CN104560223A - Gas desulfurization device and method thereof - Google Patents
Gas desulfurization device and method thereof Download PDFInfo
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- CN104560223A CN104560223A CN201410759406.8A CN201410759406A CN104560223A CN 104560223 A CN104560223 A CN 104560223A CN 201410759406 A CN201410759406 A CN 201410759406A CN 104560223 A CN104560223 A CN 104560223A
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K1/00—Purifying combustible gases containing carbon monoxide
- C10K1/002—Removal of contaminants
- C10K1/003—Removal of contaminants of acid contaminants, e.g. acid gas removal
- C10K1/004—Sulfur containing contaminants, e.g. hydrogen sulfide
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K1/00—Purifying combustible gases containing carbon monoxide
- C10K1/08—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors
- C10K1/10—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors with aqueous liquids
- C10K1/12—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors with aqueous liquids alkaline-reacting including the revival of the used wash liquors
- C10K1/124—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors with aqueous liquids alkaline-reacting including the revival of the used wash liquors containing metal compounds other than alkali- or earth-alkali carbonates, hydroxides- or oxides- or salts of inorganic acids derived from sulfur
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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
- 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
- Y02P20/151—Reduction of greenhouse gas [GHG] emissions, e.g. CO2
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Abstract
The invention provides a gas desulfurization device and a method thereof. Based on the difference of three gases in acidity and solubility, SO2 in the gas is quickly washed by use of the soluble alkaline washing liquid such as Na2CO3 and MgO, and H2S is washed off by a wet catalytic oxidation method by adopting a supergravity bed with selective absorption washing ability and adopting Na2CO3 or NH3H2O and the like as an alkali source to finally achieve the aim of desulfurization. The gases H2S and SO2 are selectively absorbed by adopting the main reaction equipment such as a venturi tower, a rotating packed bed and an ejecting regenerator and using the special properties of the equipment, and the gas desulfurization process is realized while the alkali consumption and energy consumption of the system are reduced. The desulfurization effect is good, the cost is low, and little difficulty is caused; and meanwhile, the finished product of sulfur can be recycled to protect the environment. If further removal of CO2 is required, an adsorption-desorption method can be adopted.
Description
Technical field
The present invention relates to a kind of containing H
2s, SO
2, CO
2in the fuel such as coal gas, Sweet natural gas, shale gas of impurity component or the purification process technique of unstripped gas and equipment, the purification process technique especially relating to a kind of semicoke coal gas and device.
Background technology
The raw materials such as coal gas Sweet natural gas, fuel gas have a wide range of applications mode, mainly contain: produce other Chemicals as unstripped gas, produce special rolling-mill section, as fuel for the generating of coal gas steam turbine, MAGNESIUM METAL gas making, coal tar processing, lime kilning, machine brick, building block, solid caustic soda, gas turbines for power generation, oil engine generating, methyl alcohol processed, city air feed etc.No matter be which kind of Land use systems, all will carry out desulfurization, front desulfurization and rear desulfurization can be divided into according to the position of desulfurization.
Desulfurization after 1
Rear desulfurization mentioned here refer to gas utilize complete after again desulfurization is carried out to the waste gas, the flue gas that produce, as first coal gas being used for generating, then to the flue gas desulfurization produced after generating, at this moment because of H after burning
2s is converted into SO
2, after desulfurization process to as if flue gas, main desulfurization be SO
2.This method must be that coal gas carries out as after fuel combustion, and the technique of producing other Chemicals as unstripped gas for coal gas is not suitable for.
Desulfurization before 2
Front desulfurization refers to that coal gas enters later use operation after first carrying out desulfurization again, as first carried out desulfurization to coal gas, then the coal gas after desulfurization is generated electricity, MAGNESIUM METAL processed or other utilize etc.Front desulfurization process to as if coal gas, that mainly slough is H in coal gas
2s and SO
2.
3 front desulfurization and rear desulfurization are compared
First large 7 ~ 10 times of volume ratio burning after gas-fired, therefore, the gas volume of the required process of rear desulfurization is large compared with front desulfurization, and required equipment is also large compared with front desulfurization; The second, for the technique that coal gas need be utilized as unstripped gas, rear desulfurization can not be adopted; 3rd, the sour gas contained in coal gas during rear desulfurization can damage equipment, pipeline, therefore, and desulfurization gas treatment desulfurization before adopting as far as possible.
