CN116462160B - By flue gas SO2Method and system for preparing steady-state chlorine dioxide for raw materials - Google Patents
By flue gas SO2Method and system for preparing steady-state chlorine dioxide for raw materials Download PDFInfo
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- CN116462160B CN116462160B CN202310319768.4A CN202310319768A CN116462160B CN 116462160 B CN116462160 B CN 116462160B CN 202310319768 A CN202310319768 A CN 202310319768A CN 116462160 B CN116462160 B CN 116462160B
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- chlorine dioxide
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- OSVXSBDYLRYLIG-UHFFFAOYSA-N dioxidochlorine(.) Chemical compound O=Cl=O OSVXSBDYLRYLIG-UHFFFAOYSA-N 0.000 title claims abstract description 100
- 239000004155 Chlorine dioxide Substances 0.000 title claims abstract description 51
- 235000019398 chlorine dioxide Nutrition 0.000 title claims abstract description 51
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 31
- 239000003546 flue gas Substances 0.000 title claims abstract description 31
- 239000002994 raw material Substances 0.000 title claims abstract description 21
- 238000006243 chemical reaction Methods 0.000 claims abstract description 46
- 238000010521 absorption reaction Methods 0.000 claims abstract description 37
- 239000007788 liquid Substances 0.000 claims abstract description 26
- UKLNMMHNWFDKNT-UHFFFAOYSA-M sodium chlorite Chemical compound [Na+].[O-]Cl=O UKLNMMHNWFDKNT-UHFFFAOYSA-M 0.000 claims abstract description 24
- 229960002218 sodium chlorite Drugs 0.000 claims abstract description 24
- FQENQNTWSFEDLI-UHFFFAOYSA-J sodium diphosphate Chemical compound [Na+].[Na+].[Na+].[Na+].[O-]P([O-])(=O)OP([O-])([O-])=O FQENQNTWSFEDLI-UHFFFAOYSA-J 0.000 claims abstract description 24
- 229940048086 sodium pyrophosphate Drugs 0.000 claims abstract description 24
- 235000019818 tetrasodium diphosphate Nutrition 0.000 claims abstract description 24
- 239000001577 tetrasodium phosphonato phosphate Substances 0.000 claims abstract description 24
- 238000000034 method Methods 0.000 claims abstract description 23
- 239000000292 calcium oxide Substances 0.000 claims abstract description 19
- ODINCKMPIJJUCX-UHFFFAOYSA-N calcium oxide Inorganic materials [Ca]=O ODINCKMPIJJUCX-UHFFFAOYSA-N 0.000 claims abstract description 19
- KZBUYRJDOAKODT-UHFFFAOYSA-N Chlorine Chemical compound ClCl KZBUYRJDOAKODT-UHFFFAOYSA-N 0.000 claims abstract description 18
- BRPQOXSCLDDYGP-UHFFFAOYSA-N calcium oxide Chemical compound [O-2].[Ca+2] BRPQOXSCLDDYGP-UHFFFAOYSA-N 0.000 claims abstract description 18
- 229920000168 Microcrystalline cellulose Polymers 0.000 claims abstract description 14
- 239000008108 microcrystalline cellulose Substances 0.000 claims abstract description 14
- 235000019813 microcrystalline cellulose Nutrition 0.000 claims abstract description 14
- 229940016286 microcrystalline cellulose Drugs 0.000 claims abstract description 14
- 239000000843 powder Substances 0.000 claims abstract description 10
- 239000007787 solid Substances 0.000 claims abstract description 10
- 238000005192 partition Methods 0.000 claims description 47
- 239000007789 gas Substances 0.000 claims description 45
- 238000002156 mixing Methods 0.000 claims description 39
- 239000007864 aqueous solution Substances 0.000 claims description 3
- 238000006477 desulfuration reaction Methods 0.000 abstract description 22
- 230000023556 desulfurization Effects 0.000 abstract description 22
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 abstract description 16
- 239000000460 chlorine Substances 0.000 abstract description 16
- 229910052801 chlorine Inorganic materials 0.000 abstract description 16
- 239000002912 waste gas Substances 0.000 abstract description 5
- 239000002253 acid Substances 0.000 abstract description 4
- 239000003463 adsorbent Substances 0.000 abstract description 3
- 239000003381 stabilizer Substances 0.000 abstract description 3
- 239000000203 mixture Substances 0.000 abstract description 2
- 238000005516 engineering process Methods 0.000 description 8
- 238000002485 combustion reaction Methods 0.000 description 6
- 239000010440 gypsum Substances 0.000 description 6
