CN104368240A - Method and device for magnetizing and purifying flue gas in gas-solid reaction - Google Patents
Method and device for magnetizing and purifying flue gas in gas-solid reaction Download PDFInfo
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- CN104368240A CN104368240A CN201410653602.7A CN201410653602A CN104368240A CN 104368240 A CN104368240 A CN 104368240A CN 201410653602 A CN201410653602 A CN 201410653602A CN 104368240 A CN104368240 A CN 104368240A
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- 238000000034 method Methods 0.000 title claims abstract description 49
- 239000007787 solid Substances 0.000 title claims abstract description 23
- 239000003546 flue gas Substances 0.000 title claims abstract description 22
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 18
- 238000006243 chemical reaction Methods 0.000 title abstract description 11
- 230000005291 magnetic effect Effects 0.000 claims abstract description 152
- 239000003054 catalyst Substances 0.000 claims abstract description 106
- 239000007789 gas Substances 0.000 claims abstract description 99
- 238000006555 catalytic reaction Methods 0.000 claims abstract description 54
- 230000003197 catalytic effect Effects 0.000 claims abstract description 29
- 238000007254 oxidation reaction Methods 0.000 claims abstract description 12
- 230000003647 oxidation Effects 0.000 claims abstract description 11
- 230000008569 process Effects 0.000 claims abstract description 11
- 239000003344 environmental pollutant Substances 0.000 claims abstract description 9
- 231100000719 pollutant Toxicity 0.000 claims abstract description 7
- 239000007788 liquid Substances 0.000 claims description 23
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 22
- 229910052799 carbon Inorganic materials 0.000 claims description 21
- 239000011148 porous material Substances 0.000 claims description 18
- 238000012856 packing Methods 0.000 claims description 15
- 238000003746 solid phase reaction Methods 0.000 claims description 12
- 229910021536 Zeolite Inorganic materials 0.000 claims description 11
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 claims description 11
- 239000010457 zeolite Substances 0.000 claims description 11
- 239000000779 smoke Substances 0.000 claims description 9
- 238000001035 drying Methods 0.000 claims description 8
- 229910021645 metal ion Inorganic materials 0.000 claims description 8
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 claims description 5
- 229910052751 metal Inorganic materials 0.000 claims description 5
- 239000002184 metal Substances 0.000 claims description 5
- 150000000703 Cerium Chemical class 0.000 claims description 3
- 150000001868 cobalt Chemical class 0.000 claims description 3
- RBTARNINKXHZNM-UHFFFAOYSA-K iron trichloride Chemical compound Cl[Fe](Cl)Cl RBTARNINKXHZNM-UHFFFAOYSA-K 0.000 claims description 3
- 150000002603 lanthanum Chemical class 0.000 claims description 3
- 150000002696 manganese Chemical class 0.000 claims description 3
- 239000002808 molecular sieve Substances 0.000 claims description 3
- 150000002815 nickel Chemical class 0.000 claims description 3
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 claims description 3
- 230000004913 activation Effects 0.000 claims description 2
- 239000000969 carrier Substances 0.000 claims description 2
- 238000005470 impregnation Methods 0.000 claims description 2
- 238000001802 infusion Methods 0.000 claims description 2
- 238000010521 absorption reaction Methods 0.000 abstract description 13
- 238000000746 purification Methods 0.000 abstract description 8
