CN104946315A - Method for purifying coke oven gas and recycling desulfurated liquid waste by virtue of vacuum potassium carbonate method - Google Patents
Method for purifying coke oven gas and recycling desulfurated liquid waste by virtue of vacuum potassium carbonate method Download PDFInfo
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- CN104946315A CN104946315A CN201410125208.6A CN201410125208A CN104946315A CN 104946315 A CN104946315 A CN 104946315A CN 201410125208 A CN201410125208 A CN 201410125208A CN 104946315 A CN104946315 A CN 104946315A
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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
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01C—AMMONIA; CYANOGEN; COMPOUNDS THEREOF
- C01C3/00—Cyanogen; Compounds thereof
- C01C3/08—Simple or complex cyanides of metals
- C01C3/12—Simple or complex iron cyanides
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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
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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
- C10K1/002—Removal of contaminants
- C10K1/003—Removal of contaminants of acid contaminants, e.g. acid gas removal
- C10K1/006—Hydrogen cyanide
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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
- C10K1/04—Purifying combustible gases containing carbon monoxide by cooling to condense non-gaseous materials
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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
- C10K1/085—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors two direct washing treatments, one with an aqueous liquid and one with a non-aqueous liquid
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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
- C10K1/101—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors with aqueous liquids with water only
-
- 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
- C10K1/105—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors with aqueous liquids containing metal compounds other than alkali- or earth-alkali carbonates, -hydroxides, oxides, or salts of inorganic acids derived from sulfur
-
- 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
-
- 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
- C10K1/16—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors with non-aqueous liquids
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Abstract
The invention relates to a method for purifying coke oven gas by removing sulfur by virtue of a vacuum carbonate method. According to the method, purified coke oven gas enters a desulfuration and decyanation system and is subjected to desulfuration and decyanation processes by virtue of the vacuum carbonate method; liquid waste which is subjected to desulfuration and decyanation is recycled, so that the phenomena of deterioration of water quality and wasting of resources are effectively improved.
Description
Technical field
The present invention relates to a kind of purifying method of coke-oven gas, particularly a kind of purifying method of coke-oven gas of matched with vacuum carbonate desulphurization.
Background technology
Coke-oven gas, as the byproduct of coking, because calorific value is higher, is widely used in metallurgy industry power generation project.Vacuum potassium carbonate desulfurization is a kind of wet type desulfurizing technique, and because its desulfuration efficiency is high, coke-oven plant is used widely at home.This technique uses solution of potassium carbonate directly to absorb the sour gas such as H2S and HCN in coke-oven gas, then carries out secondary washing by NaOH solution to coal gas, reaches requirement to make H2S content in coal gas.Coal gas desulfurization tower is divided into two sections, bottom salt of wormwood absorber portion and top sodium hydroxide alkali cleaning section.Coal gas first flows through absorber portion and salt of wormwood lean solution counter current contact from bottom to top, and the sour gas such as H2S, HCN, CO2 of more than 90% in coal gas are absorbed, and salt of wormwood lean solution changes into the salt of wormwood rich solution absorbing a large amount of H2S thereupon; The diluted sodium hydroxide of top sodium hydroxide alkali cleaning section optionally absorbs in coal gas sour gas such as remaining small portion H2S, to make after desulfurization H2S≤200mg/m3 in coal gas.The rich solution absorbing sour gas enters regenerator column to carry out parsing and obtains salt of wormwood lean solution, then returns salt of wormwood absorber portion and recycle.Carry out in the process of coke-oven-gas desulfurization and decyanation in employing vacuum carbonation, the waste liquid containing high density prussiate and sulfide can be produced.The main component of this desulfurization waste lye is sodium carbonate (or potassium), sodium cyanide (or potassium) and sodium sulphite (or potassium), and also containing organism such as a small amount of tar, phenol, color is sorrel, and its pH value is about 10.
Conventional processing is that desulfurization waste lye is delivered to biochemical water treatment system, and desulfurization waste lye causes extreme shock to biochemical water treatment system, causes biochemical system microorganism active greatly to reduce, causes the deterioration of effluent quality, cause the wasting of resources simultaneously.
Summary of the invention
The object of this invention is to provide a kind of purifying method of coke-oven gas of matched with vacuum carbonate desulphurization, to solve the technical problem of water quality deterioration that in prior art, desulfurization waste lye causes, the wasting of resources.
