.3%, therefore just contain in relieving haperacidity tail gas
A certain amount of SO2, a certain amount of SO is in addition also contained in tail gas3.In order to control SO in sulphuric acid plant tail gas3（Sulfuric acid mist）Contain
Amount is equipped with control of acid fog unit before condensation of sulfuric acid device, generates crystalline silica nuclei using silicone oil burning and acid mist is gathered into acid
Drop, this nucleus are conducive to acid and drip the precipitation in condenser and grow up and be unlikely to form excessive too small droplet, but in practical behaviour
Fluctuation and other factors during work by device load are influenced, and control of acid fog unit is ineffective to control of acid fog, easily
It causes acid mist in tail gas exceeded, the phenomenon that chimney " smoldering " occurs.
The requirement of Air Pollutant Emission was increasingly stringenter in recent years, GB31570-2015《Petroleum refining industry pollution
Object discharge standard》Regulation executes special limit value area Acidic Gas Treating device SO2Emission limit be 100mg/Nm3, sulfuric acid mist
Emission limit is 5mg/Nm3, GB26132-2010《Sulfuric acid industry pollutant emission standard》Middle regulation executes special limit value area
The emission limit of tail gas sulfuric acid mist is 5mg/Nm in Acidic Gas Treating device3, some provincial standards require SO in emissions2's
Content is less than 35mg/Nm3, sulfuric acid mist content be less than 5mg/Nm3.The formulation of the above standard, is required to sulphuric acid plant
Tail gas carries out further desulfurization process.
Currently, wet desulphurization is the processing common method of sulphuric acid plant tail gas, but limited by wet desulfurizing process feature,
Into the SO of wet desulfurization system3It is readily formed the SO that diameter is 0.1 μm3Aerosol will remove these SO3Needed for aerosol
Pressure drop than the wet desulfurization system of normal design operation pressure drop it is much higher, general wet desulfurization system is to SO3Removing
Rate < 30%, causes tail gas at the case where just will appear chimney " smoldering " when the concentration of sulfuric acid aerosol in tail gas is more than 5-8ppm
Middle SO3（Acid mist）Content is exceeded, and corrosion can be also generated to equipment, and blocking, the harm such as fouling influences the normal of desulphurization system
Stable operation.
Summary of the invention
The purpose of the present invention is in order to solve the above technical problems, providing a kind of acidity combined with semidry method tail gas desulfurization
Air humidity method acid-making process for the first time combines semi-dry desulphurization with wet process acid-making process, the SO in removing tail gas2While it is real
Existing SO3（Sulfuric acid mist）97%-100% removal efficiency realizes the qualified discharge of tail gas.
The present invention is in order to solve the above technical problems, provided technical solution is：One kind is mutually tied with semidry method tail gas desulfurization
The sour gas wet process acid-making process of conjunction contains H2The sour gas and fuel gas of S, the excessive hot-air of secondary air fan enter sour gas combustion
It burns in furnace, process gas of the ignition temperature control after 900-1300 DEG C, burning cools to after the heat exchange of sour gas waste heat boiler
390-420 DEG C and enter SO 2 converter, to enter sulfuric acid cold for the 270-290 DEG C of process gas come out through SO 2 converter
In condenser, the sulfuric acid and the cold acid-mixed of circulation of condensation of sulfuric acid device bottom outflow enter sulfuric acid mixing channel after closing, then through sulfuric acid water cooler
40 DEG C are cooled to as product sulfuric acid and sends out battery limit (BL), the 80-100 DEG C of tail gas and condensation of sulfuric acid device come out at the top of condensation of sulfuric acid device
After the part hot-air mixing that temperature out is 210 DEG C -230 DEG C, formation temperature is that 150 DEG C -160 DEG C of relieving haperacidity tail gas is gone forward side by side
The venturi section for entering circulating fluidized bed desulfurization tower lower part, comes into full contact with the calcium hydroxide in tower, is sprayed by atomizing lance into tower
Water, the SO in tail gas2、SO3It reacts with calcium hydroxide, the tail gas containing calcium hydroxide powder enters in sack cleaner, by pocket type
A part of absorbent that deduster is collected returns to circulating fluidized bed desulfurization tower through returning charge skewed slot under the action of returning charge skewed slot blower
In recycle, another part is delivered to desulfurization ash cellar, cleaning of off-gas smoke evacuation chimney after desulfurization air-introduced machine.