- 238000005265 energy consumption Methods 0.000 abstract description 4
- 230000008901 benefit Effects 0.000 abstract description 3
- 238000002156 mixing Methods 0.000 abstract description 3
- 238000009827 uniform distribution Methods 0.000 abstract description 3
- 230000007613 environmental effect Effects 0.000 abstract description 2
- RBFQJDQYXXHULB-UHFFFAOYSA-N arsane Chemical compound [AsH3] RBFQJDQYXXHULB-UHFFFAOYSA-N 0.000 abstract 2
- 229910000070 arsenic hydride Inorganic materials 0.000 abstract 2
- 239000010410 layer Substances 0.000 description 103
- 239000003463 adsorbent Substances 0.000 description 29
- 230000000694 effects Effects 0.000 description 15
- 239000007790 solid phase Substances 0.000 description 15
- 230000008929 regeneration Effects 0.000 description 13
- 238000011069 regeneration method Methods 0.000 description 13
- 238000013461 design Methods 0.000 description 12
- 238000009826 distribution Methods 0.000 description 12
- 230000008859 change Effects 0.000 description 8
- 230000005415 magnetization Effects 0.000 description 8
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 7
- 230000003139 buffering effect Effects 0.000 description 6
- 238000004140 cleaning Methods 0.000 description 5
- 239000003599 detergent Substances 0.000 description 5
- 238000011010 flushing procedure Methods 0.000 description 5
- 238000000265 homogenisation Methods 0.000 description 5
- 230000004044 response Effects 0.000 description 5
- 239000011949 solid catalyst Substances 0.000 description 5
- 238000006424 Flood reaction Methods 0.000 description 4
- 238000005516 engineering process Methods 0.000 description 4
- 239000000945 filler Substances 0.000 description 4
- 239000012535 impurity Substances 0.000 description 4
- 239000011229 interlayer Substances 0.000 description 4
- 239000007791 liquid phase Substances 0.000 description 4
- 239000001301 oxygen Substances 0.000 description 4
- 229910052760 oxygen Inorganic materials 0.000 description 4
- 238000010025 steaming Methods 0.000 description 4
- 230000003213 activating effect Effects 0.000 description 3
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 3
- 230000033228 biological regulation Effects 0.000 description 3
- 230000015572 biosynthetic process Effects 0.000 description 3
- 239000011521 glass Substances 0.000 description 3
- 238000010438 heat treatment Methods 0.000 description 3
- 230000006872 improvement Effects 0.000 description 3
- 229910052757 nitrogen Inorganic materials 0.000 description 3
- 230000005298 paramagnetic effect Effects 0.000 description 3
- 238000011160 research Methods 0.000 description 3
- 238000001179 sorption measurement Methods 0.000 description 3
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 description 2
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 2
- 229910019142 PO4 Inorganic materials 0.000 description 2
- 239000002250 absorbent Substances 0.000 description 2
- 230000002745 absorbent Effects 0.000 description 2
- 239000000654 additive Substances 0.000 description 2
- 230000000996 additive effect Effects 0.000 description 2
- HSJPMRKMPBAUAU-UHFFFAOYSA-N cerium(3+);trinitrate Chemical compound [Ce+3].[O-][N+]([O-])=O.[O-][N+]([O-])=O.[O-][N+]([O-])=O HSJPMRKMPBAUAU-UHFFFAOYSA-N 0.000 description 2
- UFMZWBIQTDUYBN-UHFFFAOYSA-N cobalt dinitrate Chemical compound [Co+2].[O-][N+]([O-])=O.[O-][N+]([O-])=O UFMZWBIQTDUYBN-UHFFFAOYSA-N 0.000 description 2
- 229910001981 cobalt nitrate Inorganic materials 0.000 description 2
- ORTQZVOHEJQUHG-UHFFFAOYSA-L copper(II) chloride Chemical compound Cl[Cu]Cl ORTQZVOHEJQUHG-UHFFFAOYSA-L 0.000 description 2
- 238000011161 development Methods 0.000 description 2