In order to solve the problem, the invention provides a kind of purification and vacuum potassium carbonate method desulfurization waste liquor method of resource of coke-oven gas, comprising the following steps:
1), the raw gas without purification is passed into primary cooler ammoniacal liquor and carry out sprinkling cooling;
2), pass into from primary cooler coke-oven gas out the removing that electrical tar precipitator carries out tar fog;
3), pass into gas blower from electrical tar precipitator coke-oven gas out to heat up;
4), pass into pickling tower from gas blower coke-oven gas out and carry out deamination;
5), pass into final cooling tower from pickling tower coke-oven gas out to carry out lowering the temperature;
6), pass into from final cooling tower coke-oven gas out and wash naphthalene tower absorption agent and carry out de-naphthalene;
7), from washing naphthalene tower coke-oven gas out send into and wash benzene tower lower end, washing oil sprays and benzene class material in lower absorption coke-oven gas by washing benzene top of tower, washes the coke-oven gas that benzene tower upper end is purified, washes benzene tower bottom and obtain rich oil;
8), from wash benzene top of tower out coke-oven gas pass into water wash column washings spray remove washing oil, tar, naphthalene further;
9) coke-oven gas, after above-mentioned steps purification enters desulfuration and decyanation system, carries out vacuum carbonate desulphurization decyanation technology;
10), resource utilization recovery is carried out to desulfuration and decyanation waste liquid.
As a preferred embodiment of the present invention, the method that desulfuration and decyanation waste liquid described in step 10) carries out resource utilization recovery is: in desulfuration and decyanation waste liquid, add soluble ferrite precipitate prussiate in waste liquid and sulfide simultaneously, throw out at high temperature reacts with dense sodium hydroxide or potassium hydroxide alkali lye and generates yellow prussiate of potash after centrifugation goes out under 100 ~ 140 DEG C of conditions, yellow prussiate of potash mother liquor is crystallisation by cooling at 10 ~ 20 DEG C, crystallisate obtains yellow prussiate of potash product through centrifugation, alkali lye reusable edible; Remove the waste liquid after most of prussiate and sulfide and can directly enter coking chemical waste water conventional processing systems after pH regulator and coagulating sedimentation.Soluble ferrite described above is ferrous sulfate, iron protochloride.Waste liquid is the waste liquid of sulfur compound and the prussiate produced in vacuum potassium carbonate method coke-oven-gas desulfurization and decyanation process.
The yellow prussiate of potash mother liquor of heat enters crystallizer tank, and at 5 ~ 25 DEG C after cooling, yellow prussiate of potash crystallization, crystallized product obtains yellow prussiate of potash product by centrifugation.Stirred autoclave recycle can be got back to the residue alkali lye of centrifugal generation after crystallization, add fresh alkali lye to meet the requirement of products production simultaneously.
As another kind of preferred version of the present invention, the method that the desulfuration and decyanation waste liquid described in step 10) carries out resource utilization recovery is: first make desulfuration and decyanation waste liquid and phosphatase reaction, produces gas phase and liquid phase; , there is catalytic oxidation after reacted mixed gas burning, after absorbing with sulphuric acid soln, obtain sulfuric acid product in described gas phase generation prussic acid cartalytic decomposition effect; Described liquid phase after oxidation adsorption-edulcoration, filter after, in filtrate, add phosphoric acid or carbonate reacts, evaporation concentration obtains phosphate product.
Described gas phase is through ferrum-cobalt catalyst generation prussic acid cartalytic decomposition effect; Preferably, after the burning of reacted mixed gas through vanadium catalyst generation catalytic oxidation.
As another kind of preferred version of the present invention, send in the middle part of debenzolizing tower in step 7) after the rich oil obtained heats, absorb the benzene class material in rich oil after pure nitrogen heating bottom feeding debenzolizing tower, debenzolizing tower upper end obtains mixed gas, obtains oil-poor bottom debenzolizing tower; The rich oil temperature entering debenzolizing tower is 150 ~ 180 DEG C, and the nitrogen temperature passed into bottom debenzolizing tower is 220 ~ 500 DEG C; Benzene class substances content in the nitrogen amount that debenzolizing tower passes into and rich oil is calculated in molar ratio as 10:l.