- 229910052602 gypsum Inorganic materials 0.000 description 6
- 239000000047 product Substances 0.000 description 6
- 239000006096 absorbing agent Substances 0.000 description 4
- 239000006227 byproduct Substances 0.000 description 4
- 230000008569 process Effects 0.000 description 4
- 230000009286 beneficial effect Effects 0.000 description 3
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 description 3
- 239000000920 calcium hydroxide Substances 0.000 description 3
- 229910001861 calcium hydroxide Inorganic materials 0.000 description 3
- 239000003795 chemical substances by application Substances 0.000 description 3
- 239000003245 coal Substances 0.000 description 3
- 230000003009 desulfurizing effect Effects 0.000 description 3
- XLYOFNOQVPJJNP-ZSJDYOACSA-N heavy water Substances [2H]O[2H] XLYOFNOQVPJJNP-ZSJDYOACSA-N 0.000 description 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 2
- 235000019738 Limestone Nutrition 0.000 description 2
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 description 2
- 238000004458 analytical method Methods 0.000 description 2
- 239000006028 limestone Substances 0.000 description 2
- 238000004064 recycling Methods 0.000 description 2
- 238000003756 stirring Methods 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 1
- UXVMQQNJUSDDNG-UHFFFAOYSA-L Calcium chloride Chemical compound [Cl-].[Cl-].[Ca+2] UXVMQQNJUSDDNG-UHFFFAOYSA-L 0.000 description 1
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 1
- 230000004913 activation Effects 0.000 description 1
- 239000003513 alkali Substances 0.000 description 1
- 150000001412 amines Chemical class 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- 239000004566 building material Substances 0.000 description 1
- 239000011575 calcium Substances 0.000 description 1
- 229910052791 calcium Inorganic materials 0.000 description 1
- 239000001110 calcium chloride Substances 0.000 description 1
- 229910001628 calcium chloride Inorganic materials 0.000 description 1
- QKIRHLCRDJURQV-UHFFFAOYSA-K calcium;sodium;trihydroxide Chemical compound [OH-].[OH-].[OH-].[Na+].[Ca+2] QKIRHLCRDJURQV-UHFFFAOYSA-K 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 238000004891 communication Methods 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000001035 drying Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 230000003993 interaction Effects 0.000 description 1
- 239000000395 magnesium oxide Substances 0.000 description 1
- CPLXHLVBOLITMK-UHFFFAOYSA-N magnesium oxide Inorganic materials [Mg]=O CPLXHLVBOLITMK-UHFFFAOYSA-N 0.000 description 1
- AXZKOIWUVFPNLO-UHFFFAOYSA-N magnesium;oxygen(2-) Chemical compound [O-2].[Mg+2] AXZKOIWUVFPNLO-UHFFFAOYSA-N 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 239000000376 reactant Substances 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 239000011780 sodium chloride Substances 0.000 description 1
- 239000001509 sodium citrate Substances 0.000 description 1
- NLJMYIDDQXHKNR-UHFFFAOYSA-K sodium citrate Chemical compound O.O.[Na+].[Na+].[Na+].[O-]C(=O)CC(O)(CC([O-])=O)C([O-])=O NLJMYIDDQXHKNR-UHFFFAOYSA-K 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
- 238000005507 spraying Methods 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
- 238000011144 upstream manufacturing Methods 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B11/00—Oxides or oxyacids of halogens; Salts thereof
- C01B11/02—Oxides of chlorine
- C01B11/022—Chlorine dioxide (ClO2)
- C01B11/023—Preparation from chlorites or chlorates
- C01B11/024—Preparation from chlorites or chlorates from chlorites
-
- 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
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A50/00—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE in human health protection, e.g. against extreme weather
- Y02A50/20—Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters
Landscapes
- Life Sciences & Earth Sciences (AREA)
- General Life Sciences & Earth Sciences (AREA)
- Geology (AREA)
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Inorganic Chemistry (AREA)
- Treating Waste Gases (AREA)
Abstract