- 230000018109 developmental process Effects 0.000 description 2
- 230000005684 electric field Effects 0.000 description 2
- 239000012530 fluid Substances 0.000 description 2
- FBAFATDZDUQKNH-UHFFFAOYSA-M iron chloride Chemical compound [Cl-].[Fe] FBAFATDZDUQKNH-UHFFFAOYSA-M 0.000 description 2
- VCJMYUPGQJHHFU-UHFFFAOYSA-N iron(3+);trinitrate Chemical compound [Fe+3].[O-][N+]([O-])=O.[O-][N+]([O-])=O.[O-][N+]([O-])=O VCJMYUPGQJHHFU-UHFFFAOYSA-N 0.000 description 2
- 230000033001 locomotion Effects 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 230000007246 mechanism Effects 0.000 description 2
- KBJMLQFLOWQJNF-UHFFFAOYSA-N nickel(ii) nitrate Chemical compound [Ni+2].[O-][N+]([O-])=O.[O-][N+]([O-])=O KBJMLQFLOWQJNF-UHFFFAOYSA-N 0.000 description 2
- 230000005408 paramagnetism Effects 0.000 description 2
- 239000010452 phosphate Substances 0.000 description 2
- NBIIXXVUZAFLBC-UHFFFAOYSA-K phosphate Chemical compound [O-]P([O-])([O-])=O NBIIXXVUZAFLBC-UHFFFAOYSA-K 0.000 description 2
- DJHGAFSJWGLOIV-UHFFFAOYSA-K Arsenate3- Chemical compound [O-][As]([O-])([O-])=O DJHGAFSJWGLOIV-UHFFFAOYSA-K 0.000 description 1
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 description 1
- 229910021586 Nickel(II) chloride Inorganic materials 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 239000005864 Sulphur Substances 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 230000002378 acidificating effect Effects 0.000 description 1
- 238000003915 air pollution Methods 0.000 description 1
- 229940000489 arsenate Drugs 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- VYLVYHXQOHJDJL-UHFFFAOYSA-K cerium trichloride Chemical compound Cl[Ce](Cl)Cl VYLVYHXQOHJDJL-UHFFFAOYSA-K 0.000 description 1
- OZECDDHOAMNMQI-UHFFFAOYSA-H cerium(3+);trisulfate Chemical compound [Ce+3].[Ce+3].[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O OZECDDHOAMNMQI-UHFFFAOYSA-H 0.000 description 1
- 229910000333 cerium(III) sulfate Inorganic materials 0.000 description 1
- GVPFVAHMJGGAJG-UHFFFAOYSA-L cobalt dichloride Chemical compound [Cl-].[Cl-].[Co+2] GVPFVAHMJGGAJG-UHFFFAOYSA-L 0.000 description 1
- MPMSMUBQXQALQI-UHFFFAOYSA-N cobalt phthalocyanine Chemical class [Co+2].C12=CC=CC=C2C(N=C2[N-]C(C3=CC=CC=C32)=N2)=NC1=NC([C]1C=CC=CC1=1)=NC=1N=C1[C]3C=CC=CC3=C2[N-]1 MPMSMUBQXQALQI-UHFFFAOYSA-N 0.000 description 1
- KTVIXTQDYHMGHF-UHFFFAOYSA-L cobalt(2+) sulfate Chemical compound [Co+2].[O-]S([O-])(=O)=O KTVIXTQDYHMGHF-UHFFFAOYSA-L 0.000 description 1
- 239000012141 concentrate Substances 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 239000000356 contaminant Substances 0.000 description 1
- XTVVROIMIGLXTD-UHFFFAOYSA-N copper(II) nitrate Chemical compound [Cu+2].[O-][N+]([O-])=O.[O-][N+]([O-])=O XTVVROIMIGLXTD-UHFFFAOYSA-N 0.000 description 1
- ARUVKPQLZAKDPS-UHFFFAOYSA-L copper(II) sulfate Chemical compound [Cu+2].[O-][S+2]([O-])([O-])[O-] ARUVKPQLZAKDPS-UHFFFAOYSA-L 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 235000003891 ferrous sulphate Nutrition 0.000 description 1
- 239000011790 ferrous sulphate Substances 0.000 description 1
- 239000008246 gaseous mixture Substances 0.000 description 1
- 230000002779 inactivation Effects 0.000 description 1
- 239000002440 industrial waste Substances 0.000 description 1
- 229910052742 iron Inorganic materials 0.000 description 1
- BAUYGSIQEAFULO-UHFFFAOYSA-L iron(2+) sulfate (anhydrous) Chemical compound [Fe+2].[O-]S([O-])(=O)=O BAUYGSIQEAFULO-UHFFFAOYSA-L 0.000 description 1
- RUTXIHLAWFEWGM-UHFFFAOYSA-H iron(3+) sulfate Chemical compound [Fe+3].[Fe+3].[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O RUTXIHLAWFEWGM-UHFFFAOYSA-H 0.000 description 1
