CN1600410A - Integration method for ammonia process of desulfurizing flue gas and multiple utilizing desulfurized products and equipment - Google Patents
Integration method for ammonia process of desulfurizing flue gas and multiple utilizing desulfurized products and equipment Download PDFInfo
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- CN1600410A CN1600410A CN 03157599 CN03157599A CN1600410A CN 1600410 A CN1600410 A CN 1600410A CN 03157599 CN03157599 CN 03157599 CN 03157599 A CN03157599 A CN 03157599A CN 1600410 A CN1600410 A CN 1600410A
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- 238000000034 method Methods 0.000 title claims abstract description 44
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 title claims abstract description 41
- 229910021529 ammonia Inorganic materials 0.000 title claims abstract description 20
- 230000003009 desulfurizing effect Effects 0.000 title claims abstract description 12
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims description 43
- 239000003546 flue gas Substances 0.000 title claims description 43
- 230000010354 integration Effects 0.000 title 1
- 239000000243 solution Substances 0.000 claims abstract description 31
- 239000007789 gas Substances 0.000 claims abstract description 24
- 239000007787 solid Substances 0.000 claims abstract description 23
- 239000007864 aqueous solution Substances 0.000 claims abstract description 20
- 238000006243 chemical reaction Methods 0.000 claims abstract description 20
- PQUCIEFHOVEZAU-UHFFFAOYSA-N Diammonium sulfite Chemical compound [NH4+].[NH4+].[O-]S([O-])=O PQUCIEFHOVEZAU-UHFFFAOYSA-N 0.000 claims abstract description 18
- 239000002253 acid Substances 0.000 claims abstract description 16
- GEHJYWRUCIMESM-UHFFFAOYSA-L sodium sulfite Chemical compound [Na+].[Na+].[O-]S([O-])=O GEHJYWRUCIMESM-UHFFFAOYSA-L 0.000 claims abstract description 16
- 150000003863 ammonium salts Chemical class 0.000 claims abstract description 15
- 239000007788 liquid Substances 0.000 claims abstract description 12
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 claims abstract description 11
- 235000011114 ammonium hydroxide Nutrition 0.000 claims abstract description 11
- 229940101006 anhydrous sodium sulfite Drugs 0.000 claims abstract description 10
- 239000000126 substance Substances 0.000 claims abstract description 10
- 238000001914 filtration Methods 0.000 claims abstract description 5
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 claims description 76
- 238000006477 desulfuration reaction Methods 0.000 claims description 76
- 230000023556 desulfurization Effects 0.000 claims description 76
- AOSFMYBATFLTAQ-UHFFFAOYSA-N 1-amino-3-(benzimidazol-1-yl)propan-2-ol Chemical compound C1=CC=C2N(CC(O)CN)C=NC2=C1 AOSFMYBATFLTAQ-UHFFFAOYSA-N 0.000 claims description 19
- 238000010521 absorption reaction Methods 0.000 claims description 13
- BFNBIHQBYMNNAN-UHFFFAOYSA-N ammonium sulfate Chemical group N.N.OS(O)(=O)=O BFNBIHQBYMNNAN-UHFFFAOYSA-N 0.000 claims description 13
- 229910052921 ammonium sulfate Inorganic materials 0.000 claims description 13
- 235000011130 ammonium sulphate Nutrition 0.000 claims description 13
- 238000000746 purification Methods 0.000 claims description 12
- NLXLAEXVIDQMFP-UHFFFAOYSA-N Ammonia chloride Chemical compound [NH4+].[Cl-] NLXLAEXVIDQMFP-UHFFFAOYSA-N 0.000 claims description 10
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 claims description 10
- NBIIXXVUZAFLBC-UHFFFAOYSA-N Phosphoric acid Chemical compound OP(O)(O)=O NBIIXXVUZAFLBC-UHFFFAOYSA-N 0.000 claims description 10
- MNNHAPBLZZVQHP-UHFFFAOYSA-N diammonium hydrogen phosphate Chemical compound [NH4+].[NH4+].OP([O-])([O-])=O MNNHAPBLZZVQHP-UHFFFAOYSA-N 0.000 claims description 10
- 238000004519 manufacturing process Methods 0.000 claims description 9
- QAOWNCQODCNURD-UHFFFAOYSA-N sulfuric acid Substances OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 claims description 9
- 238000001816 cooling Methods 0.000 claims description 7
- 239000003513 alkali Substances 0.000 claims description 6
- 238000001035 drying Methods 0.000 claims description 6
- PAWQVTBBRAZDMG-UHFFFAOYSA-N 2-(3-bromo-2-fluorophenyl)acetic acid Chemical compound OC(=O)CC1=CC=CC(Br)=C1F PAWQVTBBRAZDMG-UHFFFAOYSA-N 0.000 claims description 5
