CN110585919A - High-precision desulfurization method by flue gas adsorption catalytic reaction - Google Patents
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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
- B01D53/501—Sulfur oxides by treating the gases with a solution or a suspension of an alkali or earth-alkali or ammonium compound
- B01D53/502—Sulfur oxides by treating the gases with a solution or a suspension of an alkali or earth-alkali or ammonium compound characterised by a specific solution or suspension
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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
- B01D53/501—Sulfur oxides by treating the gases with a solution or a suspension of an alkali or earth-alkali or ammonium compound
- B01D53/504—Sulfur oxides by treating the gases with a solution or a suspension of an alkali or earth-alkali or ammonium compound characterised by a specific device
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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
- B01D53/96—Regeneration, reactivation or recycling of reactants
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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
Abstract
The invention discloses a high-precision desulfurization method for flue gas adsorption catalytic reaction, which comprises the following steps: A. flue gas pretreatment cooling; B. after the temperature is reduced, the flue gas flows through an adsorption catalyst solid bed layer arranged in a desulfurizing tower; then introducing alkali liquor into the desulfurizing tower, and enabling the alkali liquor to flow through the adsorption catalyst solid bed layer to react with gas molecules adsorbed in the adsorption catalyst solid bed layer; C. carrying out solid-liquid separation on the desulfurization solution to obtain clear solution and a solid phase; D. returning a part of the clear liquid to a desulfurizing tower to flush the adsorption catalyst solid bed layer so as to regenerate the adsorption catalyst solid bed layer; adding alkali to the other part of clear liquid, adjusting pH, and feeding into a desulfurizing tower for recycling as alkali liquor; E. and gas-liquid separation is carried out to remove the liquid phase in the desulfurized flue gas, so as to obtain the exhaust gas. The invention has the advantages that: realizes the deep desulfurization of sulfur dioxide gas in flue gas and simplifies the production process.
Description
Technical Field
The invention relates to an industrial tail gas treatment method, in particular to a flue gas desulfurization method.
Background
The emission index of sulfur dioxide is improved along with the environmental protection requirement, and sulfur dioxide, sulfur trioxide and fluorine-chlorine gas (HF, HCl and Cl) are removed from the flue gas2Etc.) are difficult to reach the emission index, the emission can be reachedThe technical operation cost and investment of the indexes are high. The prior art is basically a chemical method for removing sulfur dioxide (double alkali method) because of the characteristics of large flow rate of flue gas, low pressure, complex components, corrosiveness and the like.
In the specific operation process, the prepared alkali liquor is generally fed into a desulphurization device in a spraying or atomizing mode to react with gases such as sulfur dioxide, sulfur trioxide and the like to generate CaSO3、CaSO4And the corresponding solid phase substances are added to realize desulfurization. However, in this scheme, the contact time of the alkali solution with gases such as sulfur dioxide is short, and the contact area between molecules is small, so that deep desulfurization is difficult to achieve.
The other method is to use absorbent such as active carbon, coal desulfurizer, zeolite and the like to absorb sulfur dioxide and the like for desulfurization, and the principle is to use the absorption effect of the absorbent on gases such as sulfur dioxide and the like to absorb sulfur dioxide and the like, so as to prevent harmful gases from being discharged into the atmosphere.
The method has the defects that the adsorption capacity of the adsorbent to gases such as sulfur dioxide is limited, the adsorption capacity is gradually reduced after a period of time, the adsorbent must be frequently replaced to ensure the treatment quality, the continuous production is difficult to realize, and the process operation is very troublesome.
Disclosure of Invention
The invention provides a high-precision desulfurization method for flue gas adsorption catalytic reaction, which aims to realize deep desulfurization of sulfur dioxide gas in flue gas and simplify the production process.
The technical scheme adopted by the invention is as follows: the high-precision desulfurization method by flue gas adsorption catalytic reaction comprises the following steps:
A. carrying out pretreatment cooling on the flue gas to obtain cooled flue gas;
B. introducing the cooled flue gas into a desulfurizing tower, and enabling the cooled flue gas to flow through an adsorption catalyst solid bed layer arranged in the desulfurizing tower; then introducing alkali liquor into the desulfurizing tower, and allowing the alkali liquor to flow through the adsorption catalyst solid bed layer to react with gas molecules adsorbed in the adsorption catalyst solid bed layer to obtain desulfurized flue gas and desulfurized liquid; the adsorption catalyst loaded on the adsorption catalyst solid bed layer is a sulfide adsorption catalyst;
C. carrying out solid-liquid separation on the desulfurization solution to obtain clear solution and a solid phase;
D. returning a part of the clear liquid to a desulfurizing tower to flush the adsorption catalyst solid bed layer so as to regenerate the adsorption catalyst solid bed layer; adding alkali to the other part of clear liquid, adjusting pH, and feeding into a desulfurizing tower for recycling as alkali liquor;
E. and gas-liquid separation is carried out to remove the liquid phase in the desulfurized flue gas, so as to obtain the exhaust gas.
