CN109569251A - A kind of utilize contains SO2The device and method of flue gas dilute sulfuric acid - Google Patents
A kind of utilize contains SO2The device and method of flue gas dilute sulfuric acid Download PDFInfo
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- CN109569251A CN109569251A CN201910045641.1A CN201910045641A CN109569251A CN 109569251 A CN109569251 A CN 109569251A CN 201910045641 A CN201910045641 A CN 201910045641A CN 109569251 A CN109569251 A CN 109569251A
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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
- B01D53/77—Liquid phase processes
- B01D53/78—Liquid phase processes with gas-liquid contact
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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
- B01D53/507—Sulfur oxides by treating the gases with other liquids
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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
- B01D53/86—Catalytic processes
- B01D53/8603—Removing sulfur compounds
- B01D53/8609—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
- B01D53/86—Catalytic processes
- B01D53/8671—Removing components of defined structure not provided for in B01D53/8603 - B01D53/8668
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- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
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- B01D2257/704—Solvents not covered by groups B01D2257/702 - B01D2257/7027
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2258/00—Sources of waste gases
- B01D2258/02—Other waste gases
- B01D2258/0283—Flue gases
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Abstract
The invention discloses a kind of using containing SO2The device and method of flue gas dilute sulfuric acid, including the cooling and dedusting device connected according to certain way, hypergravity absorption plant, Despumation device, rich solution storage tank, rich solution delivery pump, rich solution flow control valve, dilute stream of sulphuric acid adjustable valve, hypergravity reduction apparatus, dioxygen water storage tank, hydrogen peroxide delivery pump, dioxygen Water flow adjusting valve, this process utilize hypergravity absorption plant by SO2It is removed in depth, improves extraction dilute sulfuric acid concentration, by the way that catalyst is supported on formation hypergravity reduction apparatus on filler, the hydrogen peroxide in dilute sulfuric acid product is effectively decomposed.SO may be implemented in the present invention2Deep removal, effective recycling of Sulphur ressource, while by-product high-quality dilute sulfuric acid is suitable for alkylation plant flue gas, sulfuric acid plant's flue gas etc. and contains SO2The processing of industrial smoke.
Description
Technical field
The present invention relates to a kind of SO using in flue gas2The device and method of dilute sulfuric acid product processed realizes SO2It is removed in depth
While by-product high quality dilute sulfuric acid.
Background technique
Sulfur dioxide (SO2) it is one of main atmosphere pollution, SO2Excessive emissions can be to human health and ecological environment
Bring serious harm.The high speed development of China's industry in recent years, SO2Emissions levels are at 20,000,000 tons/year or so, to control SO2It is dirty
Contaminate the discharge of object, many SO2Removing sulfuldioxide is applied and is given birth to, currently, industrialized sulfur-containing tail gas processing method mainly has lime stone
High SO may be implemented in gypsum, ammonia process, calcium sodium alkali etc., these desulfurization technologies2Removal efficiency, but it is useless to generate desulfurization simultaneously
Gurry, processing difficulty is big, causes secondary pollution to environment.
Dioxygen water desulfurizing process is one of the Wet Flue Gas Desulfurization Technique developed in recent years, and principle is SO2It is given birth to by hydrogen peroxide oxidation
At dilute sulfuric acid, sulfuric acid is a kind of important basic chemical raw materials, is widely used in the industrial process such as metallurgy, alkylation, therefore,
It is control SO using hydrogen peroxide desulfurization by-product sulfuric acid product2Discharge while the effective ways for realizing Sulphur ressource recycling.For
Hydrogen peroxide sulfur removal technology, SO2Removal efficiency is higher, and dilute sulfuric acid product design is higher, and remaining hydrogen peroxide content is lower, then desulfurization work
Skill effect is better.Presently disclosed to be related to the patent of hydrogen peroxide desulfurization technology, there are still one in technological design or technological effect
Determine problem.In 104671221 A of patent CN 105749715 A and CN, to hydrogen peroxide desulphurization mechanism and device connection type into
Description is gone, but there are certain defect, one side desulphurization plant uses traditional tower equipment, such as packed tower, fixed bed etc.