The invention relates to the technical field of waste gas desulfurization, in particular to a method and a system for preparing steady-state chlorine dioxide by taking flue gas SO 2 as a raw material, wherein SO 2 in the flue gas reacts with sodium chlorite, sodium pyrophosphate and chlorine gas which are fed into a tubular absorption reactor to generate liquid ClO 2, and the liquid ClO 2 enters a reaction kettle to be adsorbed by calcium oxide and microcrystalline cellulose to generate a chlorine dioxide solid powder product. The invention does not adopt strong acid, thus improving the safety of the reaction; calcium oxide is taken as a stabilizer of chlorine dioxide, microcrystalline cellulose is added as an adsorbent, and the mixture is directly reacted to generate solid powder of the chlorine dioxide, and the solid powder of the chlorine dioxide is dried to obtain a product; by adopting a tube array type absorption reactor, negative pressure is formed in the tube by utilizing high-speed liquid flow to absorb SO 2 and chlorine, and the chlorine dioxide is generated by reacting in a main tube, SO that the absorption and conversion efficiency is higher than that of the traditional absorption tower.
Description
Technical Field
The invention relates to the technical field of waste gas desulfurization, in particular to a method and a system for preparing steady-state chlorine dioxide by taking flue gas SO 2 as a raw material.
Background
The world is the largest SO 2 emission country, and annual SO 2 emission reduction is increased year by year. At present, the common control technology of the SO 2 of the coal at home and abroad is mainly divided into pre-combustion desulfurization, in-combustion desulfurization and post-combustion flue gas desulfurization. Before burning, sulfur content in raw coal is controlled by washing and selecting method. The desulfurization in combustion is mainly a circulating fluidized bed combustion desulfurization technology and a furnace calcium spraying and tail humidifying activation technology at present. Desulfurization efficiency of desulfurization technology before and during combustion is limited, and along with the increasingly strict emission standard of SO 2 in China, flue gas desulfurization becomes a necessary way for controlling emission of fire coal SO 2. The flue gas desulfurization technology capable of realizing recycling of desulfurization byproducts comprises a limestone-gypsum wet method, a double-alkali method, a magnesium oxide method, an ammonia method, a circulating fluidized bed semi-dry method, a sodium citrate absorption and analysis method, a regenerated organic amine absorption and analysis method, an active carbon adsorption method and the like.
The limestone-gypsum wet desulfurization has the advantages of mature technical process, higher desulfurization efficiency and the like, and becomes the most widely applied desulfurization technology at present. In the technology, the desulfurizing agent is limestone, which is a non-renewable desulfurizing agent, and the natural environment is seriously damaged by limestone exploitation. The desulfurization product is desulfurization gypsum (CaSO 4·2H2 O) which is often used as a building material, but the desulfurization gypsum has higher water content, poorer quality, lower value, high transportation cost and more transportation cost than the natural gypsum. At present, a large amount of desulfurization gypsum produced every year in China is discarded, so that pollution transfer is caused.
Because of the huge discharge amount of SO 2 in China, a large amount of desulfurization byproducts are produced while a large amount of desulfurizing agents are consumed in flue gas desulfurization, SO that the problem of recycling the byproducts of the flue gas desulfurization technology is more concerned.
Disclosure of Invention
In view of the defects of the prior art, the invention provides a method and a system for preparing steady-state chlorine dioxide by taking flue gas SO 2 as a raw material, which are used for preparing the chlorine dioxide by taking SO 2 in waste gas and cheap chlorine as raw materials, and do not adopt strong acid, SO that the safety of the reaction is improved.