- 229910000359 iron(II) sulfate Inorganic materials 0.000 description 1
- 229910000360 iron(III) sulfate Inorganic materials 0.000 description 1
- FYDKNKUEBJQCCN-UHFFFAOYSA-N lanthanum(3+);trinitrate Chemical compound [La+3].[O-][N+]([O-])=O.[O-][N+]([O-])=O.[O-][N+]([O-])=O FYDKNKUEBJQCCN-UHFFFAOYSA-N 0.000 description 1
- GJKFIJKSBFYMQK-UHFFFAOYSA-N lanthanum(3+);trinitrate;hexahydrate Chemical compound O.O.O.O.O.O.[La+3].[O-][N+]([O-])=O.[O-][N+]([O-])=O.[O-][N+]([O-])=O GJKFIJKSBFYMQK-UHFFFAOYSA-N 0.000 description 1
- VQEHIYWBGOJJDM-UHFFFAOYSA-H lanthanum(3+);trisulfate Chemical compound [La+3].[La+3].[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O VQEHIYWBGOJJDM-UHFFFAOYSA-H 0.000 description 1
- ICAKDTKJOYSXGC-UHFFFAOYSA-K lanthanum(iii) chloride Chemical compound Cl[La](Cl)Cl ICAKDTKJOYSXGC-UHFFFAOYSA-K 0.000 description 1
- 238000010297 mechanical methods and process Methods 0.000 description 1
- 230000005226 mechanical processes and functions Effects 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- QMMRZOWCJAIUJA-UHFFFAOYSA-L nickel dichloride Chemical compound Cl[Ni]Cl QMMRZOWCJAIUJA-UHFFFAOYSA-L 0.000 description 1
- LGQLOGILCSXPEA-UHFFFAOYSA-L nickel sulfate Chemical compound [Ni+2].[O-]S([O-])(=O)=O LGQLOGILCSXPEA-UHFFFAOYSA-L 0.000 description 1
- 229910000363 nickel(II) sulfate Inorganic materials 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 239000012071 phase Substances 0.000 description 1
- 239000012286 potassium permanganate Substances 0.000 description 1
- 230000002028 premature Effects 0.000 description 1
- 238000003672 processing method Methods 0.000 description 1
- 230000001737 promoting effect Effects 0.000 description 1
- 239000000376 reactant Substances 0.000 description 1
- 230000009257 reactivity Effects 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 238000012216 screening Methods 0.000 description 1
- 229910001220 stainless steel Inorganic materials 0.000 description 1
- 239000010935 stainless steel Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 239000002912 waste gas Substances 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
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- Treating Waste Gases (AREA)
- Exhaust Gas Treatment By Means Of Catalyst (AREA)
- Physical Or Chemical Processes And Apparatus (AREA)
- Catalysts (AREA)
Abstract
The invention discloses a method and device for magnetizing and purifying flue gas in gas-solid reaction and belongs to the field of atmospheric pollution control of environmental protection. The method comprises the following steps of: under the conditions that the temperature is 0-200 DEG C and the magnetic field exists, introducing the flue gas to be purified into a reactor containing a catalyst to carry out catalytic-oxidation enriched purification on one or more pollutants in AsH3, H2S, HCN and PH3 in the gas. The method disclosed by the invention has the advantages that enriched purification for target foreign gas in the flue gas is realized by the magnetic-assisting type catalysis process, highly-uniform distribution, absorption and catalytic oxidation of one or more pollutants in AsH3, H2S, HCN and PH3 in the reactor can be realized, gas-solid two-phase high-efficiency uniform mixing is realized, the method is simple, the cost is low and the energy consumption can be reduced.
Description
Technical field
The present invention relates to method and device that a kind of magnetic helps gas-solid phase reaction purifying smoke, belong to environmental protection air contaminant treatment field.