Form, fluid are gravity in the power resources wherein flowed, and the mass transfer separative efficiency in these equipment will receive the influence of gravity,
Lead to SO2It is difficult to be removed in depth, the dilute sulfuric acid product design of extraction is low, and hydrogen peroxide reduction apparatus is also due to gravity limitation is difficult to
Deep decomposition remnants hydrogen peroxide causes dioxygen water residual quantity in dilute sulfuric acid product big；In process flow, the hydrogen peroxide that is newly added and
It is not contacted with sulfurous gas first after sulfur removing pregnant solution mixing, but has first passed through the glide path of circulation extraction, having in this way can
Fresh hydrogen peroxide can be made also not contact to be just directly plucked out of with sulfurous gas and cause the waste of hydrogen peroxide into dilute sulfuric acid product
With the increase of decomposing hydrogen dioxide solution difficulty in dilute sulfuric acid product.In addition, other are related to the patent of hydrogen peroxide desulfurization, there is also technique effects
Deficiency in terms of fruit, disclose in 106606924 A and CN205627604 A of patent CN the method for reporting hydrogen peroxide desulfurization and
Device, but the dilute sulfuric acid product design of its by-product is in 30w% or less；A kind of removing sulfuric acid work is disclosed in 202070285 U of CN
Industry sulfur dioxide in tail gas recycles the device of sulfuric acid, and treated, and sulfur dioxide in tail gas content still has 40~60mg/m3；CN
100354028 C, which are disclosed, reports a kind of method by with hydroperoxidation scrubbing CO_2 from exhaust gas, generation
Still remnants 500ppm hydrogen peroxide in dilute sulfuric acid.The present invention is based on current hydrogen peroxide desulfurization technology there are the problem of, propose one kind
Using containing SO2The device and method of flue gas dilute sulfuric acid, may be implemented SO2Deep removal, the effective use of Sulphur ressource, simultaneously
By-product concentration is higher, the few dilute sulfuric acid product of dioxygen water residual quantity.
Summary of the invention
It is an object of the invention to by SO contained in industrial process flue gas2It is removed in depth, recycling Sulphur ressource and by-product height
Quality dilute sulfuric acid, specifically:
The present invention relates to a kind of using containing SO2The device of flue gas dilute sulfuric acid, comprising: (1) cooling and dedusting device, (2) are super
Gravity absorption plant, (3) Despumation device, (4) rich solution storage tank, (5) rich solution delivery pump, (6) rich solution flow control valve, (7) dilute sulphur
Sour flow control valve, (8) hypergravity reduction apparatus, (9) dioxygen water storage tank, (10) hydrogen peroxide delivery pump, (11) dioxygen water flow
Regulating valve.Wherein, the gas feed of gas vent connection (2) hypergravity absorption plant of described (1) cooling and dedusting device, (2)
The gas vent of hypergravity absorption plant connects (3) Despumation device, and liquid outlet connection (2) hypergravity of (3) Despumation device is inhaled
Receiving apparatus inlet pipe, the liquid outlet of (9) dioxygen water storage tank is by (10) hydrogen peroxide delivery pump and (11) dioxygen water flow tune
It saves valve and connects (2) hypergravity absorption plant liquid inlet conduit, the liquid export line of (2) hypergravity absorption plant connects (4)
The liquid outlet of rich solution storage tank, (4) rich solution storage tank connects two branches by (5) rich solution delivery pump, and one is passed through (6) rich liquid stream
Adjustable valve connects (2) hypergravity absorption plant liquid inlet conduit, and connection (7) dilute stream of sulphuric acid adjustable valve and (8) are super
Gravity reduction apparatus produces line as product.