In order to achieve the purpose, the technical scheme provided by the invention is that the method for preparing steady-state chlorine dioxide by taking flue gas SO 2 as a raw material is characterized in that SO 2 in flue gas reacts with sodium chlorite, sodium pyrophosphate and chlorine gas which are fed into a tubular absorption reactor to generate liquid ClO 2, and the liquid ClO 2 enters a reaction kettle to be adsorbed by calcium oxide and microcrystalline cellulose to generate a chlorine dioxide solid powder product.
Preferably, the concentration of the sodium chlorite is 0.2mol/L-0.3mol/L, and the concentration of the sodium pyrophosphate is 0.02mol/L-0.03mol/L of aqueous solution.
Preferably, the volume ratio of sodium chlorite to sodium pyrophosphate fed into the tubular absorption reactor is 1:1.
Further, the tail gas after the reaction in the tubular absorption reactor is introduced into a reaction kettle.
On the other hand, the invention provides a system for preparing steady-state chlorine dioxide by taking flue gas SO 2 as a raw material, which comprises a mixing tank, a sodium chlorite storage tank, a sodium pyrophosphate storage tank, a tubular absorption reactor and a reaction kettle; the sodium chlorite storage tank is connected with the mixing tank; the sodium pyrophosphate storage tank is connected with the mixing tank; the tubular absorption reactor is connected with the mixing tank, and is provided with a chlorine gas inlet, an SO 2 gas inlet, a chlorine dioxide liquid outlet and a tail gas outlet, wherein the chlorine gas inlet is connected with a chlorine gas bottle, and the SO 2 gas inlet is connected with an external flue gas pipeline; the reaction kettle is connected with the chlorine dioxide liquid outlet, and calcium oxide and microcrystalline cellulose are accommodated in the reaction kettle.
Further, the sodium chlorite storage tank is connected with the mixing tank through a first pipeline, and a first metering pump is arranged on the first pipeline.
Further, the sodium pyrophosphate storage tank is connected with the mixing tank through a second pipeline, and a second metering pump is arranged on the second pipeline.
Further, the mixing tank is connected with the tubular absorption reactor through a third pipeline, and a jet pump is arranged on the third pipeline.
Further, a gas distributor is arranged in the reaction kettle, and the tail gas outlet is connected to the gas distributor through a pipeline.
Further, the shell and tube absorption reactor includes many single tubes that are parallel to each other, the single tube includes the body is inside to be provided with first division wall and the second division wall, the inboard of first division wall separates out the convergent chamber, the inboard of second division wall separates out the divergent chamber, the tip of convergent chamber with the tip of divergent chamber sets up relatively, the outside of the inside first division wall of body is provided with the third division wall, the outside of the inside second division wall of body is provided with the fourth division wall, the third division wall and the fourth division wall separate out the mixing chamber with the space outside first division wall and the second division wall, mixing chamber UNICOM convergent chamber and divergent chamber, the body has been seted up liquid entry, liquid entry UNICOM extremely the convergent chamber has been seted up to the body, gas entry UNICOM extremely mixing chamber.
Further, the first partition wall and the second partition wall are both conical, and the third partition wall and the fourth partition wall are both annular.
The invention has the beneficial effects that: the SO 2 in the waste gas and the cheap chlorine are used as raw materials to prepare the chlorine dioxide, strong acid is not used, and the safety of the reaction is improved; calcium oxide is taken as a stabilizer of chlorine dioxide, microcrystalline cellulose is added as an adsorbent, and the mixture is directly reacted to generate solid powder of the chlorine dioxide, and the solid powder of the chlorine dioxide is dried to obtain a product; by adopting a tube array type absorption reactor, negative pressure is formed in the tube by utilizing high-speed liquid flow to absorb SO 2 and chlorine, and the chlorine dioxide is generated by reacting in a main tube, SO that the absorption and conversion efficiency is higher than that of the traditional absorption tower.