The raising again and again of national environmental standard, requires that coal gas, Sweet natural gas, coking industry need further Optimization Technology, improves level of purification, H
2s concentration requirement is by original 200mg/m
3bring up to 20mg/m
3.Future may require higher, is less than 5mg/m
3.For the semicoke coal gas in coking industry, because its gas composition is special, simultaneously containing H
2s, SO
2, CO
2deng sour gas, if adopt the treatment technology of high-temperature coking gas purification process, emission request can not be reached.
1 blue charcoal gas composition is analyzed
Semicoke also claims blue charcoal, and the principle of its producer and high-temperature coking are not high, and cause the coke-oven gas of blue charcoal coal gas ratio of components high temperature carbonization complicated because part coal gas melts down secondary combustion, major impurity contains H
2s, SO
2, CO
2, N
xo etc.
The caloric power of gas that blue charcoal coke oven is produced is low, is about 1609 ~ 2017kcal/Nm
3, NH in coal gas
3lower, the H of content
2s and SO
2content also low, but CO
2content is comparatively large, and therefore, carrying out desulfurization to this coal gas is at high CO
2de-H is carried out under concentration
2s and SO
2technique.
In above-mentioned three kinds of gases, SO
2acidity the strongest, because of H
2s and CO
2all weak diacid, their acidity mainly based on primary ionisation, H
2the primary ionisation constant of S is less than CO
2ionization constant once, i.e. H
2the acidity of S compares CO
2weak, if so adopt traditional High-temperature carbonization coal qi exhaustion H
2during the technique of S, due to CO
2existence can have an impact to sweetening effectiveness.Research finds, H
2the solvability of S compares CO
2by force, the CO when reaction times is in 5s
2impact can ignore, but after being above 5s, CO
2impact can be super next superpower, consume alkali lye amount and increase, cause sweetening effectiveness obviously to reduce.Therefore adopt traditional coal gas desulfurization technique to carry out desulfurization to blue charcoal coal gas and do not reach desirable effect.
2 traditional coal desulfurization techniques are used for the comparison of blue charcoal desulfurization
2.1 catalytic wet oxidation techniques
Catalytic wet oxidation technique is the main coal gas desulfurization technique of current China coking industry, is under the effect of catalyzer, utilizes the ammonia in coal gas or additional sodium carbonate to be the H in alkali source absorption coal gas
2the technique of S.Absorb H
2doctor solution after S send regeneration section to carry out oxidation regeneration, by the H absorbed
2s separates out and forms sulphur simple substance, to defoam groove, then carries out centrifugal or melting treatment, generate raw sulphur or ripe sulphur with the gravity flow of the form of sulphur foam.Usual catalytic wet oxidation technique has PDS, tannin extract, HPF, FRC etc.; Sweetener form has high tower reclaiming process, regeneration tank reclaiming process, a tower desulfurization regeneration technique, a tower half formula desulfurization regeneration technique etc.
When adopting catalytic wet oxidation technique to be used for blue charcoal coal gas desulfurization, doctor solution is absorbing the H in coal gas
2can with the SO in coal gas while S
2reaction, generates (NH
3)
2sO
3or Na
2sO
3, it cannot react sulfur removing pregnant solution regeneration NH with oxygen in regeneration tank or regenerator column
3h
2o or Na
2cO
3solution, can generate (NH on the contrary
3)
2sO
4or Na
2sO
4deng secondary salt, therefore, due to SO
2existence, desulfurization regeneration effect reduces greatly, and the consumption of doctor solution increases greatly, keep identical assimilation effect, must add more fresh desulfurization alkali lye continuously in system.
In addition, the packing tower tower speed adopted due to Wet Catalytic Oxidation Method desulfurization is generally 0.4 ~ 0.6m/s, and absorber portion height is about 15m, and the reaction times is much larger than 5s, CO
2impact very large, partial desulfurization alkali lye can be consumed, sweetening effectiveness is reduced.
Therefore, it is impracticable that the Wet Catalytic Oxidation Method of high temperature coke oven coal gas desulfurization is applied to blue charcoal coal gas desulfurization, need adjust it, removes SO
2and CO
2interference.
2.2 absorption and desorption techniques
Conventional absorption and desorption method has hydramine method, vacuum carbonation, AS method etc., is utilize absorption liquid and coal gas counter current contact, absorbs the H in coal gas
2s, absorbs H
2sulfur removing pregnant solution after S send desorption and regeneration in reclaim equiment, and the lean solution of generation send the H in thionizer cyclic absorption coal gas
2s, the sour gas of generation removes acid-producing apparatus, produces sulfuric acid.