The present invention provides use above-mentioned apparatus to utilize containing SO2The method of flue gas dilute sulfuric acid, specifically includes the following steps:
(1) contain SO2Flue gas enter cooling and dedusting device, temperature reduces, and wherein entrained solid impurity is removed；
(2) gas in step (1) after cooling dedusting enters hypergravity absorption plant, with absorbent hydrogen peroxide solution super
It is contacted in gravity absorption plant, SO2Into liquid phase, the hydrogen peroxide blend absorbent comprising sulfuric acid, the gas after desulfurization are formed
Into the absorbing liquid of Despumation device removal entrainment, downstream process is discharged or gone to from chimney, and the entrainment absorbing liquid of removing returns super
Gravity absorption plant；
(3) the absorption rich solution in step (2) after desulfurization enters rich solution storage tank, and the rich solution in rich solution storage tank is defeated by rich solution
It send pump and flow control valve to carry out cyclic absorption, is adjusted after dilute sulfuric acid concentration reaches prescribed concentration in rich solution by dilute sulfuric acid flow
Valve extraction；
(4) dilute sulfuric acid is produced after reaching prescribed concentration by dilute stream of sulphuric acid adjustable valve in step (3), also into hypergravity
Original device, filler used in hypergravity reduction apparatus load hydrogen peroxide reducing catalyst, under the effect of the catalyst, extraction it is dilute
Remaining hydrogen peroxide is removed in sulfuric acid, then collects or be sent to downstream process as product；
(5) certain density hydrogen peroxide is stored in dioxygen water storage tank, when detecting hydrogen peroxide concentration in desulfurization absorbing liquid
When too low, being replenished in time for absorbent can be carried out by hydrogen peroxide delivery pump and dioxygen Water flow adjusting valve.
Preferably, the flue-gas temperature in step (1) after cooling dedusting is controlled at 15~50 DEG C.
Preferably, in step (2) hypergravity absorption plant select include but is not limited to rotary packed bed, deflector type,
The hypergravities rotating devices such as fixed-rotor.
Preferably, pressure is 0.05~0.5MPa in hypergravity absorption plant in step (2), and temperature is 15~50 DEG C, is inhaled
Receipts agent initial concentration is 0.1~8w%, and the hypergravity level of hypergravity absorption plant is 80~200, in hypergravity absorption plant
Gas-liquid volume flow ratio is 200~650.
Preferably, the mass fraction of dilute sulfuric acid product is 20~55% in step (3).
Preferably, filler load hydrogen peroxide reducing catalyst used, including but not limited to MnO in step (4)2, CuO,
The catalyst such as Pt, Ag, Cr, catalyst load are 2~10v%, and the hypergravity level of hypergravity reduction apparatus is 90~180.
The present invention may be implemented it is following the utility model has the advantages that
The present invention uses hypergravity absorption plant as core equipment, can strengthen SO2With the gas-liquid mass transfer of hydrogen peroxide system
Process, hypergravity absorption plant gas vent SO2Concentration can be reduced to 25mg/m3Hereinafter, Sulphur ressource almost all enters dilute sulfuric acid
Product realizes SO2Deep removal and Sulphur ressource effective use；Due to SO2Removal efficiency it is high, dilute sulfuric acid can be
It is produced under the higher concentration of 40w% or more, reduces the difficulty that dilute sulfuric acid purification is the concentrated sulfuric acid；Process is also original-pack using hypergravity
It sets, by MnO2Etc. decomposing hydrogen dioxide solutions catalyst be loaded on the filler of hypergravity reduction apparatus, liquid phase is crushed by filler, is exposed
More areas and catalyst contact, and the concentration of remaining hydrogen peroxide can be reduced to 300ppb hereinafter, improving in dilute sulfuric acid product
The quality of dilute sulfuric acid product.Meanwhile pollution-free waste generates, and process is simple, and it is easy for installation, it is suitable for alkylation tail gas, sulphur
Acid plant tail gas etc. contains SO2The treatment process of industrial smoke.