Drawings
FIG. 1 is a process flow diagram of preparing steady-state chlorine dioxide from flue gas SO 2 in accordance with an embodiment of the present invention;
FIG. 2 is a schematic view showing the structure of a single tube in a tubular absorption reactor according to an embodiment of the present invention;
In the figure: 100. a mixing tank is arranged on the upper surface of the mixing tank,
200. A sodium chlorite storage tank,
300. A storage tank for sodium pyrophosphate,
400. A tubular absorption reactor 410, a chlorine inlet, 420, an SO 2 gas inlet, 430, a chlorine dioxide liquid outlet, 440, a tail gas outlet, 450, a single tube, 451, a tubular body, 4511, a liquid inlet, 4512, a gas inlet, 452, a first partition wall, 453, a second partition wall, 454, a tapering chamber, 455, a diverging chamber, 456, a third partition wall, 457, a fourth partition wall, 458, a mixing chamber,
500. A reaction kettle, 510 and a gas distributor,
600. A chlorine cylinder is used for the chlorine cylinder,
700. The first conduit, 710, the first metering pump,
800. A second pipeline, 810, a second metering pump,
900. Third pipe, 910, jet pump.
Detailed Description
In order that the above objects, features and advantages of the invention will be readily understood, a more particular description of the invention will be rendered by reference to the appended drawings. In the following description, numerous specific details are set forth in order to provide a thorough understanding of the present invention. The present invention may be embodied in many other forms than described herein and similarly modified by those skilled in the art without departing from the spirit of the invention, whereby the invention is not limited to the specific embodiments disclosed below.
An embodiment of the present invention provides a method for preparing steady-state chlorine dioxide from flue gas SO 2, which reacts SO 2 in flue gas with sodium chlorite, sodium pyrophosphate and chlorine gas fed into a tubular absorption reactor 400 to generate liquid ClO 2. The reaction equation is as follows:
SO2+Cl2+2H2O→H2SO4+2HCl
5NaClO2+2H2SO4→4ClO2+2Na2SO4+NaCl+2H2O
5NaClO2+4HCl→4ClO2+5NaCl+2H2O
Then enters a reaction kettle 500 to be adsorbed by calcium oxide and microcrystalline cellulose to generate a chlorine dioxide solid powder product.
According to the method for preparing the steady-state chlorine dioxide, SO 2 in the waste gas and cheap chlorine are used as raw materials to prepare the steady-state chlorine dioxide, strong acid is not needed, and the safety of the reaction is improved. Calcium oxide is taken as a stabilizer of chlorine dioxide, microcrystalline cellulose is added as an adsorbent, and the calcium oxide is directly reacted to generate solid powder of the chlorine dioxide, and the product is obtained after drying. By adopting the shell-and-tube absorption reactor 400, namely utilizing high-speed liquid flow to form negative pressure in the tube to absorb SO 2 and chlorine, and reacting in the main tube to generate chlorine dioxide, the absorption and conversion efficiency is higher than that of the traditional absorption tower.
Further, in one embodiment, the tail gas after the reaction in the shell-and-tube absorber 400 enters the reactor 500 through the gas distributor 510 in the reactor 500. The reaction equation of the residual SO 2 in the tail gas and the chlorine gas are reacted by sodium hydroxide calcium generated after the calcium oxide in the reaction kettle 500 absorbs water is as follows:
CaO+H2O→Ca(OH)2；
Ca(OH)2+SO2→CaSO3+H2O；
Ca(OH)2+Cl2→CaCl2+H2O。
SO set up, in the reaction kettle 50 tail gas enters into the reaction kettle through the gas distributor 510, plays the effect of stirring, and residual SO 2 and chlorine in the tail gas can react with calcium oxide and be absorbed, SO no pollution gas is discharged.
Preferably, in one embodiment, sodium chlorite is used at a concentration of 0.2mol/L to 0.3mol/L and sodium pyrophosphate is used at a concentration of 0.02mol/L to 0.03mol/L in aqueous solution.
Preferably, in one embodiment, the volume ratio of sodium chlorite to sodium pyrophosphate fed to the tubular absorber reactor 400 is 1:1, a step of; further, the volume ratio of SO 2 to chlorine is 1:1. when the metering pump is specifically arranged, the metering pump can be used for feeding in an equal volume.