As another kind of preferred version of the present invention, described step 8) in, the step 7 of described feeding water wash column) after the tar content of coke-oven gas control at≤0.15g/m3, naphthalene content controls at≤0.10g/m3, and washing oil content controls at≤2.5g/m3.
As another kind of preferred version of the present invention, the desulfurization and decyanation technology described in step 9) mainly comprises the steps:
1) adopt salt of wormwood lean solution to contact with coke-oven gas air-flow is reverse at thionizer hypomere as sweetening agent, salt of wormwood lean solution generates sulfur removing pregnant solution after absorbing the sour gas in coke-oven gas;
2) sulfur removing pregnant solution produced in step 1) is sent into regenerator column regeneration, sour gas is desorbed from rich solution, obtain the salt of wormwood lean solution regenerated;
3) KOH solution is added by step 2) fully mix in the salt of wormwood lean solution that obtains, then this mixed solution is delivered to thionizer hypomere, contact with coke-oven gas air-flow is reverse, cyclically utilizing;
4) adopt NaOH solution or from the mixed solution that step 3) obtains, distribute a part of mixed solution as washing composition, at thionizer epimere, secondary washing being carried out to coke-oven gas with this washing composition.
The beneficial effect that the present invention brings is: reclaimed by the optimization to desulfurization and decyanation technology and the resource utilization to desulfurization waste lye, effectively improve the phenomenon of water quality deterioration, the wasting of resources.
Embodiment
A kind of purification and vacuum potassium carbonate method desulfurization waste liquor method of resource of preferred coke-oven gas are provided in the present embodiment, mainly comprise the steps and processing condition:
1), the raw gas without purification is passed into primary cooler ammoniacal liquor and carry out sprinkling cooling;
2), pass into from primary cooler coke-oven gas out the removing that electrical tar precipitator carries out tar fog;
3), pass into gas blower from electrical tar precipitator coke-oven gas out to heat up;
4), pass into pickling tower from gas blower coke-oven gas out and carry out deamination;
5), pass into final cooling tower from pickling tower coke-oven gas out to carry out lowering the temperature;
6), pass into from final cooling tower coke-oven gas out and wash naphthalene tower absorption agent and carry out de-naphthalene;
7), from washing naphthalene tower coke-oven gas out send into and wash benzene tower lower end, washing oil sprays and benzene class material in lower absorption coke-oven gas by washing benzene top of tower, washes the coke-oven gas that benzene tower upper end is purified, washes benzene tower bottom and obtain rich oil;
8), from wash benzene top of tower out coke-oven gas pass into water wash column washings spray remove washing oil, tar, naphthalene further; Tar content controls at≤0.15g/m3, and naphthalene content controls at≤0.10g/m3, and washing oil content controls at≤2.5g/m3;
9) coke-oven gas, after above-mentioned steps purification enters desulfuration and decyanation system, carries out vacuum carbonate desulphurization decyanation technology;
10), resource utilization recovery is carried out to desulfuration and decyanation waste liquid.
Send into after the rich oil obtained in step 7) heats in the middle part of debenzolizing tower, absorb the benzene class material in rich oil after pure nitrogen heating bottom feeding debenzolizing tower, debenzolizing tower upper end obtains mixed gas, obtains oil-poor bottom debenzolizing tower; The rich oil temperature entering debenzolizing tower is 150 ~ 180 DEG C, and the nitrogen temperature passed into bottom debenzolizing tower is 220 ~ 500 DEG C; Benzene class substances content in the nitrogen amount that debenzolizing tower passes into and rich oil is calculated in molar ratio as 10:l.
Desulfurization and decyanation technology described in step 9) mainly comprises the steps:
1) adopt salt of wormwood lean solution to contact with coke-oven gas air-flow is reverse at thionizer hypomere as sweetening agent, salt of wormwood lean solution generates sulfur removing pregnant solution after absorbing the sour gas in coke-oven gas;
2) sulfur removing pregnant solution produced in step 1) is sent into regenerator column regeneration, sour gas is desorbed from rich solution, obtain the salt of wormwood lean solution regenerated;
3) KOH solution is added by step 2) fully mix in the salt of wormwood lean solution that obtains, then this mixed solution is delivered to thionizer hypomere, contact with coke-oven gas air-flow is reverse, cyclically utilizing; The mass percent concentration scope of described KOH solution is 20 ~ 40%;
4) adopt NaOH solution or from the mixed solution that step 3) obtains, distribute a part of mixed solution as washing composition, at thionizer epimere, secondary washing being carried out to coke-oven gas with this washing composition.
