CN109573958A - A kind of resource utilization method of flue gas during smelting - Google Patents
A kind of resource utilization method of flue gas during smelting Download PDFInfo
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- CN109573958A CN109573958A CN201811613525.7A CN201811613525A CN109573958A CN 109573958 A CN109573958 A CN 109573958A CN 201811613525 A CN201811613525 A CN 201811613525A CN 109573958 A CN109573958 A CN 109573958A
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- flue gas
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B17/00—Sulfur; Compounds thereof
- C01B17/69—Sulfur trioxide; Sulfuric acid
- C01B17/74—Preparation
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- 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
- Y02P20/10—Process efficiency
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- Treating Waste Gases (AREA)
Abstract
The invention discloses a kind of resource utilization methods of flue gas, by adding hydrogen sulfide gas in flue gas, so that the SO in flue gas3It is converted into SO2And sulphur simple substance, completely eliminate the SO in flue gas3, so as to avoid SO3Subsequent recuperation of heat and dust collecting process are impacted, and prepared by reasonable technological design in addition to the sulfuric acid product with high added value, is had high economic benefit.
Description
Technical field
This application involves a kind of resource utilization methods of flue gas during smelting, and in particular to a kind of discharge of sulfur-bearing mining and metallurgy furnace
The resource utilization method of flue gas.
Background technique
At present in China, the raw material for non-ferrous metal metallurgy is mainly sulphide ore, is contained in the flue gas that smelting process generates
There is a large amount of so2, without effective desulfurization process, on the one hand will seriously pollute atmosphere, and on the one hand cause Sulphur ressource again
Serious waste.And in the prior art, there is technology to handle SO2 gas to obtain sulfuric acid product, which is dropping
The product with certain values can be obtained while low pollution.However, sulfur-bearing mining and metallurgy refine caused by ingredient is more in flue gas
Complexity mainly includes SO2, SO3, solid particulate matter, oxygen, carbon dioxide etc..Wherein, to obtain more pure SO2 gas
Body, needs to be dusted flue gas and recuperation of heat is handled, and the SO3 gas then contained in flue gas can be to dedusting, recuperation of heat, wind
The equipment such as machine and corresponding pipeline are corroded, and processing cost is increased.Therefore, it is badly in need of a kind of pair of flue gas during smelting to be located in advance
Reason is to meet acid plant's relieving haperacidity demand.
Summary of the invention
The present invention is in view of the above-mentioned problems, propose a kind of resource utilization method of flue gas during smelting comprising following steps:
(1) by from smelting furnace flue gas and hydrogen sulfide gas I simultaneously be passed through in reduction reactor I so that the big portion in flue gas
Divide sulfur trioxide to react with hydrogen sulfide and be converted into sulfur dioxide, while consuming the oxygen in flue gas；
(2) admixture of gas and hydrogen sulfide gas II that reduction reactor I is discharged are continued while are passed through in reduction reactor II,
So that the remaining sulfur trioxide in admixture of gas is completely converted into sulphur simple substance；
(3) admixture of gas that reduction reactor II is discharged successively is passed through in heat exchanger and deduster and carries out heat recovery and removes
Dirt processing；
(4) admixture of gas of deduster discharge and ozone are passed through in oxidation reactor with by containing in admixture of gas
Hydrogen sulfide is all oxidized；
(5) by oxidation reactor be discharged admixture of gas continue to be passed through in hydrogen peroxide spray column so that in admixture of gas two
Sulfur oxide is totally converted as sulfuric acid and deposits to spray tower bottom；
(6) sulfuric acid for spraying tower bottom is passed through pan tank.
Preferably, convey on flue gas to the pipeline of reduction reactor I that be provided with flue gas flow detector I, sulfur trioxide dense
Spend detector I and oxygen concentration detecting instrument.
Preferably, flue gas stream is provided on from I transport gas mixture of reduction reactor to the pipeline of reduction reactor II
Measure detector II and sulfur trioxide concentration detector II.
Preferably, the amount of the hydrogen sulfide gas in reduction reactor I is passed through in step (1) lower than sulfur trioxide amount in flue gas
One third and amount of oxygen 2/3rds and.
Preferably, the amount for the hydrogen sulfide gas in reduction reactor I being passed through in cloth rapid (1) is equal to sulfur trioxide amount in flue gas
0.2 times with 0.6 times of 2/3rds of amount of oxygen.