Detailed description of the invention
Fig. 1 is proposed by the present invention a kind of using containing SO2The schematic device of flue gas dilute sulfuric acid.
In Fig. 1: 1- cooling and dedusting device, 2- hypergravity absorption plant, 3- Despumation device, 4- rich solution storage tank, 5- rich solution are defeated
Send pump, 6- rich solution flow control valve, 7- dilute stream of sulphuric acid adjustable valve, 8- hypergravity reduction apparatus, 9- dioxygen water storage tank, 10- is bis-
Oxygen water delivery pump, 11- dioxygen Water flow adjusting valve.
Specific embodiment
Referring to shown in attached drawing, embodiment of the present invention is described further with reference to the accompanying drawings and examples.
It is utilized using the device of the invention and method and contains SO2Flue gas dilute sulfuric acid, process are as follows: containing SO2Flue gas it is first
It is introduced into cooling and dedusting device, flue-gas temperature reduces OK range, wherein the solid impurity contained is removed, after the dedusting that cools down
Flue gas enters hypergravity absorption plant, contacts in hypergravity absorption plant with the hydrogen peroxide solution of certain initial concentration, flue gas
In SO2It is rapidly absorbed into liquid phase, the flue gas after desulfurization leaves from hypergravity absorption plant gas vent, goes by Despumation device
Except downstream process is sent to after the absorbing liquid of entrainment, entrainment absorbing liquid returns to hypergravity absorption plant, and the rich solution after desulfurization enters
Rich solution storage tank, the rich solution in rich solution storage tank is recycled by rich solution delivery pump and rich solution flow control valve, when in rich solution
Sulfuric acid concentration reach a certain concentration after, can be produced by dilute stream of sulphuric acid adjustable valve, the dilute sulfuric acid of extraction by hypergravity also
Original device removes wherein remaining a small amount of hydrogen peroxide, then collects or be sent to downstream process as dilute sulfuric acid product.
Embodiment 1
It is utilized using above-mentioned apparatus and method and contains SO2Flue gas dilute sulfuric acid.Wherein, the temperature control of flue gas cool-down dedusting exists
25 DEG C, for the control of hypergravity absorption plant temperature at 25 DEG C, pressure 0.1MPa, hydrogen peroxide initial concentration is 2w%, hypergravity water
Putting down is 100, and 450, the mass fraction control of dilute sulfuric acid product exists the flow-ratio control of gas-liquid volume in hypergravity absorption plant
45w%, the load of hydrogen peroxide reduction used catalyst are 5v%, and the hypergravity level of hypergravity reduction apparatus is 120.
Gas sample is taken to analyze in Despumation device gas vent, SO2Concentration is 15mg/m3, export and sample in hypergravity reduction apparatus
It analyzes, hydrogen peroxide content is 280ppb in dilute sulfuric acid product.
Embodiment 2~25
Process flow and step are the same as embodiment 1, the temperature of each embodiment, pressure, hydrogen peroxide concentration, hypergravity absorption plant
Horizontal, the hydrogen peroxide reducing catalyst load capacity with the hypergravity of hypergravity reduction apparatus, gas-liquid volume in hypergravity absorption plant
Flow-rate ratio, dilute sulfuric acid concentration and Despumation device gas vent SO2Concentration, hydrogen peroxide content the results are shown in Table 1 in dilute sulfuric acid product.