Because containing SO in blue charcoal coal gas
2, CO
2and O
2, can consume a large amount of circulation desulfurization liquid, and make the sulfurous acid thing of generation be oxidized to sulfuric acid thing, secondary salt growing amount strengthens; A large amount of CO
2exist and make H in desorb acid gas
2the concentration of S reduces, and increases cost and the difficulty of relieving haperacidity, optionally need absorb H
2s, therefore, absorption and desorption process application in blue charcoal desulfurization be also problematic.
2.3 dry desulfurization
Dry process utilizes solid adsorbent to remove hydrogen sulfide in coal gas and organosulfur, the degree of purification of desulfurization is higher, be applicable to lean sulphurous gas process, be used for fine de-sulfur, operation is simple and reliable, at present conventional sweetening agent is inexpensive ferric oxide, and other as the sweetening agents such as gac, molecular sieve, manganese oxide, zinc oxide all costly, less use; For identical coal gas treatment capacity, the equipment of dry desulfurization is huge, and sweetening agent is changed frequent, and consumption is large, not easily regenerate, cause process cost to increase, labour intensity is large, can not reclaim finished product sulphur, waste desulfurizing agent, waste gas, waste water serious environment pollution, therefore general tolerance is greater than 20000Nm simultaneously
3the coal gas of/h does not consider dry desulfurizing process.
Summary of the invention
For prior art Problems existing, the invention provides a kind of gas desulfurizer and method thereof, utilize three kinds of gaseous acidic, deliquescent difference, first use Na
2cO
3or the SO in the deliquescent alkaline detergent solution quick wash coal gas such as MgO
2, then by having the hypergravity bed of selective absorbing washability, with Na
2cO
3or NH
3h
2o etc. are alkali source, remove H with Wet Catalytic Oxidation Method washing
2s, finally reaches the object of desulfurization.Sweetening effectiveness is good, and cost is low, difficulty is little, can also reclaim finished product sulphur, protection of the environment simultaneously.
Technical scheme of the present invention is: a kind of gas desulfurizer, comprises venturi tower, circulation liquid pool, rotary packed bed, rich solution groove, jet regeneration device, regeneration tank, lean solution and H
2s rinse bath;
Be provided with crude gas import bottom described venturi tower, middle part is Venturi district, top is spraying layer; Described spraying layer inside is provided with the first alkaline detergent solution, and spraying layer sidewall opening connects washings pipe gravity flow pipeline, and described washings pipe gravity flow pipeline is provided with SO
2cleaning circulation pump and waste liquid outlet and the other end is communicated to circulation liquid pool;
Described circulation liquid pool is provided with the first alkali lye liquid-inlet pipe, inside is provided with oxidation unit, oxidation unit is provided with oxidation air inlet pipe;
Air outlet, described venturi tower top pipeline is connected to rotary packed bed inlet mouth, and rotary packed bed air outlet pipeline is connected to peripheral equipment, and rotary packed bed rich solution outlet conduit is connected to rich solution groove;
The liquid outlet of described rich solution groove is connected to the fluid inlet of jet regeneration device by rich solution circulating pump pipeline, described jet regeneration device is provided with air from suction inlet, and the mixed solution after the air reaction of rich solution and self-priming is delivered in regeneration tank through the liquid outlet of jet regeneration device;
Described regeneration tank top is provided with regulator of level and sulphur foam outlet, and the liquid outlet pipeline of regulator of level is connected to lean solution and H
2s rinse bath, described lean solution and H
2the liquid outlet of S rinse bath is by lean solution and H
2s washing pump pipeline is connected to rotary packed bed fluid inlet, and described lean solution and H
2s rinse bath is provided with the second alkali lye liquid-inlet pipe;
Described sulphur foam outlet is connected to desulfuration foam treatment system.
Further, described Venturi district comprises the Venturi-type pipe that space is left in several centres side by side.
Further, described jet regeneration device is Venturi spray tube.