Background technology
In recent years, atmosphere polluting problem becomes the hot issue of field of environment protection gradually, especially compares to the improvement of industrial smoke etc. the stage being still in technology and relatively falling behind with other developed countries.The smoke gas treatment technology of industrial applications is gas-solid phase reactor comparatively widely at present.It is made up of sections such as gas pre-distributor, homogenizing space, fixed bed (comprising beds and inert filler layer) and outlet gas sections usually.Be characterized in that the flowing of bed inner fluid is close to piston flow, structure is simple, easy to operate, and investment cost is low, the catalytic mechanical wearing and tearing feature such as little in bed.
One of important indicator of gas-solid phase reactor performance quality is exactly that can the adsorbent (catalyst) at each position in adsorbent (catalyst) bed obtain and utilize to greatest extent.Suppose that gas-solid phase reactor design is bad, can be uneven due to air flow method, make to occur dead angle and poisoned region in adsorbent (catalyst) bed, cause a part of adsorbent (catalyst) excess load and premature inactivation, another part adsorbent (catalyst) but works hardly, thus causing whole course of reaction in reactor to worsen, reactivity worth declines.
Typical gas-solid phase reactor, its inside comprises the sections such as air inlet, gas pre-distributor, homogenizing space, top, top inert filler layer, bottom inert filler layer, supporting screening plate, homogenizing space, bottom and gas outlet from top to bottom.These sections are maintained close ties with, influence each other, and all around a common target---when low-energy-consumption, realization response thing uniform stream is distributed on each cross section of adsorbent (catalyst) bed, whole catalyst can be obtained and evenly and fully utilize.But in actual mechanical process, often there is reactant flow skewness, catalyst can not evenly and fully be utilized, and the problem that droop loss is large.
There are many researchers to post and wish to be made by improvement flue gas mode of entrance, fixed bed bed structural reform, realize uniform catalyst use efficiency in real time, these changes make original technology obtain many improvement really, especially little for reactor diameter, the situation that uniform fluid distribution problem is not given prominence to, but constantly advance along with process of industrialization, the expansion of industrial development and scale, plant capacity maximizes, and the airflow uniform distribution problem day of large diameter gas-solid phase reactor is aobvious outstanding.
Patent CN2075277 discloses a kind of Combined flow velocity uniform distributor, similar multistage baffle plate gas pre-distributor, and can accomplish that air flow method in catalytic bed relatively evenly but its complex structure, reactor pressure decrease loss is larger.
Research mostly all concentrates on inlet gas pre-distributor component itself and carries out, and the research that binding reactor packing layer carries out is then less, and patent CN201454503 is also by realizing airflow uniform distribution to the design of air inlet.
Although backflow phenomenon can be avoided at air inlet as far as possible, improving the uniform property of air inlet, for entering bed main body, when reacting with adsorbent (catalyst) bed, being still difficult to control its equally distributed stability.
Summary of the invention
The present invention to solve exist in gas-solid phase reactor because of adsorption catalyst or filler self size, the difference of shape and character, and the problem of uniform inequality in the catalytic bed caused, a kind of magnetic is provided to help the method for gas-solid phase reaction purifying smoke, pending flue gas, under temperature 0 ~ 200 DEG C, magnetic field existence condition, passes in the reactor that catalyst is housed the AsH in gas by the method
3, H
2s, HCN, PH
3in one or more pollutants carry out catalytic oxidation enrichment, above-mentioned pollutant is effectively separated with other substance Cs O in gas etc., thus realize the enrichment of target impurity gas in flue gas is purified, wherein magnetic field intensity is 0.05 ~ 10T.
Described catalyst is adopt conventional infusion process at the obtained unitary metal ion catalyst of one or both metal ions of supported on carriers or binary metal enhancement mode catalyst, wherein carrier is the one in active carbon, molecular sieve, zeolite, alundum (Al2O3), unitary metal ion catalyst be by concentration be the molysite of 0.01 ~ 1mol/L, after mantoquita, manganese salt or nickel salt impregnated carrier dry activation is formed, binary metal enhancement mode catalyst be by unitary metal ion catalyst concentration be the cobalt salt of 0.01 ~ 1mol/L, impregnation drying obtains after activating in lanthanum salt or cerium salt.