Because the adsorption catalyst has a large number of micropores, when the flue gas passes through the solid bed layer of the adsorption catalyst, the adsorption catalyst selectively and strongly adsorbs SO2To make SO2Build up on the adsorbent; concentrated SO2Change of SO on the adsorbent2The mass transfer mode of the method is that the reaction is carried out on the surface of the micropore and alkali liquor, so that the reaction environment is changed, the acid-base reaction carried out in the original gas-liquid contact environment is changed into the acid-base reaction carried out in the micropore of the adsorption catalyst, namely, the reaction is carried out in the fixed bed layer, so that the mass transfer channel is optimized, and the environment of the acid-base molecule contact depth is achieved; because the specific surface area of the adsorption catalyst is increased in a geometric series manner relative to the original area of direct contact between gas and liquid, SO in the flue gas can be converted2Almost all the alkali liquor and the acid gas can be solidified in the adsorption catalyst, the alkali liquor and the acid gas are subjected to simple acid-base reaction in the micropores, the equilibrium partial pressure is extremely high, and the reaction is extremely thorough, so that the technical problem of incomplete gas-liquid contact reaction in the prior art is solved, and the qualified rate of the desulfurized flue gas is remarkably improved. Meanwhile, the adsorbent catalyst also has a catalytic function, so that the acid-base reaction speed is increased, and the reaction efficiency is improved.
As will be readily understood by those skilled in the art in view of the foregoing description of the principles, the term "sulfide adsorption catalyst" as used herein refers to a solid that has an adsorptive effect on at least the sulfide, i.e., sulfur dioxide, in the flue gas, and more preferably is capable of catalyzing SO2Reaction with alkali liquor.
The present invention preferably uses a pseudoboehmite adsorption catalyst which is an aluminum oxy compound having a water content greater than boehmite and a grain size smaller than boehmite. Pseudo-thin water aluminiumThe sol has good bonding property, and can generate gamma-A1 containing abundant pore structures by heat treatment2O3To SO in flue gas2Has good adsorption effect.
Preferably, the pseudo-boehmite adsorption catalyst is prepared by loading CuO, LiO and RuO by dip-dyeing after the pseudo-boehmite is used as a framework and the aluminum-magnesium silicate is used as an auxiliary material for roasting2And then the product is obtained. The adsorption catalyst provided by the invention can selectively and strongly adsorb SO in flue gas2、SO3HCl, HF and the like, and can play a catalytic role in acidolysis reaction. Has obvious promoting effect on deep desulfurization and defluorination of chlorine.
On the other hand, clear liquid obtained after the solid-liquid separation of the desulfurization solution obtained by the reaction returns to the desulfurization tower to wash the adsorption catalyst solid bed layer, so that the adsorption catalyst solid bed layer can be regenerated.
As a further improvement of the invention, the specific method for pre-treating and cooling the flue gas in the step A comprises the following steps: and (4) carrying out spray washing and cooling on the flue gas by using alkaline spray washing water. The purpose of pre-treatment cooling is to reduce the temperature of the high-temperature flue gas to 30-70 ℃ of the process temperature required by desulfurization, so that a person skilled in the art can select various cooling methods to achieve the purpose, and preferably adopts the cooling method of the scheme, because the flue gas is cooled by adopting alkaline water to spray and wash the flue gas into direct contact, the heat efficiency is high, and the energy consumption is low; and a preliminary desulfurization process can be realized by adopting alkaline water spray washing; and because the dissolution ratio of water to fluorine and chlorine is 1:500, the alkaline water can also react with gases such as HF, HCl and the like in the flue gas, and the effect of removing fluorine and chlorine with high precision can be achieved; the smoke dust in the flue gas is also remained in the slurry after being sprayed, and most of the smoke dust is precipitated through the slurry circulating system. The alkali water after heat exchange can be recycled after being cooled by cooling equipment. In the scheme, the pH value of the alkaline spray washing water is preferably controlled to be 6-9, and the temperature is preferably controlled to be 25-70 ℃.