The process conditions and experimental result of each embodiment of table 1
Note: T1Temperature after flue gas cool-down dedusting；T2Hypergravity absorption plant temperature；P1Hypergravity absorption plant pressure
Power；
ω hydrogen peroxide-hydrogen peroxide initial concentration；β1The hypergravity of hypergravity absorption plant is horizontal；G/L- gas-liquid volume flow
Amount ratio；
ω dilute sulfuric acid-dilute sulfuric acid controlled concentration；β2The hypergravity of hypergravity reduction apparatus is horizontal；Hydrogen peroxide reduction catalysts
Agent load capacity；
SO2SO in concentration-Despumation device exit gas2Concentration；Hydrogen peroxide content in C hydrogen peroxide-dilute sulfuric acid product
Comparative example 1~12
Process flow and step are the same as embodiment 1, the temperature of each comparative example, pressure, hydrogen peroxide concentration, hypergravity absorption plant
Horizontal, the hydrogen peroxide reducing catalyst load capacity with the hypergravity of hypergravity reduction apparatus, gas-liquid volume in hypergravity absorption plant
Flow-rate ratio, dilute sulfuric acid concentration and Despumation device gas vent SO2Concentration, hydrogen peroxide content the results are shown in Table 2 in dilute sulfuric acid product.
The process conditions and experimental result of each comparative example of table 2
Note: T1Temperature after flue gas cool-down dedusting；T2Hypergravity absorption plant temperature；P1Hypergravity absorption plant pressure
Power；
ω hydrogen peroxide-hydrogen peroxide initial concentration；β1The hypergravity of hypergravity absorption plant is horizontal；G/L- gas-liquid volume flow
Amount ratio；
ω dilute sulfuric acid-dilute sulfuric acid controlled concentration；β2The hypergravity of hypergravity reduction apparatus is horizontal；Hydrogen peroxide reduction is urged
Agent load capacity；
SO2SO in concentration-Despumation device exit gas2Concentration；Hydrogen peroxide content in C hydrogen peroxide-dilute sulfuric acid product
Comparative example 13
As described in Example 1, other conditions are constant, and hypergravity absorption plant is changed to the identical packed tower of packing volume.
Gas sample is taken to analyze in Despumation device gas vent, SO2Concentration is greater than 100mg/m3, exported in hypergravity reduction apparatus
Sampling analysis, hydrogen peroxide content is 305ppb in dilute sulfuric acid product.
Comparative example 14
As described in Example 1, other conditions are constant, and hypergravity reduction apparatus is changed in equal volume, wait filling out for catalyst load
Expect tower.
Gas sample is taken to analyze in Despumation device gas vent, SO2Concentration is 28mg/m3, export and sample in hypergravity reduction apparatus
It analyzes, hydrogen peroxide content is 950ppb in dilute sulfuric acid product.
Comparative example 15
As described in Example 1, other conditions are constant, and the liquid delivery tube routing connection after dioxygen Water flow adjusting valve is overweight
The liquid inlet conduit of power absorption plant is changed to the export pipeline of connection hypergravity absorption plant.
In Despumation device gas vent sampling analysis, SO2Concentration is 30mg/m3, in hypergravity reduction apparatus outlet sampling point
It analyses, the hydrogen peroxide content in dilute sulfuric acid product is 340ppb.