The present invention also provides a kind of coal gas desulfurization method, and concrete steps are as follows:
(1) crude gas enters bottom venturi tower by crude gas import, and the first alkaline detergent solution upwards sprayed with spraying layer after Venturi district accelerates reacts, and removes the SO in gas after reaction
2, generate sulphite, the washings with sulphite flows automatically to circulation liquid pool by washings pipe gravity flow pipeline, then by SO
2cleaning circulation pump pressurization is sent to venturi tower circulated sprinkling;
(2) in circulation liquid pool, oxidation unit is set, oxidation air enters oxidation unit by oxidation air inlet pipe, be vitriol by sulfite oxidation, when the sulfate concentration in circulation liquid pool reaches set(ting)value, discharged by waste liquid outlet, in circulation liquid pool, add the first alkaline detergent solution by the first alkali lye liquid-inlet pipe simultaneously;
(3) SO is removed through venturi tower washing
2coal gas by air outlet, top be delivered to rotary packed bed in, rotate through rotary packed bed the hypergravity reaction zone and lean solution and H that produce
2the second alkaline detergent solution reaction that S washing pump is delivered to, the H in washing absorption coal gas
2s, the coal gas after purification is delivered to peripheral equipment by rotary packed bed air outlet;
(4) by rotary packed bed absorption H
2rich solution after S flows automatically to rich solution groove, then sends into jet regeneration device by rich solution recycle pump, H
2s reacts rich solution through the reacted rich solution of jet regeneration device mixing air self-suction further reaction regeneration in regeneration tank, and the lean solution after regeneration flows automatically to lean solution and H through regeneration tank top regulator of level
2s rinse bath, by lean solution and H
2s washing pump sends into rotary packed bed circulation cleaning;
(5) the sulphur foam that sulfur removing pregnant solution regenerative response produces is delivered to sulphur foam treatment system by the sulphur foam outlet at regeneration tank top, produces raw sulphur or sulphur;
(6) along with the carrying out of reaction, the alkali concn in system constantly reduces, by the second alkali lye liquid-inlet pipe to lean solution and H
2the second alkaline detergent solution is added in S rinse bath.
Further, the coal gas in step (3) after purification is delivered to peripheral equipment, if need remove CO further to the coal gas after purification
2, the method that absorption can be adopted to resolve is removed.
Further, described first alkaline detergent solution is Na
2cO
3, MgO, Ca (OH)
2, CaCO
3or NH
3h
2o.
Further, described second alkaline detergent solution is Na
2cO
3or NH
3h
2o.
The invention has the beneficial effects as follows: a kind of gas desulfurizer and method thereof are provided, utilize three kinds of gaseous acidic, deliquescent difference, first use Na
2cO
3or the SO in the deliquescent alkaline detergent solution quick wash coal gas such as MgO
2, then by having the hypergravity bed of selective absorbing washability, with Na
2cO
3or NH
3h
2o etc. are alkali source, remove H with Wet Catalytic Oxidation Method washing
2s, finally reaches the object of desulfurization.Adopt the principal reaction equipment such as venturi tower, rotary packed bed, jet regeneration device and use the property of each equipment optionally to absorb H
2s, SO
2gas, achieves the sweetening process of coal gas.Reduce system alkaline consumption and energy consumption simultaneously.Sweetening effectiveness is good, and cost is low, difficulty is little, can also reclaim finished product sulphur, protection of the environment simultaneously.CO is removed further if also need
2, available absorption analytic method is removed.
Accompanying drawing explanation
Fig. 1 is the system diagram of apparatus of the present invention.
Embodiment
Below in conjunction with accompanying drawing, the present invention is described further.
The present invention utilizes three kinds of gaseous acidic, deliquescent difference, first uses Na
2cO
3or the SO in the deliquescent alkaline detergent solution quick wash coal gas such as MgO
2, then by having the hypergravity bed of selective absorbing washability, with Na
2cO
3or NH
3h
2o etc. are alkali source, remove H with Wet Catalytic Oxidation Method washing
2s, finally reaches the object of desulfurization.Sweetening effectiveness is good, and cost is low, difficulty is little, can also reclaim finished product sulphur, protection of the environment simultaneously.CO is removed further if also need
2, available absorption analytic method is removed.