As a kind of advanced optimizing for sour gas wet process acid-making process combined with semidry method tail gas desulfurization of the invention：
The water return amount that atomizing lance is controlled according to circulating fluidized bed desulfurization tower outlet temperature, to control to circulating fluidized bed desulfurization tower
Amount of water sprayed, so that circulating fluidized bed desulfurization tower exports fibre selection at 80-90 DEG C.
As a kind of advanced optimizing for sour gas wet process acid-making process combined with semidry method tail gas desulfurization of the invention：
According to SO in chimney breast cleaning of off-gas2And SO3Concentration adjust circulating fluidized bed desulfurization tower in calcium hydroxide amount, make in tail gas
SO2Content be less than 100mg/Nm3, SO3Content be less than 5mg/Nm3。
As a kind of advanced optimizing for sour gas wet process acid-making process combined with semidry method tail gas desulfurization of the invention：
Cycle flue is additionally provided between the circulating fluidized bed desulfurization tower inlet tube and chimney inlet tube.
As a kind of advanced optimizing for sour gas wet process acid-making process combined with semidry method tail gas desulfurization of the invention：
Controllable register is provided at the air outlet of the desulfurization air-introduced machine.
As a kind of advanced optimizing for sour gas wet process acid-making process combined with semidry method tail gas desulfurization of the invention：
The smoke inlet pipeline of the circulating fluidized bed desulfurization tower and the material of venturi section are stainless steel.
As a kind of advanced optimizing for sour gas wet process acid-making process combined with semidry method tail gas desulfurization of the invention：
Cloth bag in the bag filter is PTFE cloth bag.
As a kind of advanced optimizing for sour gas wet process acid-making process combined with semidry method tail gas desulfurization of the invention：
The part hot-air of the condensation of sulfuric acid device is recycled to sour gas burning furnace as combustion air.
As a kind of advanced optimizing for sour gas wet process acid-making process combined with semidry method tail gas desulfurization of the invention：
The circulating fluidized bed desulfurization tower is using the calcium hydroxide of 300-400 mesh as absorbent.
Beneficial effect
（1）The present invention for the first time combines sour gas wet process acid-making process with semi-dry desulfurizing process, it is ensured that smoke stack emission
SO in tail gas3（Sulfuric acid mist）Content is not higher than 5mg/Nm3, SO2Content is not higher than 100mg/Nm3, realize the qualified discharge of tail gas,
There are preferable economy and environmental benefit；
（2）Condensation of sulfuric acid device of the invention uses air for cooling medium, and air a part after exchanging heat enters combustion furnace work
For the tail gas mix and convert that combustion air, extra part can come out with condensation of sulfuric acid device, the temperature of semi-dry desulphurization is entered with raising,
Equipment investment is reduced, heat utilization ratio is improved；
（3）The exhaust temperature of wet process acid-making process discharge of the invention is 150 DEG C -160 DEG C, is able to satisfy semi-dry desulphurization requirement
Inlet temperature, and cleaning exhaust gas recirculation circuit is also set up, when device load is lower than the 60% of Design cooling load, open circulation
Pipeline returns to Partial cleansing tail gas on circulating fluidized bed desulfurization tower inlet pipeline, it is ensured that the stable operation of desulphurization system.
（4）It is the hydrated lime particle of 300-400 mesh or so as absorbent, at low cost, money that partial size is used in the present invention
Source is abundant, the operating cost of desulphurization system is reduced, and the absorbent has huge adsorption surface area, to SO3Aerosol has
Strong adsorption capacity removes SO in tail gas in circulating fluidized bed desulfurization tower2While realize to SO3（Sulfuric acid mist）97%-
100% removal efficiency, significantly larger than wet desulfurization system is to SO330% removal efficiency of highest, fundamentally ensure that reaching for acid mist
Mark discharge.