Temperature after flue gas cool-down, the temperature and pressure in hypergravity absorption plant, hypergravity is horizontal, gas-liquid volume flow
Than and extraction when dilute sulfuric acid concentration be influence SO2The key factor of removal effect.Temperature and hypergravity after flue gas cool-down are inhaled
Temperature is identical in receiving apparatus, and temperature is too low, hydrogen peroxide and SO2Reactivity decline, temperature is excessively high, the resolution ratio meeting of hydrogen peroxide
It improves；Pressure in hypergravity absorption plant will affect SO2Solubility in absorbing liquid, pressure is higher, and solubility is bigger, more
Be conducive to the progress absorbed, but when pressure rise is to a certain degree, gas-liquid mass transfer efficiency can be restricted by other degree and is difficult to
Continue to improve, requirement of the high pressure to equipment is maintained also to correspondingly increase；The concentration of hydrogen peroxide is higher, with SO2Reaction rate it is faster,
However also it is easy to make in final products remaining hydrogen peroxide concentration excessively high；The hypergravity level of hypergravity absorption plant is the pass of equipment
Bond parameter, it is adjusted by changing the revolving speed of hypergravity absorption equipment, and revolving speed is higher, and liquid phase can be fractured into smaller micro-
Member exposes more surface areas and improves mass-transfer efficiencies, but the raising of revolving speed shortens but also liquid is thrown away more quickly
The time of gas-liquid contact；Gas-liquid volume flow ratio is also the key for influencing assimilation effect, and small gas liquid ratio condition has better
Assimilation effect, but unit absorbing liquid processing contain SO2Exhaust gas volumn is small；The accumulation of dilute sulfuric acid, as previously mentioned, will lead to assimilation effect
Decline, but in order to reduce the difficulty of dilute sulfuric acid purification, it is often desirable that obtain the higher dilute sulfuric acid product of concentration；So these works
Skill condition needs to control in suitable range, could obtain good SO under the premise of matter energy consumes small as far as possible2Removing
Effect and dilute sulfuric acid product.Decomposition for remaining hydrogen peroxide in extraction dilute sulfuric acid, equally strengthens dioxygen using high-gravity technology
The hypergravity level of the reduction process of water, catalyst loadings and hypergravity reduction apparatus is the important parameter of this process, is urged
Agent load capacity is too low to be likely to result in liquid and just leaves without catalyst, so that mass-transfer efficiency is reduced, in catalyst amount
In the case where abundance, decomposing hydrogen dioxide solution will be limited by other factors；Influence of the hypergravity level to decomposing hydrogen dioxide solution effect is similar
In to SO2The influence of absorption process, hypergravity level is higher, liquid be broken degree height, the area that liquid is contacted with catalyst
It is bigger, and on the other hand, hypergravity level is higher, and the time that liquid is contacted with catalyst is shorter；Therefore, the decomposition of hydrogen peroxide
Journey needs to control the load of catalyst and the hypergravity level of hypergravity reduction apparatus.
In conclusion in order to guarantee SO2Removal effect, dilute sulfuric acid product quality and decomposing hydrogen dioxide solution efficiency are in preferable water
Flat, the process conditions being related to should be controlled in suitable range, if condition control is improper, it will cause the decline of technological effect or
The increase of operation difficulty, cost.
The above description is merely a specific embodiment, but scope of protection of the present invention is not limited thereto, any
Those familiar with the art in the technical scope disclosed by the present invention, can easily think of the change or the replacement, and should all contain
Lid is within protection scope of the present invention.Therefore, protection scope of the present invention should be based on the protection scope of the described claims.
Claims (8)
1. a kind of using containing SO2The device of flue gas dilute sulfuric acid characterized by comprising cooling and dedusting device (1), hypergravity are inhaled
Receiving apparatus (2), Despumation device (3), rich solution storage tank (4), rich solution delivery pump (5), rich solution flow control valve (6), dilute sulfuric acid flow
Regulating valve (7), hypergravity reduction apparatus (8), dioxygen water storage tank (9), hydrogen peroxide delivery pump (10), dioxygen Water flow adjusting valve
(11)；Wherein, the gas feed of gas vent connection hypergravity absorption plant (2) of the cooling and dedusting device (1), hypergravity
The gas vent of absorption plant (2) connects Despumation device (3), and the liquid outlet of Despumation device (3) connects hypergravity absorption plant
(2) liquid outlet of inlet pipe, dioxygen water storage tank (9) passes through hydrogen peroxide delivery pump (10) and dioxygen Water flow adjusting valve (11)
Hypergravity absorption plant (2) liquid inlet conduit is connected, the liquid export line of hypergravity absorption plant (2) connects rich solution storage tank
(4), the liquid outlet of rich solution storage tank (4) connects two branches by rich solution delivery pump (5), and one is passed through rich solution flow control valve
(6) hypergravity absorption plant (2) liquid inlet conduit, a connection dilute stream of sulphuric acid adjustable valve (7) and hypergravity reduction are connected
Device (8) produces line as product.