With Na
2cO
3for absorption washing composition is example, its technological principle is:
SO
2absorption reaction principle:
SO
2+Na
2CO
3+H
2O→2NaHSO
3
SO
2+Na
2CO
3→Na
2SO
3+CO
2
2NaHSO
3+Na
2CO
3→2Na
2SO
3+CO
2+H
2O
2Na
2SO
3+O
2→2Na
2SO
4
H
2s absorber portion reaction principle:
H
2S+Na
2CO
3→NaHS+NaHCO
3
Na
2CO
3+H
2S→Na
2S+H
2O+CO
2
Na
2CO
3+CO
2+H
2O→2NaHCO
3
H
2the primitive reaction occurred in S regeneration tank is as follows:
NaHS+1/2O
2→NaOH+S↓
Na
2S+1/2O
2+H
2O→2NaOH+S↓
Na
2S
X+1/2O
2+H
2O→2NaOH+S
X
Except above reaction, also carry out following side reaction:
2NaHS+2O
2→Na
2S
2O
3+H
2O
2Na
2S
2O
3+O
2→2Na
2SO
4+2S↓
As shown in Figure 1, system construction drawing of the present invention, a kind of gas desulfurizer, comprises venturi tower 2, circulation liquid pool 9, rotary packed bed 5, rich solution groove 10, jet regeneration device 12, regeneration tank 13, lean solution and H
2s rinse bath 14; Be provided with crude gas import 1 bottom described venturi tower 2, middle part is Venturi district 3, top is spraying layer 4; Described spraying layer 4 inside is provided with the first alkaline detergent solution 7, and spraying layer sidewall opening connects washings pipe gravity flow pipeline 7, and described washings pipe gravity flow pipeline 7 is provided with SO
2cleaning circulation pump 8 and waste liquid outlet 19 and the other end is communicated to circulation liquid pool 9; Described circulation liquid pool 9 is provided with the first alkali lye liquid-inlet pipe 20, inside is provided with oxidation unit, oxidation unit is provided with oxidation air inlet pipe 17; Air outlet, described venturi tower 2 top pipeline is connected to the inlet mouth of rotary packed bed 5, and the air outlet pipeline of rotary packed bed 5 is connected to peripheral equipment, and the rich solution outlet conduit of rotary packed bed 5 is connected to rich solution groove 10; The liquid outlet of described rich solution groove 10 is connected to the fluid inlet of jet regeneration device 12 by rich solution recycle pump 11 pipeline, described jet regeneration device 12 is provided with air from suction inlet 18, the mixed solution after the air reaction of rich solution and self-priming is delivered in regeneration tank 13 through the liquid outlet of jet regeneration device 12; Described regeneration tank 13 top is provided with regulator of level and sulphur foam outlet 16, and the liquid outlet pipeline of regulator of level is connected to lean solution and H
2s rinse bath 14, described lean solution and H
2the liquid outlet of S rinse bath 14 is by lean solution and H
2s washing pump 15 pipeline is connected to the fluid inlet of rotary packed bed 5, and described lean solution and H
2s rinse bath 14 is provided with the second alkali lye liquid-inlet pipe 21; Described sulphur foam outlet 16 is connected to desulfuration foam treatment system.
Wherein: the venturi tower of this device is different from a conventional venturi tower, its reactive behavior Venturi district is that the pipe arranged in parallel leaving space by a series of centre combines, define upper and lower space comparatively large, middle narrower Venturi phenomenon, thus produce Venturi effect.Upper strata is sprayed by nozzle simultaneously, forms range of atomization, improves reaction effect further.In this equipment, at strong acidic environment SO
2under atmosphere, CO
2and H
2s gas does not participate in reaction substantially, achieves optionally acceptance condition.
The rotary packed bed powerful centrifugal force (or hypergravity) utilizing the bed of packings of high speed rotating to produce makes the flow velocity of gas-liquid and the effective ratio area of filler greatly improve, liquid more contacts with great speed of relative movement with gas under news rapidly at high dispersive, high mixing, strong turbulence and interface in curved channel, greatly strengthening transfer process, is embodied in:
Gas tangentially enters rotor exocoel through gas feed, under the effect of gaseous tension, enter filler by rotor periphery.Liquid introduces rotor internal cavity by liquid inlet tube, through shower nozzle sprinkle on rotor inner edge.The liquid entering rotor is subject to the effect of filler in rotor, and circumferential speed increases, and the centrifugal force produced pushes it against rotor periphery.In the process, the filled dispersion of liquid, crushing-type become greatly, the surface-area of continuous renewal, and tortuous runner exacerbates the renewal of fluid surface.Liquid more contacts so that great speed of relative movement is reverse in bending duct with gas under news rapidly at high dispersive, high turbulence, strong mixing and interface, greatly enhances mass transfer process.Like this, define fabulous mass transfer and reaction conditions at internal rotor, liquid is thrown after shell collects by rotor and is left overweight machine through liquid outlet tube.Gas leaves rotor from rotor center, is drawn by gas outlet tube, completes mass transfer and reaction process.