Preferably, the concentration of the calcium oxide is 20-40g/L, and the content of the microcrystalline cellulose is 10-20g/L.
The embodiment of the invention provides a system for preparing steady-state chlorine dioxide by taking flue gas SO 2 as a raw material, which comprises a mixing tank 100, a sodium chlorite storage tank 200, a sodium pyrophosphate storage tank 300, a tubular absorption reactor 400 and a reaction kettle 500, wherein sodium chlorite stored in the sodium chlorite storage tank 200 and sodium pyrophosphate stored in the sodium pyrophosphate storage tank 300 are sent into the mixing tank 100 for mixing and then are sent into the tubular absorption reactor 400; the sodium chlorite storage tank 200 is connected with the mixing tank 100; the sodium pyrophosphate storage tank 300 is connected with the mixing tank 100; the shell and tube absorption reactor 400 is connected with the mixing tank 100, the shell and tube absorption reactor 400 is provided with a chlorine gas inlet 410, an SO 2 gas inlet 420, a chlorine dioxide liquid outlet 430 and a tail gas outlet 440, the chlorine gas inlet 410 is connected with a chlorine gas bottle 600, and the SO 2 gas inlet 420 is connected with an external flue gas pipeline (not shown in the figure); the reaction kettle 500 is connected with a chlorine dioxide liquid outlet 430, and calcium oxide and microcrystalline cellulose are accommodated in the reaction kettle 500. Preferably, the reaction vessel 500 contains calcium oxide (concentration of 20-40 g/L) and microcrystalline cellulose (concentration of 10-20 g/L).
The specific process of the reaction is as follows: raw materials of sodium chlorite storage tank 200 and sodium pyrophosphate storage tank 300 are introduced into mixing tank 100, mixed liquid enters tubular absorption reactor 400, meanwhile chlorine in chlorine cylinder 600 enters tubular absorption reactor 400 through chlorine inlet 410, SO 2 gas enters tubular absorption reactor 400 through SO 2 gas inlet 420, liquid chlorine dioxide is generated after reaction and enters reaction kettle 500, and chlorine dioxide reacts with calcium oxide and microcrystalline cellulose in reaction kettle 500 to form chlorine dioxide solid powder product.
In one embodiment, sodium chlorite storage tank 200 is connected to mixing tank 100 by a first conduit 700 with a first metering pump 710 disposed on first conduit 700.
In one embodiment, the sodium pyrophosphate storage tank 300 is connected to the mixing tank 100 by a second pipe 800, and a second metering pump 810 is provided on the second pipe 800.
It should be noted that, the first metering pump 710 is disposed on the first pipe 700, and the second metering pump 810 is disposed on the second pipe 800, so that the equal volume of the materials in the sodium chlorite storage tank 200 and the sodium pyrophosphate storage tank 300 can be monitored and controlled to be counted into the mixing tank 100, which is more beneficial to the reaction.
In one embodiment, the mixing tank 100 is connected to the shell-and-tube absorber 400 through a third pipe 900, and a jet pump 910 is disposed on the third pipe 900.
It should be noted that, the ejector pump 910 is disposed upstream of the tubular absorption reactor 400, which is more beneficial to mixing the reactants.
In one embodiment, a gas distributor 510 is provided inside the reaction vessel 500, and the tail gas outlet 440 is connected to the gas distributor 510 through a pipe. By the arrangement, the tail gas entering the reaction kettle 500 can be distributed more uniformly inside the reaction kettle 500, so that the reaction efficiency of the liquid chlorine dioxide, the calcium oxide and the microcrystalline cellulose is improved, and the yield of steady-state chlorine dioxide is improved. The reaction byproducts in the tubular absorption reactor 400 all enter the reaction kettle 500, and no residual liquid is discharged; in the reaction kettle 500, the tail gas enters the reaction kettle 500 through the gas distributor 510 to play a role in stirring, and residual SO 2 and chlorine in the tail gas can react with calcium oxide to be absorbed, SO that no pollution gas is discharged.