- GRYLNZFGIOXLOG-UHFFFAOYSA-N Nitric acid Chemical compound O[N+]([O-])=O GRYLNZFGIOXLOG-UHFFFAOYSA-N 0.000 claims description 5
- 229910000147 aluminium phosphate Inorganic materials 0.000 claims description 5
- 235000019270 ammonium chloride Nutrition 0.000 claims description 5
- 229910000388 diammonium phosphate Inorganic materials 0.000 claims description 5
- 235000019838 diammonium phosphate Nutrition 0.000 claims description 5
- 229910017604 nitric acid Inorganic materials 0.000 claims description 5
- 238000002425 crystallisation Methods 0.000 claims description 4
- 230000008025 crystallization Effects 0.000 claims description 4
- 239000000428 dust Substances 0.000 claims description 4
- 238000004062 sedimentation Methods 0.000 claims description 3
- 230000003472 neutralizing effect Effects 0.000 claims description 2
- 239000003517 fume Substances 0.000 abstract 2
- ZETCGWYACBNPIH-UHFFFAOYSA-N azane;sulfurous acid Chemical compound N.OS(O)=O ZETCGWYACBNPIH-UHFFFAOYSA-N 0.000 abstract 1
- 238000010410 dusting Methods 0.000 abstract 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 11
- 239000003795 chemical substances by application Substances 0.000 description 4
- 239000012266 salt solution Substances 0.000 description 4
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 3
- 230000008901 benefit Effects 0.000 description 3
- 239000003337 fertilizer Substances 0.000 description 3
- 238000010438 heat treatment Methods 0.000 description 3
- 235000008733 Citrus aurantifolia Nutrition 0.000 description 2
- 235000011941 Tilia x europaea Nutrition 0.000 description 2
- 230000018044 dehydration Effects 0.000 description 2
- 238000006297 dehydration reaction Methods 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 230000007613 environmental effect Effects 0.000 description 2
- 239000010439 graphite Substances 0.000 description 2
- 229910002804 graphite Inorganic materials 0.000 description 2
- 239000004571 lime Substances 0.000 description 2
- 239000007791 liquid phase Substances 0.000 description 2
- 239000012071 phase Substances 0.000 description 2
- 239000012047 saturated solution Substances 0.000 description 2
- 239000000779 smoke Substances 0.000 description 2
- 229940001482 sodium sulfite Drugs 0.000 description 2
- 235000010265 sodium sulphite Nutrition 0.000 description 2
- 239000007921 spray Substances 0.000 description 2
- 238000003860 storage Methods 0.000 description 2
- XTQHKBHJIVJGKJ-UHFFFAOYSA-N sulfur monoxide Chemical class S=O XTQHKBHJIVJGKJ-UHFFFAOYSA-N 0.000 description 2
- 229910052815 sulfur oxide Inorganic materials 0.000 description 2
- 229910052799 carbon Inorganic materials 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000010894 electron beam technology Methods 0.000 description 1
- 238000011049 filling Methods 0.000 description 1
- 239000010881 fly ash Substances 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 238000006386 neutralization reaction Methods 0.000 description 1
- 229910052755 nonmetal Inorganic materials 0.000 description 1
- 238000004806 packaging method and process Methods 0.000 description 1
- 239000012716 precipitator Substances 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 239000008213 purified water Substances 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 239000004071 soot Substances 0.000 description 1
- 238000005728 strengthening Methods 0.000 description 1
- 230000001502 supplementing effect Effects 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
- 239000008946 yang xin Substances 0.000 description 1
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Abstract
A process and apparatus for desulfurizing fume by ammonia method and reclaiming the desulfurized products is disclosed. Said process includes dusting the fume of boiler, desulfurizing reaction on ammonia water to generate the aqueous solution of ammonium hydrogen sulfite and ammonium sulfite, filtering to remove suspended substance, adding excessive acid solution, reacting to generate SO2 gas and aqueous solution of ammonium salt, preparing liquid SO2 or anhydrous sodium sulfite from SO2 gas, and preparing solid ammonium salt from its aqueous solution.