The rotary packed bed reaction times is extremely short, just can react, therefore to CO less than in the time of 1s
2and H
2the mixed gas of S, can selective absorbing H preferably
2s, is just in time applicable to semicoke etc. and contains CO simultaneously
2and H
2the special gas of S.
Jet regeneration device is a Venturi spray tube, sulfur removing pregnant solution produces negative pressure after being pumped into jet regeneration device after its trunnion, air self-suction, with the air of self-priming in trunnion portion, convergent divergent channel portion intense mixing reacts, a series of jet regeneration device constitutes the regeneration system rapidly of sulfur removing pregnant solution jointly, achieves the oxidation regeneration of sulfur removing pregnant solution.
Technical process: a kind of coal gas desulfurization method, concrete steps are as follows:
(1) crude gas enters bottom venturi tower by crude gas import, and the first alkaline detergent solution upwards sprayed with spraying layer after Venturi district accelerates reacts, and removes the SO in gas after reaction
2, generate sulphite, the washings with sulphite flows automatically to circulation liquid pool by washings pipe gravity flow pipeline, then by SO
2cleaning circulation pump pressurization is sent to venturi tower circulated sprinkling;
(2) in circulation liquid pool, oxidation unit is set, oxidation air enters oxidation unit by oxidation air inlet pipe, be vitriol by sulfite oxidation, when the sulfate concentration in circulation liquid pool reaches set(ting)value, discharged by waste liquid outlet, in circulation liquid pool, add the first alkaline detergent solution by the first alkali lye liquid-inlet pipe simultaneously;
(3) SO is removed through venturi tower washing
2coal gas by air outlet, top be delivered to rotary packed bed in, rotate through rotary packed bed the hypergravity reaction zone and lean solution and H that produce
2the second alkaline detergent solution reaction that S washing pump is delivered to, the H in washing absorption coal gas
2s, the coal gas after purification is delivered to peripheral equipment by rotary packed bed air outlet;
(4) by rotary packed bed absorption H
2rich solution after S flows automatically to rich solution groove, then sends into jet regeneration device by rich solution recycle pump, H
2s reacts rich solution through the reacted rich solution of jet regeneration device mixing air self-suction further reaction regeneration in regeneration tank, and the lean solution after regeneration flows automatically to lean solution and H through regeneration tank top regulator of level
2s rinse bath, by lean solution and H
2s washing pump sends into rotary packed bed circulation cleaning;
(5) the sulphur foam that sulfur removing pregnant solution regenerative response produces is delivered to sulphur foam treatment system by the sulphur foam outlet at regeneration tank top, produces raw sulphur or sulphur;
(6) along with the carrying out of reaction, the alkali concn in system constantly reduces, by the second alkali lye liquid-inlet pipe to lean solution and H
2the second alkaline detergent solution is added in S rinse bath.
Wherein: the coal gas in step (3) after purification is delivered to peripheral equipment, if CO need be removed further to the coal gas after purification
2, the method that absorption can be adopted to resolve is removed.Described first alkaline detergent solution is Na
2cO
3, MgO, Ca (OH)
2, CaCO
3or NH
3h
2o.Described second alkaline detergent solution is Na
2cO
3or NH
3h
2o.
It should be pointed out that for those skilled in the art, under the premise without departing from the principles of the invention, can also make some improvements and modifications, these improvements and modifications also should be considered as protection scope of the present invention.The all available prior art of each integral part not clear and definite in the present embodiment is realized.