As a preferred embodiment of the present invention, the method that desulfuration and decyanation waste liquid described in step 10) carries out resource utilization recovery is: in desulfuration and decyanation waste liquid, add soluble ferrite precipitate prussiate in waste liquid and sulfide simultaneously, throw out at high temperature reacts with dense sodium hydroxide or potassium hydroxide alkali lye and generates yellow prussiate of potash after centrifugation goes out under 100 ~ 140 DEG C of conditions, yellow prussiate of potash mother liquor is crystallisation by cooling at 10 ~ 20 DEG C, crystallisate obtains yellow prussiate of potash product through centrifugation, alkali lye reusable edible; Remove the waste liquid after most of prussiate and sulfide and can directly enter coking chemical waste water conventional processing systems after pH regulator and coagulating sedimentation.Soluble ferrite described above is ferrous sulfate, iron protochloride.Waste liquid is the waste liquid of sulfur compound and the prussiate produced in vacuum potassium carbonate method coke-oven-gas desulfurization and decyanation process.
The yellow prussiate of potash mother liquor of heat enters crystallizer tank, and at 5 ~ 25 DEG C after cooling, yellow prussiate of potash crystallization, crystallized product obtains yellow prussiate of potash product by centrifugation.Stirred autoclave recycle can be got back to the residue alkali lye of centrifugal generation after crystallization, add fresh alkali lye to meet the requirement of products production simultaneously.
As another kind of preferred version of the present invention, the method that the desulfuration and decyanation waste liquid described in step 10) carries out resource utilization recovery is: first make desulfuration and decyanation waste liquid and phosphatase reaction, produces gas phase and liquid phase; , there is catalytic oxidation after reacted mixed gas burning, after absorbing with sulphuric acid soln, obtain sulfuric acid product in described gas phase generation prussic acid cartalytic decomposition effect; Described liquid phase after oxidation adsorption-edulcoration, filter after, in filtrate, add phosphoric acid or carbonate reacts, evaporation concentration obtains phosphate product.
Described gas phase is through ferrum-cobalt catalyst generation prussic acid cartalytic decomposition effect; Preferably, after the burning of reacted mixed gas through vanadium catalyst generation catalytic oxidation.
Those of ordinary skill in the art will be appreciated that, above embodiment is only used to the present invention is described, and be not used as limitation of the invention, as long as in spirit of the present invention, all will drop in Claims scope of the present invention the change of the above embodiment, modification.
Claims (9)
1. the purification of coke-oven gas and a vacuum potassium carbonate method desulfurization waste liquor method of resource, is characterized in that, comprise the following steps:
1), the raw gas without purification is passed into primary cooler ammoniacal liquor and carry out sprinkling cooling;
2), pass into from primary cooler coke-oven gas out the removing that electrical tar precipitator carries out tar fog;
3), pass into gas blower from electrical tar precipitator coke-oven gas out to heat up;
4), pass into pickling tower from gas blower coke-oven gas out and carry out deamination;
5), pass into final cooling tower from pickling tower coke-oven gas out to carry out lowering the temperature;
6), pass into from final cooling tower coke-oven gas out and wash naphthalene tower absorption agent and carry out de-naphthalene;
7), from washing naphthalene tower coke-oven gas out send into and wash benzene tower lower end, washing oil sprays and benzene class material in lower absorption coke-oven gas by washing benzene top of tower, washes the coke-oven gas that benzene tower upper end is purified, washes benzene tower bottom and obtain rich oil;
8), from wash benzene top of tower out coke-oven gas pass into water wash column washings spray remove washing oil, tar, naphthalene further;
9) coke-oven gas, after above-mentioned steps purification enters desulfuration and decyanation system, carries out vacuum carbonate desulphurization decyanation technology;
10), resource utilization recovery is carried out to desulfuration and decyanation waste liquid.