Description
Technical Field
The invention belongs to the technical field of environmental protection, and relates to a flue gas desulfurization method and desulfurization product post-treatment, in particular to an integrated method for flue gas ammonia desulfurization and desulfurization product comprehensive utilization and related production equipment.
Background
China is a country taking coal as a main energy source, and soot type atmospheric pollution mainly comprising sulfur oxides and smoke dust always dominates, so that the pollution of the sulfur oxides is one of the most serious countries in the world. Various desulfurization methods have been developed so far, and are mainly classified into two major types, dry methods and wet methods.
The dry desulfurization mainly comprises a lime method and an ammonia method, and a large amount of waste residues generated after the lime method is used for desulfurization are difficult to treat, so that secondary pollution is caused. The dry ammonia process such as the dry ammonia desulfurization process of Japan is employed with electron beam irradiation. Refer to chinese invention patent application examination specification CN1011858B and chinese invention patent application publication specification CN 1133749A. However, this desulfurization method is expensive in investment and high in running cost.
In wet desulfurization, ammonia is also used for desulfurization, and an ammonia-containing aqueous solution is contacted with flue gas to chemically absorb sulfur dioxide to generate ammonium bisulfite and ammonium sulfite solutions, which are easy to decompose and easily cause secondary pollution in storage or transportation, so that the products are difficult to fully utilize. Meanwhile, the desulfurization product is treated mainly by mixing fly ash to prepare a fertilizer in the prior art, and the single post-treatment method limits the full application of the desulfurization product. In addition, the existing wet desulphurization has large water consumption for ensuring the desulphurization efficiency, so that the desulphurization product is difficult to treat. Therefore, a more effective desulfurization method and an integrated method for comprehensively utilizing desulfurization products are explored, and the method has important practical application value.
Disclosure of Invention
The invention aims to provide an integrated method for flue gas ammonia desulphurization and desulphurization product comprehensive utilization, which is characterized in that after ammonia water is used for flue gas desulphurization, the desulphurization product is continuously subjected to thorough harmless and recycling treatment, and solid ammonium sulfate is produced and liquid sulfur dioxide and anhydrous sodium sulfite are produced.
The invention relates to an integrated method for flue gas ammonia desulphurization and desulphurization product comprehensive utilization, which comprises the following steps:
1) after the boiler flue gas is dedusted, the boiler flue gas and ammonia water are subjected to desulfurization reaction to generate an aqueous solution of ammonium bisulfite and ammonium sulfite, and the desulfurized flue gas is sent into a flue to be discharged;
2) purifying the aqueous solution containing ammonium bisulfite and ammoniumsulfite to remove solid suspended substances in the solution;
3) adding excessive acid solution into the purified aqueous solution of ammonium bisulfite and ammonium sulfite, and sending the aqueous solution into a reaction kettle to generate sulfur dioxide gas and an ammonium salt aqueous solution containing the excessive acid solution;
4) drying, cooling and liquefying the generated sulfur dioxide gas to obtain a liquid sulfur dioxide finished product; or absorbing sulfur dioxide gas with alkali liquor to obtain saturated sodium sulfite solution, and concentrating, crystallizing and centrifugally separating to obtain anhydrous sodium sulfite product; and neutralizing the generated ammonium salt aqueous solution containing excessive acid with ammonia water, and concentrating and crystallizing to obtain a solid ammonium salt finished product.