（5）The reaction temperature that technique of the invention can control desulphurization system is higher than 30 DEG C of tail gas dew point or more, both ensure that
Optimum temperature needed for reaction, also avoids the generation of dew point corrosion, at 80 DEG C -90 DEG C, whole system does not need exhaust gas temperature
Anti-corrosion, operation and maintenance are simple, high reliablity.
（6）The present invention solves that traditional wet desulphurization device easily blocks, is perishable, easy fouling, chimney emit white cigarette and drag
The problem of tail, water consume it is low and without waste water generate, identified through national standard, desulfurizing byproduct main component be calcium sulfate, calcium sulfite and
Unreacted Ca (OH)2Deng, it is runny dry state, belongs to Ordinary solid waste, processing mode diversification, comprehensive utilization ratio
It is high.
Detailed description of the invention
Fig. 1 is the flow diagram of present invention process；
It is marked in figure：1, primary air blower, 2, sour gas burning furnace, 3, sour gas burning furnace waste heat boiler, 4, sulfur dioxide
Converter, 5, steam expansion tank, 6, drum, 7, auxiliary air blower, 8, condensation of sulfuric acid device, 9, sulfuric acid mixing channel, 10, sulfuric acid water
Cooler, 11, sulfuric acid circulating pump, 12, calcium hydroxide feed bin, 13, circulating fluidized bed desulfurization tower, 14, sack cleaner, 15, returning charge it is oblique
Slot blower, 16, desulfurization ash cellar, 17, desulfurization air-introduced machine, 18, chimney.
Specific embodiment
Below with reference to embodiment, the invention will be further described, and but the scope of the present invention is not limited thereto, this field
Technical staff made to any conspicuous improvement of above embodiment or change, all without departing from design of the invention
And scope of protection of the claims.
As shown in the figure：A kind of sour gas wet process acid-making process combined with semidry method tail gas desulfurization, specifically includes following
Step：
（1）Sour gas wet process relieving haperacidity：
Containing H2The sour gas and the external fuel gas in battery limit (BL) of S, the excessive hot-air of secondary air fan 7 enter sour gas burning furnace 2
Interior, ignition temperature is controlled at 900-1300 DEG C, guarantees the H in sour gas2The sulfur-containing compounds such as S are fully converted to SO2, Zhi Hougong
Skill gas cools to 390-420 DEG C by sour gas waste heat boiler 3 and enters SO 2 converter 4,99.0-99.3% in process gas
SO2It is converted into SO3, the interlayer heat exchanger inside the inverted device of reaction heat is removed and presses through hot steam in generating, through sulfur dioxide
270 DEG C -290 DEG C of the process gas that converter 4 comes out enters in condensation of sulfuric acid device 8, and cooling medium is sent by primary air fan 1
Cooling air.SO in process gas3It is hydrated into sulfuric acid to flow out from 8 bottom of condensation of sulfuric acid device, enters sulphur with recycling after cold acid-mixed is closed
Sour mixing channel 9, then be cooled to 40 DEG C of left-right parts as product sulfuric acid through sulfuric acid water cooler 10 and send out battery limit (BL), steam expansion tank 5
It is technique commonly used equipment with drum 6, this will not be detailed here.