Preferably, the amount that the hydrogen sulfide gas in reduction reactor II is passed through in step (2) is mixed greater than the step gas
Three times for closing sulfur trioxide amount in object.
Preferably, the amount that the hydrogen sulfide gas in reduction reactor II is passed through in step (2) is mixed equal to the step gas
Five times for closing sulfur trioxide amount in object.
Preferably, the reduction reactor I and reduction reactor II are flue gas delivery pipe line a part.
Preferably, the temperature of the flue gas from smelting furnace is 1000-1400 DEG C, and the temperature after heat exchanger exchanges heat is
50-100℃。
Preferably, the heat exchanger includes waste heat boiler.
Preferably, the liquid of hydrogen peroxide spray tower bottom is delivered to tower top by the outer spray pump of tower and mixes with fresh hydrogen peroxide
After sprayed.
The present invention is broadly divided into four steps to the resource utilization method of flue gas, is by flue gas and hydrogen sulfide gas first
It is reacted in reduction reactor I, the reaction occurred in the reactor includes:
H2S+3SO3=H2O+4SO2(1), 2H2S+3O2=2SO2+2H2) and 3H O(22S+SO3=3H2), O+4S(3 desired anti-
It should be reaction (1) and (2), and reacting (3) is undesirable reaction type.For this purpose, the present invention passes through to hydrogen sulfide
Intake carry out control avoid reaction (3) generation, obtained optimal hydrogen sulfide additional amount through many experiments.By reduction
The processing of reactor I can convert SO2 for most of SO3 in flue gas, and not reducing the sulfur content in flue gas leads to subsequent mistake
The underproduction of sulfuric acid in journey, and the addition for passing through polluted gas hydrogen sulfide has also increase accordingly the content of SO2.
Secondly as the vulcanization hydrogen amount being passed through in reduction reactor I is limited, SO2 cannot be thoroughly converted by SO3, be
This, the admixture of gas handled by reduction reactor I is further passed through in reduction reactor II, to pass through excess H2S's
It is added so that the remaining SO3 of admixture of gas is completely converted into sulphur simple substance by reacting (3) in thoroughly removing smoke
SO3.And the flue gas for being stripped of SO3 can be to avoid the corrosiveness of heat exchanging device and deduster.
In addition, admixture of gas is passed through in oxidation reactor by smelly again due to the content for increasing H2S in flue gas
The addition of oxygen ensure that the element sulphur in admixture of gas is deposited in the form of SO2 substantially so that H2S is oxidized to oxysulfide entirely
Certainly, sulfur dioxide in flue gas is also a small amount of to be oxidized to sulfur trioxide, but the side reaction can't generate technique
It influences.
Finally, admixture of gas is continued to be passed through in hydrogen peroxide spray column, it is by the oxidation of hydrogen peroxide that sulfur dioxide is complete
Portion is oxidized to sulfuric acid.And due to before the step of in H2S be oxidized to sulfur dioxide, do not have sulphur simple substance substantially
It generates.Due to containing a certain amount of unreacted hydrogen peroxide in sulfuric acid, tower bottom feed liquid can be subjected to circulated sprinkling, and be drained through outside
By the heating of evaporator on the one hand by the hydrogen peroxide in sulfuric acid samples by heating method exclusion in journey, can also by sulfuric acid into
The concentration of one step.
Detailed description of the invention
The present invention is further described in conjunction with the accompanying drawings and embodiments:
Fig. 1 is the specific structure of inventive desulfurization tower and oxidizing tower.
Specific embodiment
For realize the present invention technological means, character of innovation, reach purpose and effect is easy to understand, below with reference to
The present invention is further described for attached drawing.
Fig. 1 is schematic diagram of the invention, as shown, the resource utilization system of the flue gas during smelting of the present embodiment include according to
Reduction reactor I, reduction reactor II and heat exchanger, deduster, oxidation reactor, the hydrogen peroxide spray column, finished product of secondary connection
Slot, wherein reduction reactor I is connect with smelting smoke transmission pipeline, and deduster is connect with smoke discharge tube road after pretreatment,
In, it is dense that flue gas flow detector I, sulfur trioxide are provided on conveying flue gas to the smelting smoke transmission pipeline of reduction reactor I
Detector I and oxygen concentration detecting instrument are spent, is set on from I transport gas mixture of reduction reactor to the pipeline of reduction reactor II
It is equipped with flue gas flow detector II and sulfur trioxide concentration detector II.In addition, on reduction reactor I and reduction reactor II
It is provided with hydrogen sulfide intake pipeline, flow control valve and hydrogen sulfide flow detector are provided on the pipeline.In oxidation reaction
Ozone intake pipeline is provided on device.Hydrogen peroxide spray column successively have from top to bottom demister, spray thrower, flue gas distributor and
Hydrops pond, wherein hydrops pond is connect by the outer spray pump of tower with spray thrower.