As a further improvement of the invention, the solid-liquid separation method in the step A specifically comprises the following steps: and (4) carrying out flocculation sedimentation and filter pressing on the separated liquid in sequence, thereby realizing solid-liquid separation. The flocculant can be selected from PAC, Polyacrylamide (PAM) and the like.
As a further improvement of the invention, the alkali liquor is calcium hydroxide solution, Ca (OH) of the calcium hydroxide solution2The mass concentration is preferably controlled to be 0.005-15%. Preferably, the solid phase obtained in step C is subjected to landfill treatment. The reaction products of the calcium hydroxide solution and sulfur dioxide and sulfur trioxide in the flue gas are calcium sulfite and calcium sulfate which are harmless neutral salts and can be directly subjected to landfill treatment, and the scheme can avoid the problem of harmful solid waste discharge.
As a further improvement of the method, the desulfurization pressure in the step B is-3 to 30 kPa.
As a further improvement of the present invention, the gas-liquid separation method in step E specifically comprises: introducing the desulfurized flue gas into a gas-liquid separator for condensation and separation to obtain a liquid phase; preferably, the gas-liquid separator is provided with a dust collecting device for collecting dust in the gas phase. Although smoke dust in the flue gas after the alkali liquor spraying treatment can be remained in the slurry, most of the smoke dust is precipitated through the slurry circulating system, the existence of extremely small escaping dust is still difficult to avoid. A dust trapping device for trapping dust in the gas phase may be provided in the gas-liquid separator for further trapping. The dust catching device can adopt a filiform filter screen.
The invention has the beneficial effects that: 1) the technical problem of incomplete gas-liquid contact reaction in the prior art is solved, and the qualification rate of the desulfurized flue gas is obviously improved; meanwhile, the adsorbent catalyst also has a catalytic function, so that the acid-base reaction speed is increased, and the reaction efficiency is improved. Experiments show that the sulfur dioxide content of the desulfurized gas can be reduced to 0-35 mg/Nm3。
2) The adsorption catalyst has good adsorption and catalytic reaction functions on sulfur dioxide and calcium hydroxide, so that the problem of sulfur dioxide concentration in large-flow flue gas at normal pressure is solved, and the adsorption catalyst can react with alkali to play a strong catalytic role. For reasons as followsThe flow rate of the flue gas can be 10-10000000 Nm3Is carried out within a/h period.
3) The adsorption catalyst has good adsorption catalytic reaction function on sulfur dioxide and calcium hydroxide, so that when the adsorption catalyst is fed back to engineering treatment flue gas or other tail gas containing sulfur dioxide, the concentration of the sulfur dioxide can be treated to be 50-10000 mg/Nm3Of the flue gas of (2).
4) The adsorption catalyst has strong anti-interference performance and high use stability, can treat the flue gas of a kiln, and can adapt to the flue gas formed by fire coal; and is also suitable for treating tail gas containing sulfur dioxide in the industries of metallurgy, chemical industry, electric power and the like.
5) The clear liquid obtained after the solid-liquid separation of the desulfurization liquid obtained by the reaction returns to the desulfurization tower to wash the solid bed layer of the adsorption catalyst, so that the solid bed layer of the adsorption catalyst can be regenerated.
Drawings
FIG. 1 is a flow chart of the apparatus of the present invention.
Labeled as: 1-a desulfurizing tower, 101-an atomizing nozzle, 102-a washing spray head, 103-an adsorption catalyst solid bed layer, 2-a gas-liquid separator, 201-a dust collecting device, 3-an induced draft fan, 4-a purifying tank, 5-a spray washing pump, 6-a liquid preparation tank, 7-an alkali liquor pump and 8-a circulating cooling pump.
Detailed Description
The invention is further illustrated with reference to the following figures and examples.
Flue gas was treated using the apparatus shown in FIG. 1, with flue gas specifications as shown in Table 1:
table 1: flue gas specification
The first embodiment is as follows:
the flue gas is treated as follows:
s1, enabling the flue gas from the flue gas main pipe to enter a flue gas pipeline under the action of a draught fan 3, wherein the flow of the flue gas is 3500m3H is used as the reference value. Meanwhile, the prepared alkaline spray water is pumped into the flue gas pipeline by the circulating cooling pump 8 to spray and cool the high-temperature flue gas, so that the flue gas is cooled, and the processes of preliminary desulfurization and dust capture are simultaneously completed. The temperature of the flue gas was measured to drop to 58 ℃ before entering the desulfurization tower.