The exhaust temperature come out at the top of condensation of sulfuric acid device 8 is 80-100 DEG C, and the temperature come out with condensation of sulfuric acid device 8 is
After 210 DEG C -230 DEG C of part hot-air mixing（Another part hot-air is recycled to sour gas burning by auxiliary air blower 7
Furnace 2）, temperature is that 150 DEG C -160 DEG C of relieving haperacidity tail gas enters in semidry process desulfurizer, SO in tail gas2Content is in 500-
1000mg/Nm3Between, sulfuric acid mist content is less than 100mg/Nm3。
（2）Semi-dry desulphurization：
Temperature is 150 DEG C -160 DEG C containing SO2, SO3（Sulfuric acid mist）Sulphuric acid plant tail gas under circulating fluidized bed desulfurization tower 13
The venturi section in portion enters, with the calcium hydroxide in tower（It is supplied by calcium hydroxide feed bin 12）It comes into full contact with, by atomizing lance to tower
Interior water spray plays the role of humidification activation to calcium hydroxide, the SO in tail gas2、SO3（Sulfuric acid mist）It reacts with calcium hydroxide, containing disappearing
The tail gas of lime powder enters in subsequent sack cleaner 14, and the material a part collected by sack cleaner 14 absorbs
Agent is returned in circulating fluidized bed desulfurization tower 13 through returning charge skewed slot under the action of returning charge skewed slot blower 15 and is recycled, another part
It is delivered to desulfurization ash cellar 16, cleaning of off-gas smoke evacuation chimney 18 after desulfurization air-introduced machine 17.It is exported according to circulating fluidized bed desulfurization tower 13
Temperature controls the water return amount of atomizing lance, so that the amount of water sprayed to circulating fluidized bed desulfurization tower 13 is controlled, so that recirculating fluidized bed
Desulfurizing tower 13 exports fibre selection at 80-90 DEG C.SO in cleaning of off-gas is exported according to chimney 182、SO3（Sulfuric acid mist）Concentration come
Adjust the amount of calcium hydroxide in circulating fluidized bed desulfurization tower 13.SO in the tail gas of semi-dry desulphurization system out2Content be less than
100mg/Nm3, the content of sulfuric acid mist is less than 5mg/Nm3, realize qualified discharge.
The reaction occurred inside circulating fluidized bed desulfurization tower is as follows：
Ca(OH)2+ SO2→CaSO3+H2O
Ca(OH)2 + SO2+1/2O2→CaSO4+H2O
Ca(OH)2 + SO3→CaSO4+H2O
What wet process sulphuric acid plant came contains SO2、SO3（Sulfuric acid mist）Tail gas from circulating sulfuration bed desulfurization tower bottom venturi section into
Enter, mixed with the absorbent in tower, water injector is arranged on venturi outlet divergent segment, by spray gun by technique water atomization pair
Absorbent calcium hydroxide plays the role of humidification activation, SO3It is highly soluble in water, this allows for SO2、SO3（Sulfuric acid mist）It is anti-with calcium hydroxide
It should be converted into the reaction of ionic type, improve reaction rate and desulfuration efficiency, the exhaust temperature after atomized water spraying is down to higher than its dew point
30 DEG C or more, optimum temperature needed for both ensure that reaction also avoids dew point corrosion, whole system does not need anti-corrosion.According to
Desulfurizing tower outlet temperature controls the water return amount of atomizing lance, to control the amount of water sprayed of desulfurizing tower, desulfurizing tower is made to export smoke temperature control
System is at 80 ~ 90 DEG C or so.According to SO in chimney breast cleaning of off-gas2、SO3（Sulfuric acid mist）Concentration adjust niter in desulfurizing tower
The magnitude of recruitment of ash.When device load is lower than the 60% of Design cooling load, cleaning exhaust gas recirculation circuit is opened, Partial cleansing tail is made
Gas returns on circulating fluidized bed desulfurization tower inlet pipeline, it is ensured that the stable operation of desulphurization system.
There is maximum slip velocity in circulating fluidized bed desulfurization tower, between tail gas and hydrated lime particle, enhances gas-solid
Between mixing, improve mass transfer, heat transfer efficiency, meet SO3The condition that aerosol is reacted with calcium hydroxide efficient chemical.Desulfurizing tower
The inertial separation of top structure further enhances the return of floccule, further improve tower endoparticle bed density and
Ca/S ratio extends calcium hydroxide and SO2 、SO3（Sulfuric acid mist）Reaction time, further enhance the heat and mass transport between gas-solid,
To realize that high desulfurization rate provides basic assurance.The tail gas of the powder containing calcium hydroxide enters in subsequent bag filter, by dedusting
Material a part that device is collected is back in circulating fluidized bed desulfurization tower through returning charge skewed slot to be recycled, another part conveying
To grey library, cleaning of off-gas smoke evacuation chimney after air-introduced machine.