Using above system, a kind of resource utilization method of flue gas during smelting is present embodiments provided comprising following step
It is rapid:
(1) by from smelting furnace flue gas and hydrogen sulfide gas I simultaneously be passed through in reduction reactor I so that the big portion in flue gas
Divide sulfur trioxide to react with hydrogen sulfide and be converted into sulfur dioxide, while consuming the oxygen in flue gas.Wherein, it is passed through reduction reaction
The amount of hydrogen sulfide gas in device I is equal in flue gas 0.2 times of sulfur trioxide amount and 0.6 times of 2/3rds of amount of oxygen, sulphur
Change being passed through so that reacting in the reactor for hydrogen: H2S+3SO3=H2O+4SO2(1), 2H2S+3O2=2SO2+2H2O(2).
The generation of above-mentioned reaction is so that most of SO in flue gas3It is converted into SO2, and consumed the oxygen in flue gas.
(2) admixture of gas and hydrogen sulfide gas II that reduction reactor I is discharged are continued while is passed through reduction reactor
In II, so that the remaining sulfur trioxide in admixture of gas is completely converted into sulphur simple substance.Wherein, it is passed through in reduction reactor II
The amount of hydrogen sulfide gas is equal to five times of sulfur trioxide amount in the step admixture of gas, and hydrogen sulfide gas is excessively protected
It has demonstrate,proved and has reacted substantially: 3H2S+SO3=3H2O+4S(3), so that the sulfur trioxide in flue gas is thoroughly discharged, to avoid it
Influence subsequent recuperation of heat and dust removal operation.
(3) admixture of gas that reduction reactor II is discharged successively is passed through waste heat boiler and carries out waste heat recycling, go forward side by side one
Step is passed through in water cooler, so that the temperature of flue gas is reduced to 100 DEG C to be passed through in electric precipitator hereinafter, continuing flue gas after exchanging heat
It is dusted processing.
(4) admixture of gas of deduster discharge and ozone are passed through in oxidation reactor with by containing in admixture of gas
Some hydrogen sulfide is all oxidized to sulfur dioxide or sulfur trioxide.
(5) admixture of gas that oxidation reactor is discharged is continued to be passed through in hydrogen peroxide spray column so that in admixture of gas
Sulfur dioxide be totally converted as sulfuric acid and deposit in the hydrops pond of spray tower bottom, liquid in hydrops pond passes through outside tower
Spray pump is delivered to after tower top is mixed with fresh hydrogen peroxide and is sprayed.
(6) sulfuric acid in hydrops pond is output in evaporator, the sulfuric acid after heated evaporation is output to pan tank.
The foregoing is merely highly preferred embodiment of the present invention, are not intended to restrict the invention.It is all in principle of the invention and
Any modification, equivalent substitution, improvement and etc. done within spirit, should be included within the scope of the present invention.
Claims (9)
1. a kind of resource utilization method of flue gas during smelting, it is characterised in that itself the following steps are included:
(1) by from smelting furnace flue gas and hydrogen sulfide gas I simultaneously be passed through in reduction reactor I so that the big portion in flue gas
Divide sulfur trioxide to react with hydrogen sulfide and be converted into sulfur dioxide, while consuming the oxygen in flue gas；
(2) admixture of gas and hydrogen sulfide gas II that reduction reactor I is discharged are continued while are passed through in reduction reactor II,
So that the remaining sulfur trioxide in admixture of gas is completely converted into sulphur simple substance；
(3) admixture of gas that reduction reactor II is discharged successively is passed through in heat exchanger and deduster and carries out heat recovery and removes
Dirt processing；
(4) admixture of gas of deduster discharge and ozone are passed through in oxidation reactor with by containing in admixture of gas
Hydrogen sulfide is all oxidized；
(5) by oxidation reactor be discharged admixture of gas continue to be passed through in hydrogen peroxide spray column so that in admixture of gas two
Sulfur oxide is totally converted as sulfuric acid and deposits to spray tower bottom；
(6) sulfuric acid for spraying tower bottom is passed through pan tank.