The reaction principle of the method according to the invention is as follows:
the flue gas is desulfurized by an ammonia method, and the chemical reaction equation is as follows:
the desulfurization product is a mixed aqueous solution of ammonium bisulfite and ammonium sulfite, wherein the ammonium bisulfite accounts for about 68% of the total solute, and the ammonium sulfite accounts for about 32% of the total solute. The solution contains solid impurities, and the solid suspended substances in the solution are filtered out after purification treatment. The purification process is very important for the post-treatment of the desulfurization product, so that the comprehensive utilization rate of the desulfurization product can be improved, and a purer product can be obtained. The purification may be carried out by any apparatus which can achieve the above-mentioned purification purpose, for example, a horizontal screw-discharge decanter centrifuge, an automatic plate and frame filter press, or the like.
The purified desulfurization product is treated by using excessive acid solution, such as concentrated sulfuric acid, phosphoric acid, hydrochloric acid or nitric acid, and the like, wherein the excessive acid solution can be used for fully converting the desulfurization product. Taking the treatment of 98% concentrated sulfuric acid as an example, a solid ammonium sulfate product is generated. The chemical reaction equation is as follows:
correspondingly, if the desulfurization product is treated by phosphoric acid, hydrochloric acid or nitric acid, the finished solid ammonium salt is diammonium hydrogen phosphate and/or ammonium hydrogen phosphate, ammonium chloride or ammonium nitrate.
The generated sulfur dioxide gas can be liquefied to produce a liquid sulfur dioxide finished product, and can also be treated by alkali liquor to generate an anhydrous sodium sulfite finished product, and the anhydrous sodium sulfite finished product can also be produced simultaneously, and the chemical equation of the alkali liquor treatment is as follows:
The ammonium sulfate solution generated by the treatment with sulfuric acid is evaporated and crystallized to obtain a solid ammonium sulfate finished product which can be used for producing a magnetic fertilizer.
Another object of the present invention is to provide an apparatus for carrying out the integrated process of ammonia desulfurization of flue gas and comprehensive utilization of desulfurization products, comprising:
1) the desulfurizing tower can be used for flue gas desulfurization reaction, and is preferably an impinging stream desulfurizing tower provided with a jet atomizer, wherein flue gas and a desulfurizing agent undergo desulfurization reaction to generate ammonium bisulfite and ammonium sulfite;
2) a desulfurization product purification device for filtering solid suspended matters in the desulfurization product solution, such as a horizontal spiral discharge sedimentation centrifuge or an automatic plate and frame filter press;
3) and the reaction kettle is used for post-treating the desulfurization product, the desulfurization product reacts with the acid solution to generate sulfur dioxide gas and ammonium salt solution containing excessive acid, and then the sulfur dioxide gas and the ammonium salt solution are respectively treated.
The device used by the invention also comprises a drying tower, a cooling system, a liquefaction system, an absorption tower, an evaporative crystallization system, a centrifuge, a rotary kiln and corresponding heat exchange and power devices and the like, which are conventional devices in the field.
According to the method and the production device provided by the invention, the preferred process flow is as follows (refer to the process flow chart of fig. 1):
after the dust of boiler flue gas is removed, the boiler flue gas enters a reactor in an impinging stream desulfurization tower provided with a jet atomizer, 5% ammonia water is prepared as a desulfurizing agent, and the desulfurizing agent is sent into the jet atomizer arranged in the reactor in the impinging stream desulfurization tower through an ammonia supply system. The desulfurizing agent is atomized and fully collided with the flue gas in a reactor in the tower in a downstream flow, and is mixed and contacted to generate desulfurization chemical reaction to generate ammonium bisulfite and ammonium sulfite. The purified flue gas is dehydrated by a dehydration and demisting device and then is sent to a chimney by a draught fan for emission. The desulfurization degree may be 95% or more. Most of water in the water solution containing ammonium bisulfite and ammonium sulfite is vaporized by the flue gas, is concentrated to 25-30% of the original sprayed liquid amount, and enters a desulfurization product purification device.
And purifying the desulfurization products of the ammonium bisulfite and the aqueous solution of the ammonium sulfite, and filtering solid suspended substances in the solution. The desulfurization product purification apparatus may employ a purification apparatus which is commonly used in such a case and can remove solid suspended substances in a solution, such as a horizontal spiral discharge decanter centrifuge or an automatic plate and frame filter press.