S2, cooling the flue gas, feeding the flue gas into a desulfurizing tower, arranging an adsorption catalyst solid bed layer 103 in the desulfurizing tower, roasting the adsorption catalyst filled in the adsorption catalyst solid bed layer 103 by using pseudo-boehmite as a framework and using aluminum-magnesium silicate as an auxiliary material, and dip-dyeing the roasted adsorption catalyst to load CuO, LiO and RuO2And in the preparation process, the flue gas enters from the lower part of the tower and passes through 1-15 layers of solid bed layers, and sulfur dioxide is selectively adsorbed.
S3, preparing Ca (OH) by using lye pump 72Pumping the alkali liquor with the mass concentration of 12% to an atomizing nozzle 101, boosting the pressure of the alkali liquor to 0.8Mpa, enabling the alkali liquor to pass through the atomizing nozzle 101 up and down through a desulfurizing tower 2, and enabling calcium hydroxide in the alkali liquor to react with sulfur dioxide concentrated in an adsorbent under the action of a catalyst to generate calcium sulfite when the alkali liquor passes through an adsorption catalyst solid bed layer 103.
And S4, enabling a liquid phase generated by the reaction to be a desulfurization solution, enabling the desulfurization solution to enter a purification tank 4 from an outlet at the lower part of the desulfurization tower, generating calcium sulfite precipitate under the action of a PAC (polyaluminium chloride) flocculant, and discharging the calcium sulfite precipitate after filter pressing for landfill treatment.
And S5, feeding the clear liquid generated by filter pressing into a liquid preparation tank 6, supplementing solid calcium hydroxide and alkali, and returning the clear liquid to the desulfurizing tower 2 through an alkali liquid pump 7 for recycling.
S6, when the control system detects that the adsorption catalyst solid bed layer 103 needs to be washed and regenerated (the control mode can be set according to the adsorption time), the spray washing pump 5 is automatically started to send a part of clear liquid generated in the purification tank 4 to the washing spray head 102 for washing the adsorption catalyst solid bed layer 103.
S7, the gas phase generated by the desulfurization reaction is the desulfurized flue gas, the desulfurized flue gas enters the gas-liquid separator 2 under the action of the induced draft fan 3, and the desulfurized flue gas enters the gas-liquid separator 2The liquid phase in the flue gas after middle desulfurization is condensed and then enters the purification tank 4, and the gas phase further traps dust through the dust trapping device 201 to obtain exhaust gas. SO of exhaust gas2The concentration was measured and the results are shown in Table 2.
Example two:
the flue gas is treated as follows:
s1, enabling the flue gas from the flue gas main pipe to enter a flue gas pipeline under the action of a draught fan 3, wherein the flow of the flue gas is 8600m3H is used as the reference value. Meanwhile, the prepared alkaline spray water is pumped into the flue gas pipeline by the circulating cooling pump 8 to spray and cool the high-temperature flue gas, so that the flue gas is cooled, and the processes of preliminary desulfurization and dust capture are simultaneously completed. The temperature of the flue gas was measured to drop to 62 c before entering the desulfurization tower.
S2, cooling the flue gas, feeding the flue gas into a desulfurizing tower, arranging an adsorption catalyst solid bed layer 103 in the desulfurizing tower, roasting the adsorption catalyst filled in the adsorption catalyst solid bed layer 103 by using pseudo-boehmite as a framework and using aluminum-magnesium silicate as an auxiliary material, and dip-dyeing the roasted adsorption catalyst to load CuO, LiO and RuO2And in the preparation process, the flue gas enters from the lower part of the tower and passes through 1-15 layers of solid bed layers, and sulfur dioxide is selectively adsorbed.
S3, preparing Ca (OH) by using lye pump 72Pumping the alkali liquor with the mass concentration of 10% to an atomizing nozzle 101, boosting the pressure of the alkali liquor to 0.2Mpa, enabling the alkali liquor to pass through the atomizing nozzle 101 up and down through a desulfurizing tower 2, and enabling calcium hydroxide in the alkali liquor to react with sulfur dioxide concentrated in an adsorbent under the action of a catalyst to generate calcium sulfite when the alkali liquor passes through an adsorption catalyst solid bed layer 103.