Described molysite is the one in ferric nitrate, iron chloride, ferric sulfate, frerrous chloride, ferrous sulfate;
Described mantoquita is the one in copper nitrate, copper chloride, copper sulphate, Schweinfurt green;
Described manganese salt is potassium permanganate;
Described nickel salt is the one in nickel nitrate, nickel chloride, nickelous sulfate;
Described cobalt salt is the one in cobalt nitrate, cobalt chloride, cobaltous sulfate, sulfonated phthalocyanine cobalt;
Described lanthanum salt is the one in lanthanum nitrate, lanthanum chloride, lanthanum sulfate;
Described cerium salt is the one in cerous nitrate, cerium chloride, cerous sulfate.
Another object of the present invention is to provide and realizes magnetic and help the gas-solid of the method for gas-solid phase reaction purifying smoke to magnetize catalytic reactor mutually, it comprises triangle dividing plate 3, upper cover 4, cylindrical shell 7, magnetic co catalysis layer 8, upper cover 4 is arranged on cylindrical shell 7 by flange 5, cylindrical shell 7 top is provided with air inlet 1, air inlet 1 lower end is provided with pore sieve plate 2, triangle dividing plate 3 is provided with below pore sieve plate 2, cylindrical shell 7 top is provided with top homogenizing layer 6, cylindrical shell 7 bottom is provided with bottom homogenizing layer 14, magnetic co catalysis layer 8 is arranged between top homogenizing layer 6 and bottom homogenizing layer 14 by packing support plate 12, homogenizing layer 14 side, bottom has gas outlet 13, liquid flowing outlet 15 is provided with bottom bottom homogenizing layer 14, cylindrical shell 7 bottom is provided with catalyst discharge port 11, wherein magnetic co catalysis layer 8 comprises magnetic field generator 17 and catalyst, magnetic field generator 17 arranges in the catalyst, and its magnetic direction produced is parallel with airflow direction, cylindrical shell 7 or pore sieve plate 2 are provided with heater (see figure 1).
Described magnetic field generator 17 is permanent magnet 9 or electromagnetic generator 18, and wherein arrange as the magnet poles direction of axial arranging arranges identical in the magnetic field of permanent magnet 9, and the magnet poles of arranged adjacent is different.
Described magnetic co catalysis layer 8 arranged outside mechanical vibrator framework 16, external frequency regulation device, rapping intensity is 50-200g, rapping time 1-2min, rapping stroke 30-50mm, rapping frequency 20-80 time/min; Described mechanical vibrator framework 16 be designed with two effects, one is the structure change in order to prevent adsorbent (catalyst) from causing because of local magnetized, two be in order to adsorbent (catalyst) regenerate time, promote adsorb (catalysis) impurity removal in solid phase microcellular structure.
The object of the invention is according to faraday's magnetic conductivity principle, utilize the difference of the element of object gas and the magnetic of nitrogen element, coordinate the paramagnetism that magnetic field is special to these gases, in catalyst solid medium, form a kind of bonding state efficiently, improve the uniform ability of gas in gas solid catalytic reactor.Although the molecule of oxygen and the nitrogen element that to be same period adjacent composition, but magnetic difference is but very large: there are two p electronics to become singly to occupy the higher antibonding orbital of energy in oxygen molecule, create molecule circulation, so have magnetic, nitrogen molecule does not then possess such ability.The p electronics of picture oxygen molecule two on antibonding orbital is unstable, so under the effect of extra electric field, by originally unordered warm-up movement, can be transformed into the motion consistent with external electric field direction.The magnetic susceptibility of oxygen is 150 times of nitrogen in addition, if this mechanism of Appropriate application, experiment condition reasonable in design, just can effectively utilize oxygen, AsH
3, H
2s, HCN, PH
3deng paramagnetic gas, to form magnetization gas, when being conducive to the condition realizing low-temperature micro-oxygen, reproducibility gaseous mixture preferably and adsorbent (catalyst) combine, improve the comprehensive utilization ratio of adsorbent (catalyst) widely, adsorbent (catalyst) time of break-through can be extended greatly.