Feeding the purified ammonium bisulfite, the purified aqueous solution of ammonium bisulfite and excessive acid solution into a reaction kettle, namely a sulfur dioxide generator, drying, cooling and liquefying the generated gas phase part of sulfur dioxide to obtain a liquid sulfur dioxide finished product; the sulfur dioxide gas can also be absorbed in an absorption tower by alkali liquor to obtain a sodium sulfite saturated solution, and the finished anhydrous sodium sulfite is obtained through concentration, crystallization and centrifugal separation. The sulfur dioxide gas which is not completely absorbed can be mixed with the tail gas of the absorption tower in the flue gas before entering the desulfurization tower, and then is desulfurized again, so that the absorption rate of the sulfur dioxide is improved.
The generated liquid phase part is ammonium salt solution containing excessive acid, and after the ammonium salt solution is neutralized by ammonia, solid ammonium salt products are obtained through concentration and crystallization. When the acid solution used in the prior art is concentrated sulfuric acid, a solid ammonium sulfate product can be obtained, and diammonium hydrogen phosphate or ammonium hydrogen phosphate can be generated if phosphoric acid is fed into the reaction kettle. If nitric acid is fed, ammonium nitrate can be generated. If hydrochloric acid is fed, ammonium chloride is produced.
The particular production equipment involved in the above process is not exclusive and it will be apparent to those skilled in the art that the process can be carried out using any equipment or apparatus that achieves the same result.
Compared with the prior art, the invention has the following obvious advantages and effects:
1) the invention integrates desulfurization and the production of solid ammonium sulfate (diammonium hydrogen phosphate or ammonium hydrogen phosphate, ammonium nitrate and ammonium chloride) by using the desulfurization product as well as the co-production of liquid sulfur dioxide and anhydrous sodium sulfite through a reasonable process, thereby not only widening the treatment method of the desulfurization product, but also solving the problem that the desulfurization product is easy to decompose and causes secondary pollution in the prior art, producing chemical products necessary for national economy, realizing the reclamation of the desulfurization product, greatly reducing the actual operation cost or having certain economic benefit.
2) The invention adopts the advanced impinging stream mass principle to mix the flue gas and the ammonia water in the impinging stream desulfurization tower, and adopts the jet atomizer to spray the ammonia water to mix with the flue gas downstream, thereby not only having small resistance, but also strengthening the absorption process, greatly reducing the water consumption, realizing the energy saving and high efficiency of the process of producing solid ammonium sulfate and co-producing liquid sulfur dioxide and anhydrous sodium sulfite by desulfurization products, and solving the problem that the desulfurization products with large water consumption are difficult to treat because the prior wet desulfurization ensures the desulfurization efficiency.
3) When the alkaline liquor is used for absorbing sulfur dioxide gas, because a negative pressure state is formed during the discharge of flue gas, the sulfur dioxide gas which is not completely absorbed by the absorption tower can be mixed with the tail gas of the absorption tower and returned to the flue gas before entering the desulfurization tower, and then enters the desulfurization tower for secondary absorption, so that the absorption rate of sulfur dioxide is improved, not only is the resource of sulfur dioxide fully utilized, but also the pollution of the discharge of the sulfur dioxide gas to air is reduced, and the existing technology for absorbing sulfur dioxide by the alkaline liquor discharges the gas containing sulfur dioxide into the atmosphere, therefore, the invention has obvious advantages for the prior art.
Drawings
FIG. 1 is a process flow diagram of the present invention
Detailed Description
The flue gas desulfurization and post-treatment processes of the present invention will be described in detail with reference to the process flow diagram and by using the following examples, without limiting the scope of the invention.
As shown in figure 1, after 99% of smoke dust in boiler flue gas is removed by an electric precipitator, the boiler flue gas enters a reactor in an impinging stream desulfurization tower (model: TS-10-1000, produced by Zhenjiang Yunto environmental protection mechanical equipment factory), a prepared 5% ammonia water desulfurizer passes through an ammonia supply system, namely a desulfurizer preparation and supply system, and is sent to a jet atomizer (model: PZQZ, produced by Beijing Yangxin New spray mechanical Co., Ltd.) installed in the impinging stream desulfurization reactor, and the desulfurizer fully collides with the flue gas in an atomized state in the reactor in the tower downstream, is mixed and contacted, and generates a desulfurization product, namely ammonium bisulfite and ammonium sulfite. The purified flue gas is dehydrated by a dehydration and demisting device and then is sent into a chimney by a draught fan to be discharged, and the desulfurization rate is about 96 percent.