In an embodiment, the shell-and-tube absorber 400 includes a plurality of single tubes 450 parallel to each other, the single tubes 450 include a tube body 451, a first partition wall 452 and a second partition wall 453 are disposed inside the tube body 451, a tapered chamber 454 is partitioned from the inner side of the first partition wall 452, a diverging chamber 455 is partitioned from the inner side of the second partition wall 453, a third partition wall 456 is disposed at the outer side of the first partition wall 452 inside the tube body 451, a fourth partition wall 457 is disposed at the outer side of the second partition wall 453 inside the tube body 451, the third partition wall 456 and the fourth partition wall 457 partition the space between the first partition wall 452 and the outer side of the second partition wall 453 into a mixing chamber 458, the tapered chamber 454 and the diverging chamber 455 are communicated with each other, a liquid inlet 4511 is formed in the tube body 451, a gas inlet 4512 is formed in the tube body 451, and the gas inlet 4512 is communicated with the mixing chamber 458.
The specific process of the reaction is as follows: the high-velocity liquid containing sodium chlorite and sodium pyrophosphate entering through liquid inlet 4511 flows through converging chamber 454 to create a negative pressure in mixing chamber 458, is drawn into mixing chamber 20 with the chlorine and SO 2 gases entering through gas inlet 4512, and reacts in diverging chamber 455 and tube 451 to form chlorine dioxide.
In one embodiment, the first partition wall 452 and the second partition wall 453 are conical, and the third partition wall 456 and the fourth partition wall 457 are annular.
The first partition wall 452 and the second partition wall 453 may have other shapes with gradually smaller cross-sectional radii than a cone, for example, a hemispherical shape, as long as the requirement of "gradually smaller diameter" is satisfied. The third partition 456 and the fourth partition 457 may be adaptively provided according to the specific shapes of the first partition 452 and the second partition 453.
In the description of the present invention, it should be understood that the terms "center", "longitudinal", "lateral", "length", "width", "thickness", "upper", "lower", "front", "rear", "left", "right", "vertical", "horizontal", "top", "bottom", "inner", "outer", "clockwise", "counterclockwise", "axial", "radial", "circumferential", etc. indicate orientations or positional relationships based on the orientations or positional relationships shown in the drawings are merely for convenience in describing the present invention and simplifying the description, and do not indicate or imply that the device or element being referred to must have a specific orientation, be configured and operated in a specific orientation, and therefore should not be construed as limiting the present invention.
Furthermore, the terms "first," "second," and the like, are used for descriptive purposes only and are not to be construed as indicating or implying a relative importance or implicitly indicating the number of technical features indicated. Thus, a feature defining "a first" or "a second" may explicitly or implicitly include at least one such feature. In the description of the present invention, the meaning of "plurality" means at least two, for example, two, three, etc., unless specifically defined otherwise.
In the present invention, unless explicitly specified and limited otherwise, the terms "mounted," "connected," "secured," and the like are to be construed broadly, and may be, for example, fixedly connected, detachably connected, or integrally formed; can be mechanically or electrically connected; either directly or indirectly, through intermediaries, or both, may be in communication with each other or in interaction with each other, unless expressly defined otherwise. The specific meaning of the above terms in the present invention can be understood by those of ordinary skill in the art according to the specific circumstances.
In the present invention, unless expressly stated or limited otherwise, a first feature "up" or "down" a second feature may be the first and second features in direct contact, or the first and second features in indirect contact via an intervening medium. Moreover, a first feature being "above," "over" and "on" a second feature may be a first feature being directly above or obliquely above the second feature, or simply indicating that the first feature is level higher than the second feature. The first feature being "under", "below" and "beneath" the second feature may be the first feature being directly under or obliquely below the second feature, or simply indicating that the first feature is less level than the second feature.
It will be understood that when an element is referred to as being "fixed" or "disposed" on another element, it can be directly on the other element or intervening elements may also be present. When an element is referred to as being "connected" to another element, it can be directly connected to the other element or intervening elements may also be present. The terms "vertical," "horizontal," "upper," "lower," "left," "right," and the like are used herein for illustrative purposes only and are not meant to be the only embodiment.