Claims (7)
1. a gas desulfurizer, is characterized in that: comprise venturi tower (2), circulation liquid pool (9), rotary packed bed (5), rich solution groove (10), jet regeneration device (12), regeneration tank (13), lean solution and H
2s rinse bath (14);
Described venturi tower (2) bottom is provided with crude gas import (1), middle part is Venturi district (3), top is spraying layer (4); Described spraying layer (4) inside is provided with the first alkaline detergent solution (7), and spraying layer sidewall opening connects washings pipe gravity flow pipeline (7), and described washings pipe gravity flow pipeline (7) is provided with SO
2cleaning circulation pump (8) and waste liquid outlet (19) and the other end is communicated to circulation liquid pool (9);
Described circulation liquid pool (9) is provided with the first alkali lye liquid-inlet pipe (20), inside is provided with oxidation unit, oxidation unit is provided with oxidation air inlet pipe (17);
Described venturi tower (2) air outlet, top pipeline is connected to the inlet mouth of rotary packed bed (5), the air outlet pipeline of rotary packed bed (5) is connected to peripheral equipment, and the rich solution outlet conduit of rotary packed bed (5) is connected to rich solution groove (10);
The liquid outlet of described rich solution groove (10) is connected to the fluid inlet of jet regeneration device (12) by rich solution recycle pump (11) pipeline, described jet regeneration device (12) is provided with air from suction inlet (18), the mixed solution after the air reaction of rich solution and self-priming is delivered in regeneration tank (13) through the liquid outlet of jet regeneration device (12);
Described regeneration tank (13) top is provided with regulator of level and sulphur foam outlet (16), and the liquid outlet pipeline of regulator of level is connected to lean solution and H
2s rinse bath (14), described lean solution and H
2the liquid outlet of S rinse bath (14) is by lean solution and H
2s washing pump (15) pipeline is connected to the fluid inlet of rotary packed bed (5), and described lean solution and H
2s rinse bath (14) is provided with the second alkali lye liquid-inlet pipe (21);
Described sulphur foam outlet (16) is connected to desulfuration foam treatment system.
2. a kind of gas desulfurizer according to claim 1, is characterized in that: described Venturi district (3) comprises the Venturi-type pipe that space is left in several centres side by side.
3. a kind of gas desulfurizer according to claim 1, is characterized in that: described jet regeneration device (12) is Venturi spray tube.
4. a coal gas desulfurization method, is characterized in that: concrete steps are as follows:
(1) crude gas enters bottom venturi tower by crude gas import, and the first alkaline detergent solution upwards sprayed with spraying layer after Venturi district accelerates reacts, and removes the SO in gas after reaction
2, generate sulphite, the washings with sulphite flows automatically to circulation liquid pool by washings pipe gravity flow pipeline, then by SO
2cleaning circulation pump pressurization is sent to venturi tower circulated sprinkling;
(2) in circulation liquid pool, oxidation unit is set, oxidation air enters oxidation unit by oxidation air inlet pipe, be vitriol by sulfite oxidation, when the sulfate concentration in circulation liquid pool reaches set(ting)value, discharged by waste liquid outlet, in circulation liquid pool, add the first alkaline detergent solution by the first alkali lye liquid-inlet pipe simultaneously;
(3) SO is removed through venturi tower washing
2coal gas by air outlet, top be delivered to rotary packed bed in, rotate through rotary packed bed the hypergravity reaction zone and lean solution and H that produce
2the second alkaline detergent solution reaction that S washing pump is delivered to, the H in washing absorption coal gas
2s, the coal gas after purification is delivered to peripheral equipment by rotary packed bed air outlet;
(4) by rotary packed bed absorption H
2rich solution after S flows automatically to rich solution groove, then sends into jet regeneration device by rich solution recycle pump, H
2s reacts rich solution through the reacted rich solution of jet regeneration device mixing air self-suction further reaction regeneration in regeneration tank, and the lean solution after regeneration flows automatically to lean solution and H through regeneration tank top regulator of level
2s rinse bath, by lean solution and H
2s washing pump sends into rotary packed bed circulation cleaning;
(5) the sulphur foam that sulfur removing pregnant solution regenerative response produces is delivered to sulphur foam treatment system by the sulphur foam outlet at regeneration tank top, produces raw sulphur or sulphur;
(6) along with the carrying out of reaction, the alkali concn in system constantly reduces, by the second alkali lye liquid-inlet pipe to lean solution and H
2the second alkaline detergent solution is added in S rinse bath.
5. a kind of coal gas desulfurization method according to claim 4, is characterized in that: the coal gas in step (3) after purification is delivered to peripheral equipment, if need remove CO further to the coal gas after purification
2, the method that absorption can be adopted to resolve is removed.
6. a kind of coal gas desulfurization method according to claim 4, is characterized in that: described first alkaline detergent solution is Na
2cO
3, MgO, Ca (OH)
2, CaCO
3or NH
3h
2o.
7. a kind of coal gas desulfurization method according to claim 4, is characterized in that: described second alkaline detergent solution is Na
2cO
3or NH
3h
2o.
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