The above described is only a preferred embodiment of the present invention, be not intended to limit the present invention in any form, though
So the present invention has been disclosed as a preferred embodiment, and however, it is not intended to limit the invention, any technology people for being familiar with this profession
Member, without departing from the scope of the present invention, when the technology contents using the disclosure above make a little change or modification
It is right according to the technical essence of the invention for the equivalent embodiment of equivalent variations, but without departing from the technical solutions of the present invention
Any simple modification, equivalent change and modification made by above embodiments, all of which are still within the scope of the technical scheme of the invention.
Claims (9)
1. a kind of sour gas wet process acid-making process combined with semidry method tail gas desulfurization, it is characterised in that：Containing H2The sour gas of S
Enter in sour gas burning furnace with the excessive hot-air of fuel gas, secondary air fan, ignition temperature controls the burning at 900-1300 DEG C
Process gas afterwards cools to 390-420 DEG C after the heat exchange of sour gas waste heat boiler and enters SO 2 converter, through dioxy
Change the 270-290 DEG C of process gas that sulphur converter comes out to enter in the condensation of sulfuric acid device using air as cooling medium, condensation of sulfuric acid
The sulfuric acid of device bottom outflow enters sulfuric acid mixing channel after closing with the cold acid-mixed of circulation, then is cooled to 40 DEG C as production through sulfuric acid water cooler
Product sulfuric acid sends out battery limit (BL), and the temperature that the 80-100 DEG C of tail gas and condensation of sulfuric acid device come out at the top of condensation of sulfuric acid device comes out is 210
After DEG C -230 DEG C of part hot-air mixing, relieving haperacidity tail gas that formation temperature is 150 DEG C -160 DEG C and to enter recirculating fluidized bed de-
The venturi section of sulphur tower lower part, comes into full contact with the calcium hydroxide in tower, is sprayed water by atomizing lance into tower, the SO in tail gas2、
SO3It reacts with calcium hydroxide, the tail gas containing calcium hydroxide powder enters in sack cleaner, one collected by sack cleaner
Partially absorb agent under the action of returning charge skewed slot blower through returning charge skewed slot return circulating fluidized bed desulfurization tower in recycle, it is another
Part is delivered to desulfurization ash cellar, cleaning of off-gas smoke evacuation chimney after desulfurization air-introduced machine.
2. a kind of sour gas wet process acid-making process combined with semidry method tail gas desulfurization as described in claim 1, feature exist
In：The water return amount that atomizing lance is controlled according to circulating fluidized bed desulfurization tower outlet temperature, to control to recirculating fluidized bed desulfurization
The amount of water sprayed of tower, so that circulating fluidized bed desulfurization tower exports fibre selection at 80-90 DEG C.
3. a kind of sour gas wet process acid-making process combined with semidry method tail gas desulfurization as described in claim 1, feature exist
In：According to SO in chimney breast cleaning of off-gas2And SO3Concentration adjust circulating fluidized bed desulfurization tower in calcium hydroxide amount, make tail gas
Middle SO2Content be less than 100mg/Nm3, SO3Content be less than 5mg/Nm3。
4. a kind of sour gas wet process acid-making process combined with semidry method tail gas desulfurization as described in claim 1, feature exist
In：Cycle flue is additionally provided between the circulating fluidized bed desulfurization tower inlet tube and chimney inlet tube.
5. a kind of sour gas wet process acid-making process combined with semidry method tail gas desulfurization as described in claim 1, feature exist
In：Controllable register is provided at the air outlet of the desulfurization air-introduced machine.
6. a kind of sour gas wet process acid-making process combined with semidry method tail gas desulfurization as described in claim 1, feature exist
In：The smoke inlet pipeline of the circulating fluidized bed desulfurization tower and the material of venturi section are stainless steel.