The desulfurization product is an aqueous solution containing ammonium bisulfite and ammonium sulfite, most of water is vaporized by flue gas, the water is concentrated to 25-30% of the original sprayed liquid amount after coming out of the desulfurization tower, and the concentrated water is collected in a desulfurization product storage tank after passing through a water seal tank and a centrifuge, can be circularly treated according to actual conditions and then enters a desulfurization product purification device.
The water solution of the desulfurization product ammonium bisulfite and ammonium sulfite contains solid suspended matters, and is sent into a purifying device (LW horizontal spiral discharge sedimentation centrifuge, produced by combined fertilizer and astronomical science and technology development Co., Ltd.) for purification, and the solid suspended matters are filtered.
The purified water solution of ammonium bisulfite and ammonium sulfite and excessive concentrated sulfuric acid are sent into a reaction kettle (model: A type four-port metering reaction tank, produced by Jiangsu Yixing nonmetal chemical machinery factory), namely a sulfur dioxide generator, the generated gas phase part of sulfur dioxide is dried by a drying tower, cooled and liquefied by a cooling and liquefying system, and then a liquid sulfur dioxide finished product is obtained by a liquid sulfur dioxide collector and can be bottled.
And the liquid phase part is an ammonium sulfate solution containing excessive sulfuric acid, the ammonium sulfate solution is neutralized by supplementing liquid ammonia through a cooling neutralization kettle to obtain the ammonium sulfate solution, the ammonium sulfate solution is concentrated and crystallized through a centrifugal machine (an SXZ three-foot type automatic lower discharging centrifugal machine, produced by Shijiazhuang new mechanical factory) and a rotary kiln (a direct heating type countercurrent rotary dryer, produced by Guilin metallurgical machinery general factory), and a solid ammonium sulfate product is obtained after packaging.
The sulfur dioxide gas generated previously is sent to a two-section absorption tower (a filling type absorption tower produced by Beijing chemical equipment factory) by a sulfur dioxide fan, is absorbed by alkali liquor with the concentration of 30 percent to obtain sodium sulfite saturated solution, and is concentrated, crystallized, centrifugally separated, dried and packaged by a transit tank, a graphite heating evaporator (YKA type original block hole graphite heating evaporator produced by Jiangsu Nantong carbon factory), a centrifugal machine and a rotary kiln in sequence to obtain the finished anhydrous sodium sulfite. In this stage of the process, as shown in fig. 1, the tail gas of the absorption tower containing unreacted sulfur dioxide gas a can be recycled back to the flue gas before entering the desulfurization tower to be mixed, and then subjected to desulfurization again. The recovery rate of sulfur dioxide can be improved.
According to the above-mentioned technological process, when the excess acid solution is used to treat desulfurization product, if phosphoric acid is fed into the reaction kettle, diammonium hydrogen phosphate or ammonium hydrogen phosphate can be produced. If nitric acid is fed, ammonium nitrate can be generated. If hydrochloric acid is fed, ammonium chloride is produced.
Claims (7)
1. An integrated method for flue gas ammonia desulphurization and desulphurization product comprehensive utilization comprises the following steps:
1) after the boiler flue gas is dedusted, the boiler flue gas and ammonia water are subjected to desulfurization reaction to generate an aqueous solution of ammonium bisulfite and ammonium sulfite, and the desulfurized flue gas is sent into a flue to be discharged;
2) purifying the aqueous solution containing ammonium bisulfite and ammonium sulfite, and filtering solid suspended substances in the solution;
3) adding excessive acid solution into the purified aqueous solution of ammonium bisulfite and ammonium sulfite, and sending the aqueous solution into a reaction kettle to generate sulfur dioxide gas and an ammonium salt aqueous solution containing the excessive acid solution;
4) drying, cooling and liquefying the generated sulfur dioxide gas to obtain a liquid sulfur dioxide finished product;or absorbing sulfur dioxide gas with alkali liquor to obtain saturated sodium sulfite solution, and concentrating, crystallizing and centrifugally separating to obtain anhydrous sodium sulfite product; and neutralizing the generated ammonium salt aqueous solution containing excessive acid with ammonia water, and concentrating and crystallizing to obtain a solid ammonium salt finished product.