2. according to the method described in claim 1, it is characterized in that being provided with cigarette on conveying flue gas to the pipeline of reduction reactor I
Throughput detector I, sulfur trioxide concentration detector I and oxygen concentration detecting instrument.
3. according to the method described in claim 1, it is characterized in that from I transport gas mixture of reduction reactor to reduction reaction
Flue gas flow detector II and sulfur trioxide concentration detector II are provided on the pipeline of device II.
4. according to the method described in claim 1, it is characterized in that being passed through the stink damp in reduction reactor I in step (1)
The amount of body lower than sulfur trioxide amount in flue gas one third and amount of oxygen 2/3rds and.
5. according to the method described in claim 1, it is characterized in that being passed through the stink damp in reduction reactor I in step (1)
The amount of body is equal in flue gas 0.2 times of sulfur trioxide amount and 0.6 times of 2/3rds of amount of oxygen.
6. according to the method described in claim 1, it is characterized in that being passed through the stink damp in reduction reactor II in step (2)
The amount of body is greater than three times of sulfur trioxide amount in the step admixture of gas.
7. according to the method described in claim 1, it is characterized in that being passed through the stink damp in reduction reactor II in step (2)
The amount of body is equal to five times of sulfur trioxide amount in the step admixture of gas.
8. according to the method described in claim 1, it is characterized in that the reduction reactor I and reduction reactor II is cigarette
Letter shoot line a part.
9. according to the method described in claim 1, it is characterized in that the liquid of the hydrogen peroxide spray tower bottom passes through outside tower
Spray pump is delivered to after tower top is mixed with fresh hydrogen peroxide and is sprayed.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201811613525.7A CN109573958A (en) | 2018-12-27 | 2018-12-27 | A kind of resource utilization method of flue gas during smelting |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201811613525.7A CN109573958A (en) | 2018-12-27 | 2018-12-27 | A kind of resource utilization method of flue gas during smelting |
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| CN109573958A true CN109573958A (en) | 2019-04-05 |
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| CN201811613525.7A Pending CN109573958A (en) | 2018-12-27 | 2018-12-27 | A kind of resource utilization method of flue gas during smelting |
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Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20060053791A1 (en) * | 2003-12-16 | 2006-03-16 | Advanced Combustion Energy Systems, Inc. | Method and apparatus for the production of energy |
| US20070154374A1 (en) * | 2006-01-05 | 2007-07-05 | Envirosolv Energy Llc | Method for removing sulfur dioxide and other acid gases, mercury, and nitrogen oxides from a gas stream with the optional production of ammonia based fertilizers |
| CN101337152A (en) * | 2008-08-07 | 2009-01-07 | 大连海事大学 | Resource ozone oxidation dry method capable of removing sulfur dioxide and nitrogen oxides in flue gas |
| CN107638790A (en) * | 2017-09-25 | 2018-01-30 | 江苏河海新能源股份有限公司 | A kind of denitrating flue gas desulfurizer |
| CN108211711A (en) * | 2017-12-06 | 2018-06-29 | 中国恩菲工程技术有限公司 | Remove smoke the method for middle sulfur trioxide |
| CN108786441A (en) * | 2018-05-31 | 2018-11-13 | 武汉钢铁有限公司 | Coke oven flue gas electromigration desulfurization sulphur technique |
-
2018
- 2018-12-27 CN CN201811613525.7A patent/CN109573958A/en active Pending
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20060053791A1 (en) * | 2003-12-16 | 2006-03-16 | Advanced Combustion Energy Systems, Inc. | Method and apparatus for the production of energy |
| US20070154374A1 (en) * | 2006-01-05 | 2007-07-05 | Envirosolv Energy Llc | Method for removing sulfur dioxide and other acid gases, mercury, and nitrogen oxides from a gas stream with the optional production of ammonia based fertilizers |
| CN101337152A (en) * | 2008-08-07 | 2009-01-07 | 大连海事大学 | Resource ozone oxidation dry method capable of removing sulfur dioxide and nitrogen oxides in flue gas |
| CN107638790A (en) * | 2017-09-25 | 2018-01-30 | 江苏河海新能源股份有限公司 | A kind of denitrating flue gas desulfurizer |
| CN108211711A (en) * | 2017-12-06 | 2018-06-29 | 中国恩菲工程技术有限公司 | Remove smoke the method for middle sulfur trioxide |
| CN108786441A (en) * | 2018-05-31 | 2018-11-13 | 武汉钢铁有限公司 | Coke oven flue gas electromigration desulfurization sulphur technique |
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