7. a kind of sour gas wet process acid-making process combined with semidry method tail gas desulfurization as described in claim 1, feature exist
In：Cloth bag in the bag filter is PTFE cloth bag.
8. a kind of sour gas wet process acid-making process combined with semidry method tail gas desulfurization as described in claim 1, feature exist
In：The part hot-air of the condensation of sulfuric acid device is recycled to sour gas burning furnace as combustion air.
9. a kind of sour gas wet process acid-making process combined with semidry method tail gas desulfurization as described in claim 1, feature exist
In：The circulating fluidized bed desulfurization tower is using the calcium hydroxide of 300-400 mesh as absorbent.
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109943375A (en) * | 2019-03-07 | 2019-06-28 | 四川迅升油气工程技术有限公司 | A kind of device and its technique for sulfur-containing gas individual well desulfurization relieving haperacidity |
| CN111482003A (en) * | 2020-03-20 | 2020-08-04 | 兖矿集团有限公司 | Ultra-low emission method and device for sulfur recovery tail gas |
| CN114307528A (en) * | 2021-12-29 | 2022-04-12 | 司少龙 | System and method for preparing concentrated sulfuric acid by using coke oven flue gas and dry quenching diffused gas |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US6068822A (en) * | 1997-03-24 | 2000-05-30 | Mitsubishi Heavy Industries, Ltd. | Desulforization method and desulfurization apparatus in geothermal power plant |
| US6096279A (en) * | 1997-03-03 | 2000-08-01 | Mitsubishi Heavy Industries, Ltd. | Flue gas treating process and system |
| CN206680184U (en) * | 2017-04-19 | 2017-11-28 | 宁波中科远东催化工程技术有限公司 | A kind of system that high-concentration sulfuric acid is continuously and stably produced using sour gas |
| CN107684808A (en) * | 2017-10-24 | 2018-02-13 | 洛阳瑞昌石油化工设备有限公司 | A kind of sulfur recovery tail gas handling process and system |
| CN207016486U (en) * | 2017-04-19 | 2018-02-16 | 宁波中科远东催化工程技术有限公司 | A kind of system that sulfuric acid is produced using sour gas |
-
2018
- 2018-07-23 CN CN201810813786.7A patent/CN108862207A/en active Pending
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US6096279A (en) * | 1997-03-03 | 2000-08-01 | Mitsubishi Heavy Industries, Ltd. | Flue gas treating process and system |
| US6068822A (en) * | 1997-03-24 | 2000-05-30 | Mitsubishi Heavy Industries, Ltd. | Desulforization method and desulfurization apparatus in geothermal power plant |
| CN206680184U (en) * | 2017-04-19 | 2017-11-28 | 宁波中科远东催化工程技术有限公司 | A kind of system that high-concentration sulfuric acid is continuously and stably produced using sour gas |
| CN207016486U (en) * | 2017-04-19 | 2018-02-16 | 宁波中科远东催化工程技术有限公司 | A kind of system that sulfuric acid is produced using sour gas |
| CN107684808A (en) * | 2017-10-24 | 2018-02-13 | 洛阳瑞昌石油化工设备有限公司 | A kind of sulfur recovery tail gas handling process and system |
Non-Patent Citations (1)
| Title |
|---|
| 孙东旭等: "节能环保型硫酸生产工艺综述", 《宁波化工》 * |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109943375A (en) * | 2019-03-07 | 2019-06-28 | 四川迅升油气工程技术有限公司 | A kind of device and its technique for sulfur-containing gas individual well desulfurization relieving haperacidity |
| CN111482003A (en) * | 2020-03-20 | 2020-08-04 | 兖矿集团有限公司 | Ultra-low emission method and device for sulfur recovery tail gas |
| CN114307528A (en) * | 2021-12-29 | 2022-04-12 | 司少龙 | System and method for preparing concentrated sulfuric acid by using coke oven flue gas and dry quenching diffused gas |
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