And S4, enabling a liquid phase generated by the reaction to be a desulfurization solution, enabling the desulfurization solution to enter a purification tank 4 from an outlet at the lower part of the desulfurization tower, generating calcium sulfite precipitate under the action of a Polyacrylamide (PAM) cationic flocculant, and discharging the precipitate after filter pressing for landfill treatment.
And S5, feeding the clear liquid generated by filter pressing into a liquid preparation tank 6, supplementing solid calcium hydroxide and alkali, and returning the clear liquid to the desulfurizing tower 2 through an alkali liquid pump 7 for recycling.
S6, when the control system detects that the adsorption catalyst solid bed layer 103 needs to be washed and regenerated (the control mode can be set according to the adsorption time), the spray washing pump 5 is automatically started to send a part of clear liquid generated in the purification tank 4 to the washing spray head 102 for washing the adsorption catalyst solid bed layer 103.
S7, the gas phase generated by the desulfurization reaction is the desulfurized flue gas, the desulfurized flue gas enters the gas-liquid separator 2 under the action of the induced draft fan 3, the liquid phase in the desulfurized flue gas in the gas-liquid separator 2 is condensed and then enters the purification tank 4, and the gas phase further traps dust through the dust trapping device 201 to obtain the exhaust gas. SO of exhaust gas2The concentration was measured and the results are shown in Table 2.
Example three:
the flue gas is treated as follows:
s1, enabling flue gas from a flue gas main pipe to enter a flue gas pipeline under the action of a draught fan 3, wherein the flow of the flue gas is 11200m3H is used as the reference value. Meanwhile, the prepared alkaline spray water is pumped into the flue gas pipeline by the circulating cooling pump 8 to spray and cool the high-temperature flue gas, so that the flue gas is cooled, and the processes of preliminary desulfurization and dust capture are simultaneously completed. The temperature of the flue gas was measured to drop to 57 c before entering the desulfurization tower.
S2, cooling the flue gas, feeding the flue gas into a desulfurizing tower, arranging an adsorption catalyst solid bed layer 103 in the desulfurizing tower, roasting the adsorption catalyst filled in the adsorption catalyst solid bed layer 103 by using pseudo-boehmite as a framework and using aluminum-magnesium silicate as an auxiliary material, and dip-dyeing the roasted adsorption catalyst to load CuO, LiO and RuO2And in the preparation process, the flue gas enters from the lower part of the tower and passes through 1-15 layers of solid bed layers, and sulfur dioxide is selectively adsorbed.
S3, preparing Ca (OH) by using lye pump 72Pumping 15% alkali liquor to the atomizing nozzle 101, increasing the pressure of the alkali liquor to 0.1Mpa, passing through the atomizing nozzle 101 up and down through the desulfurizing tower 2, and reacting calcium hydroxide in the alkali liquor with sulfur dioxide concentrated in the adsorbent under the action of the catalyst to generate calcium sulfite when passing through the adsorption catalyst solid bed layer 103.
And S4, enabling a liquid phase generated by the reaction to be a desulfurization solution, enabling the desulfurization solution to enter a purification tank 4 from an outlet at the lower part of the desulfurization tower, generating calcium sulfite precipitate under the action of a PAM flocculating agent, and discharging the precipitate after filter pressing for landfill treatment.
And S5, feeding the clear liquid generated by filter pressing into a liquid preparation tank 6, supplementing solid calcium hydroxide and alkali, and returning the clear liquid to the desulfurizing tower 2 through an alkali liquid pump 7 for recycling.
S6, when the control system detects that the adsorption catalyst solid bed layer 103 needs to be washed and regenerated (the control mode can be set according to the adsorption time), the spray washing pump 5 is automatically started to send a part of clear liquid generated in the purification tank 4 to the washing spray head 102 for washing the adsorption catalyst solid bed layer 103.
S7, the gas phase generated by the desulfurization reaction is the desulfurized flue gas, the desulfurized flue gas enters the gas-liquid separator 2 under the action of the induced draft fan 3, the liquid phase in the desulfurized flue gas in the gas-liquid separator 2 is condensed and then enters the purification tank 4, and the gas phase further traps dust through the dust trapping device 201 to obtain the exhaust gas. SO of exhaust gas2The concentration was measured and the results are shown in Table 2.
Comparative example one:
this comparative example is a control experiment of example three, carried out under the same experimental conditions as the three phases of example, with the only difference that: the desulfurization tower 1 is not provided with the adsorption catalyst solid bed layer 103. SO of exhaust gas obtained in this comparative example2The concentration was measured and the results are shown in Table 2.