2. The integrated process of ammonia desulfurization of flue gas and comprehensive utilization of desulfurization products according to claim 1, characterized in that: and after dust removal, the boiler flue gas enters a reactor in an impinging stream desulfurization tower, and ammonia water fully collides with the flue gas through a jet atomizer in the reactor in the tower in a downstream manner, is mixed and contacts with the flue gas, and generates desulfurization chemical reaction.
3. The integrated process for ammonia desulfurization of flue gas and comprehensive utilization of desulfurization products according to claim 1 or 2, characterized in that: the acid solution can be concentrated sulfuric acid, phosphoric acid, hydrochloric acid or nitric acid, and correspondingly, the finished solid ammonium salt is ammonium sulfate, diammonium hydrogen phosphate and/or ammonium hydrogen phosphate, ammonium chloride or ammonium nitrate.
4. A production facility for the integrated process of ammonia desulfurization of flue gas and comprehensive utilization of desulfurization products as defined in claim 1, comprising:
1) the desulfurizing tower is used for flue gas desulfurization reaction;
2) the desulfurization product purification device is used for filtering solid suspended matters in the desulfurization product solution;
3) the reaction kettle, namely a sulfur dioxide generator, is used for post-treatment of the desulfurization product.
5. The production apparatus according to claim 4, wherein: the desulfurizing tower is an impinging stream desulfurizing tower provided with a jet atomizer.
6. The production apparatus according to claim 4, wherein: the purification device is a horizontal spiral discharge sedimentation centrifuge or a plate and frame filter press.
7. The production apparatus according to claim 4, 5, or 6, wherein: the equipment also can comprise a drying tower, a cooling system, a liquefaction system, an absorption tower, an evaporative crystallization system, a centrifugal machine, a rotary kiln and corresponding heat exchange and power devices.
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| CNB031575994A CN100368061C (en) | 2003-09-24 | 2003-09-24 | Integration method for ammonia process of desulfurizing flue gas and multiple utilizing desulfurized products and equipment |
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| CN100494326C (en) * | 2005-05-13 | 2009-06-03 | 北京思践通科技发展有限公司 | Liquid control method and process of gaseous deacidification using said liquid control method |
| CN101987278A (en) * | 2010-07-28 | 2011-03-23 | 丁正元 | Method for preparing fertilizer grade monoammonium phosphate from sulfurous gases by ammonia-process desulfurization |
| CN102211762A (en) * | 2010-04-06 | 2011-10-12 | 山东三维石化工程股份有限公司 | Method for preparing sulfur and processing tail gas by taking ammonium bisulfite as intermediate |
| CN101601964B (en) * | 2009-06-03 | 2012-01-11 | 李鹏举 | Ammonia flue gas desulfurization device |
| CN101612515B (en) * | 2008-06-28 | 2013-01-02 | 金隆铜业有限公司 | Wet flue gas desulfurization method |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| DE2143444B2 (en) * | 1971-08-31 | 1972-11-23 | Chemiebau Dr. A. Zieren GmbH & Co KG, 5000 Köln | PROCESS FOR PROCESSING THE WASHING SOLUTION DURING THE WASHING OF EXHAUST GASES OF SO DEEP TWO |
| FR2161188A6 (en) * | 1971-06-08 | 1973-07-06 | Inst Francais Du Petrole | |
| CN1087180C (en) * | 1999-01-07 | 2002-07-10 | 华东理工大学 | Process for purifying and recovering waste SOx gas from coal boiler |
| CN2389708Y (en) * | 1999-09-22 | 2000-08-02 | 阎洪滨 | Dedusting desulfurizing equipment for boiler |
| CN1136948C (en) * | 2001-12-07 | 2004-02-04 | 罗经宇 | Process and equipment for treating flue gas with tower of kittle tray |
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