2. the apparatus according to claim 1, the hypergravity absorption plant (2) and hypergravity reduction apparatus (8) are selected from rotation
Turn the hypergravities rotating devices such as packed bed, deflector type, fixed-rotor.
3. a kind of method using claim 1 described device dilute sulfuric acid, which is characterized in that this method includes the following steps:
(1) contain SO2Flue gas enter cooling and dedusting device, temperature reduces, and wherein entrained solid impurity is removed；
(2) gas in step (1) after cooling dedusting enters hypergravity absorption plant, with absorbent hydrogen peroxide solution in hypergravity
It is contacted in absorption plant, SO2Into liquid phase, the hydrogen peroxide blend absorbent comprising sulfuric acid is formed, the gas after desulfurization enters
The absorbing liquid of Despumation device removal entrainment, is discharged or goes to downstream process from chimney, and the entrainment absorbing liquid of removing returns to hypergravity
Absorption plant；
(3) the absorption rich solution in step (2) after desulfurization enters rich solution storage tank, and the rich solution in rich solution storage tank passes through rich solution delivery pump
Cyclic absorption is carried out with flow control valve, is adopted after dilute sulfuric acid concentration reaches prescribed concentration in rich solution by dilute stream of sulphuric acid adjustable valve
Out；
(4) dilute sulfuric acid is produced after reaching prescribed concentration by dilute stream of sulphuric acid adjustable valve in step (3), also original-pack into hypergravity
It sets, filler used in hypergravity reduction apparatus loads hydrogen peroxide reducing catalyst, under the effect of the catalyst, the dilute sulfuric acid of extraction
The hydrogen peroxide of middle remnants is removed, and then collects or be sent to downstream process as product；
(5) certain density hydrogen peroxide is stored in dioxygen water storage tank, when detecting that hydrogen peroxide concentration is too low in desulfurization absorbing liquid
When, it can be replenished in time by hydrogen peroxide delivery pump and dioxygen Water flow adjusting valve.
4. technique according to claim 3, which is characterized in that the flue-gas temperature control in step (1) after cooling dedusting exists
15~50 DEG C.
5. technique according to claim 3, which is characterized in that pressure is 0.05 in hypergravity absorption plant in step (2)
~0.5MPa, temperature are 15~50 DEG C, and absorbent initial concentration is 0.1~8w%, and the hypergravity of hypergravity absorption plant is horizontal
It is 80~200, gas-liquid volume flow ratio is 200~650 in hypergravity absorption plant.
6. technique according to claim 3, which is characterized in that in step (3) mass fraction of dilute sulfuric acid product be 20~
55w%.
7. technique according to claim 3, which is characterized in that filler load hydrogen peroxide reduction catalysts used in step (4)
Agent loads as 2~10v%, and the hypergravity level of hypergravity reduction apparatus is 90~180.
8. technique according to claim 7, which is characterized in that the reducing catalyst is selected from MnO2, CuO, Pt, Ag, Cr etc.
Catalyst.
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111268657A (en) * | 2020-01-22 | 2020-06-12 | 浙江迪邦化工有限公司 | Method and system for continuously producing nitrosyl sulfuric acid |
| CN112090273A (en) * | 2020-08-28 | 2020-12-18 | 中北大学 | Photocatalyst-loaded filler and its high-gravity NO removalxApparatus and process of |
| CN112473351A (en) * | 2020-11-26 | 2021-03-12 | 赛得利(九江)纤维有限公司 | Hypergravity washing and dust removing method |
| CN112657325A (en) * | 2019-10-15 | 2021-04-16 | 中国石油化工股份有限公司 | Method for removing nitrogen oxides from gas |
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| CN112473351A (en) * | 2020-11-26 | 2021-03-12 | 赛得利(九江)纤维有限公司 | Hypergravity washing and dust removing method |
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