Table 2: residual SO2Table of concentration test results
| Item | Residual SO2Concentration (mg/Nm)3) |
| Example one | 2.1 |
| Example two | 2.6 |
| EXAMPLE III | 4.2 |
| Comparative example 1 | 37.8 |
Claims (10)
1. The high-precision desulfurization method by flue gas adsorption catalytic reaction comprises the following steps:
A. carrying out pretreatment cooling on the flue gas to obtain cooled flue gas;
B. introducing the cooled flue gas into a desulfurizing tower, and enabling the cooled flue gas to flow through an adsorption catalyst solid bed layer arranged in the desulfurizing tower; then introducing alkali liquor into the desulfurizing tower, and allowing the alkali liquor to flow through the adsorption catalyst solid bed layer to react with gas molecules adsorbed in the adsorption catalyst solid bed layer to obtain desulfurized flue gas and desulfurized liquid; the adsorption catalyst loaded on the adsorption catalyst solid bed layer is a sulfide adsorption catalyst.
C. Carrying out solid-liquid separation on the desulfurization solution to obtain clear solution and a solid phase;
D. returning a part of the clear liquid to a desulfurizing tower to flush the adsorption catalyst solid bed layer so as to regenerate the adsorption catalyst solid bed layer; adding alkali to the other part of clear liquid, adjusting pH, and feeding into a desulfurizing tower for recycling as alkali liquor;
E. and gas-liquid separation is carried out to remove the liquid phase in the desulfurized flue gas, so as to obtain the exhaust gas.
2. The flue gas adsorption catalytic reaction high-precision desulfurization method according to claim 1, characterized in that: the sulfide adsorption catalyst is a pseudo-boehmite adsorption catalyst.
3. The flue gas adsorption catalytic reaction high-precision desulfurization method according to claim 2, characterized in that: the pseudo-boehmite adsorption catalyst is pseudo-boehmiteRoasting stone as skeleton and magnesia-alumina silicate as supplementary material, and dip dyeing to load CuO, LiO and RuO2And then the product is obtained.
4. The flue gas adsorption catalytic reaction high-precision desulfurization method according to claim 1, characterized in that: the specific method for carrying out pretreatment cooling on the flue gas in the step A comprises the following steps: and (4) carrying out spray washing and cooling on the flue gas by using alkaline spray washing water.
5. The flue gas adsorption catalytic reaction high-precision desulfurization method according to claim 1, characterized in that: the solid-liquid separation method in the step C comprises the following specific steps: and (4) carrying out flocculation sedimentation and filter pressing on the separated liquid in sequence, thereby realizing solid-liquid separation.
6. The flue gas adsorption catalytic reaction high-precision desulfurization method according to claim 1, characterized in that: the alkali liquor is calcium hydroxide solution.
7. The flue gas adsorption catalytic reaction high-precision desulfurization method according to claim 6, characterized in that: and D, performing landfill treatment on the solid phase obtained in the step C.
8. The flue gas adsorption catalytic reaction high-precision desulfurization method according to claim 1, characterized in that: and the desulfurization pressure in the step B is-3-30 kPa.
9. The flue gas adsorption catalytic reaction high-precision desulfurization method according to any one of claims 1 to 8, characterized in that: the gas-liquid separation method in the step E comprises the following specific steps: and introducing the desulfurized flue gas into a gas-liquid separator for condensation and separation to obtain a liquid phase.
10. The flue gas adsorption catalytic reaction high-precision desulfurization method according to claim 9, characterized in that: and the gas-liquid separator is internally provided with a dust collecting device for collecting dust in a gas phase.
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Cited By (4)
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| CN112195043A (en) * | 2020-09-28 | 2021-01-08 | 武汉钢铁有限公司 | Blast furnace gas desulfurization method and device |
| CN112657331A (en) * | 2020-12-31 | 2021-04-16 | 成都达奇环境科技有限公司 | Flue gas desulfurization method and flue gas desulfurization equipment |
| CN113262633A (en) * | 2021-05-31 | 2021-08-17 | 重庆市渝琥玻璃有限公司 | Flue gas desulfurization process |
| CN115634558A (en) * | 2021-12-31 | 2023-01-24 | 山东庚辰环保新材料有限公司 | Desulfurization device, process and application |
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| CN115634558A (en) * | 2021-12-31 | 2023-01-24 | 山东庚辰环保新材料有限公司 | Desulfurization device, process and application |
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