Claims (9)
1. The method for preparing steady-state chlorine dioxide by using flue gas SO 2 as a raw material is characterized by comprising the following steps of: SO 2 in the flue gas reacts with sodium chlorite, sodium pyrophosphate and chlorine gas which are fed into a tubular absorption reactor to generate liquid ClO 2, and the liquid ClO 2 enters a reaction kettle to be adsorbed by calcium oxide and microcrystalline cellulose to generate a chlorine dioxide solid powder product.
2. The method for preparing steady-state chlorine dioxide by using flue gas SO 2 as raw material according to claim 1, wherein: the concentration of the sodium chlorite is 0.2mol/L-0.3mol/L, and the concentration of the sodium pyrophosphate is 0.02mol/L-0.03mol/L of aqueous solution.
3. The method for preparing steady-state chlorine dioxide by using flue gas SO 2 as raw material according to claim 2, wherein: the volume ratio of sodium chlorite to sodium pyrophosphate fed into the tubular absorption reactor is 1:1.
4. The method for preparing steady-state chlorine dioxide by using flue gas SO 2 as raw material according to claim 1, wherein: the method also comprises the step of introducing the tail gas after the reaction in the tubular absorption reactor into the reaction kettle.
5. The system for preparing steady-state chlorine dioxide by taking flue gas SO 2 as a raw material is characterized in that: comprising
A mixing tank;
a sodium chlorite storage tank connected with the mixing tank;
a sodium pyrophosphate storage tank connected with the mixing tank;
The tubular absorption reactor is connected with the mixing tank and is provided with a chlorine gas inlet, an SO 2 gas inlet, a chlorine dioxide liquid outlet and a tail gas outlet, the chlorine gas inlet is connected with a chlorine gas bottle, and the SO 2 gas inlet is connected with an external flue gas pipeline; the tube type absorption reactor comprises a plurality of single tubes which are parallel to each other, the single tubes comprise a tube body, a first partition wall and a second partition wall are arranged in the tube body, a converging chamber is separated from the inner side of the first partition wall, a diverging chamber is separated from the inner side of the second partition wall, the small end of the converging chamber and the small end of the diverging chamber are oppositely arranged, a third partition wall is arranged on the outer side of the first partition wall in the tube body, a fourth partition wall is arranged on the outer side of the second partition wall in the tube body, a mixing chamber is separated from the space on the outer side of the first partition wall and the space on the outer side of the second partition wall by the third partition wall and the fourth partition wall, the mixing chamber is communicated with the converging chamber and the diverging chamber, a liquid inlet is arranged on the tube body and is communicated with the converging chamber, a gas inlet is arranged on the tube body,
The gas inlet is communicated to the mixing chamber;
And the reaction kettle is connected with the chlorine dioxide liquid outlet, and calcium oxide and microcrystalline cellulose are accommodated in the reaction kettle.
6. The system for preparing steady-state chlorine dioxide by using flue gas SO 2 as raw material according to claim 5, wherein:
The sodium chlorite storage tank is connected with the mixing tank through a first pipeline, and a first metering pump is arranged on the first pipeline.
7. The system for preparing steady-state chlorine dioxide by using flue gas SO 2 as raw material according to claim 5, wherein: the sodium pyrophosphate storage tank is connected with the mixing tank through a second pipeline, and a second metering pump is arranged on the second pipeline; the mixing tank is connected with the tubular absorption reactor through a third pipeline, and a jet pump is arranged on the third pipeline.
8. The system for preparing steady-state chlorine dioxide by using flue gas SO 2 as raw material according to claim 5, wherein: the inside gas distributor that is provided with of reation kettle, the tail gas export is connected to through the pipeline gas distributor.
9. The system for preparing steady-state chlorine dioxide by using flue gas SO 2 as raw material according to claim 5, wherein: the first partition wall and the second partition wall are conical, and the third partition wall and the fourth partition wall are annular.
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