2. the purification of coke-oven gas as claimed in claim 1 and vacuum potassium carbonate method desulfurization waste liquor method of resource, it is characterized in that, the method that desulfuration and decyanation waste liquid described in step 10) carries out resource utilization recovery is: in desulfuration and decyanation waste liquid, add soluble ferrite precipitate prussiate in waste liquid and sulfide simultaneously, throw out at high temperature reacts with dense sodium hydroxide or potassium hydroxide alkali lye and generates yellow prussiate of potash after centrifugation goes out under 100 ~ 140 DEG C of conditions, yellow prussiate of potash mother liquor is crystallisation by cooling at 10 ~ 20 DEG C, crystallisate obtains yellow prussiate of potash product through centrifugation, alkali lye reusable edible, remove the waste liquid after most of prussiate and sulfide and can directly enter coking chemical waste water conventional processing systems after pH regulator and coagulating sedimentation.
3. the purification of coke-oven gas according to claim 2 and vacuum potassium carbonate method desulfurization waste liquor method of resource, it is characterized in that, described soluble ferrite is ferrous sulfate, iron protochloride.
4. the purification of coke-oven gas as claimed in claim 2 and vacuum potassium carbonate method desulfurization waste liquor method of resource, it is characterized in that, waste liquid is the waste liquid of sulfur compound and the prussiate produced in vacuum potassium carbonate method coke-oven-gas desulfurization and decyanation process.
5. the purification of coke-oven gas as claimed in claim 1 and vacuum potassium carbonate method desulfurization waste liquor method of resource, it is characterized in that, the method that desulfuration and decyanation waste liquid described in step 10) carries out resource utilization recovery is: first make desulfuration and decyanation waste liquid and phosphatase reaction, produces gas phase and liquid phase; , there is catalytic oxidation after reacted mixed gas burning, after absorbing with sulphuric acid soln, obtain sulfuric acid product in described gas phase generation prussic acid cartalytic decomposition effect; Described liquid phase after oxidation adsorption-edulcoration, filter after, in filtrate, add phosphoric acid or carbonate reacts, evaporation concentration obtains phosphate product.
6. the purification of coke-oven gas as claimed in claim 5 and vacuum potassium carbonate method desulfurization waste liquor method of resource, it is characterized in that, described gas phase is through ferrum-cobalt catalyst generation prussic acid cartalytic decomposition effect.
7. the purification of coke-oven gas as claimed in claim 1 and vacuum potassium carbonate method desulfurization waste liquor method of resource, it is characterized in that, send in the middle part of debenzolizing tower after the rich oil heating obtained in step 7), the benzene class material in rich oil is absorbed bottom feeding debenzolizing tower after pure nitrogen heating, debenzolizing tower upper end obtains mixed gas, obtains oil-poor bottom debenzolizing tower; The rich oil temperature entering debenzolizing tower is 150 ~ 180 DEG C, and the nitrogen temperature passed into bottom debenzolizing tower is 220 ~ 500 DEG C; Benzene class substances content in the nitrogen amount that debenzolizing tower passes into and rich oil is calculated in molar ratio as 10:l.
8. the purification of coke-oven gas as claimed in claim 1 and vacuum potassium carbonate method desulfurization waste liquor method of resource, it is characterized in that, described step 8) in, the step 7 of described feeding water wash column) after the tar content of coke-oven gas control at≤0.15g/m3, naphthalene content controls at≤0.10g/m3, and washing oil content controls at≤2.5g/m3.
9. the purification of coke-oven gas as claimed in claim 1 and vacuum potassium carbonate method desulfurization waste liquor method of resource, it is characterized in that, the desulfurization and decyanation technology described in step 9) mainly comprises the steps:
1) adopt salt of wormwood lean solution to contact with coke-oven gas air-flow is reverse at thionizer hypomere as sweetening agent, salt of wormwood lean solution generates sulfur removing pregnant solution after absorbing the sour gas in coke-oven gas;
2) sulfur removing pregnant solution produced in step 1) is sent into regenerator column regeneration, sour gas is desorbed from rich solution, obtain the salt of wormwood lean solution regenerated;
3) KOH solution is added by step 2) fully mix in the salt of wormwood lean solution that obtains, then this mixed solution is delivered to thionizer hypomere, contact with coke-oven gas air-flow is reverse, cyclically utilizing;
4) adopt NaOH solution or from the mixed solution that step 3) obtains, distribute a part of mixed solution as washing composition, at thionizer epimere, secondary washing being carried out to coke-oven gas with this washing composition.
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| CN102120937A (en) * | 2010-01-07 | 2011-07-13 | 上海宝钢化工有限公司 | Purification method of coke oven gas matched with vacuum carbonate desulphurization |
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