The method of gas-solid phase reaction flue gas magnetic purifying of the present invention is under normal temperature, magnetic field existence condition, paramagnetic gas will be had be magnetized in axial gas-solid phase reactor, it is inner that a gas part after magnetization is adsorbed on solid phase micropore by adsorbent (catalyst), makes adsorbent (catalyst) and then form certain local magnetized region.AsH
3, H
2s, HCN, PH
3deng gas molecule itself, there is paramagnetism, but its this character seldom obtains extensive use both domestic and external, in current air pollution control technique method, no matter be wet method or dry method, all need to utilize the gas be dissolved in water body medium or the gas be adsorbed in solid dielectric to carry out, and to face maximum problem be at present exactly that gas absorption is incomplete, and the problem that local penetrates too early, the magnetic field adopting permanent magnet to be formed, magnetizes object gas.The adsorbent (catalyst) of gas is magnetized by magnetic cohesion before the magnetisable gas newly entered is adsorbed with by bed and these, define " association " that magnetic is attracting, the uniform performance of object gas in solid absorbent (catalyst) medium is increased greatly, thus find one to reduce energy consumption, with low cost, the simple processing method of method, meets AsH
3, H
2s, HCN, PH
3etc. there being paramagnetic gas adsorbance in solid dielectric to increase, and can also on the basis of original gas-solid phase reactor physical absorption, chemisorbed, the means of a kind of " magnetization physical absorption " are provided.
Said apparatus air inlet 1 connects flue gas to be clean, the effect of thin mouth sieve plate 2 strengthens air stream turbulence, the design of triangle dividing plate 3 is to reduce the local return straight up and down caused by air inlet, cause the problem of inside reactor distribution of gas inequality, the top homogenizing layer 6 that cylindrical shell top is arranged, object better realizes even gas distribution; Flange 5 being set in order to open upper cover 4, easy cleaning reactor, carrying out flushing catalyst or adding catalyst; Magnetization absorption (catalysis) purification process of magnetic co catalysis layer 8 realize target gas in cylindrical shell 7;
In the present invention, permanent magnet can, material that mechanical strength large anticorrosion at outer layer covers, and object prevents magnet and object gas from reacting, and for acidic and alkaline gas, actified solution has higher decay resistance.
Gas solid-phase adsorbent (catalyst) of the present invention refers to general conventional active carbon, molecular sieve, zeolite, alundum (Al2O3) etc. and their modified product, and there is certain mechanical strength, the adsorbent (catalyst) that will bed be caused to disperse because magnetic field is excessive, such as some activated-carbon catalyst is through modification, the metal that part can be magnetized is contained in activated centre, certain magnetic can be produced after magnetization, thus make adsorbent (catalyst) in formation local magnetized district around magnet, and from magnet relatively away from space form sparse solid-phase construction.In order to improve the mechanical strength of catalytic bed, the ratio of Cuiization Ji ︰ zeolite=1 ︰ 0.5-2 can be adopted to mix, and such magnetic fields just can not make catalytic bed produce excessive gap, and catalysis efficiency is improved.
When using permanent magnet as magnetic field generator; between permanent magnet layer, buffering packing layer can be set; buffering packing layer refers to the glass dregs, zeolite etc. that mechanical strength is larger, and object is that protection fixed bed inner magnet axial spacing can not be excessive because of magnetic force, oppresses catalyst and deformation occurs.
The material that reactor of the present invention adopts is stainless steel, prevents the problems such as catalyst regeneration stage corrosion.
Gaseous Temperature Control System of the present invention can adopt increases a gas preheating unit below pore sieve plate 2, cylindrical shell 7 inside is provided with temperature detector and controls, also can adopt and carry out heated constant temperature at cylindrical shell 7 outer setting heating jacket to reactor.
Apparatus of the present invention purpose of design one is the object gas AsH making to enter reactor
3, H
2s, HCN, PH
3deng, flow through reactor from top to down, because autologous density is larger, comparatively speaking can natural subsidence, the energy loss of equipment can be reduced; Two is top homogenizing layer 6 volumes: magnetic co catalysis layer 8 volumes=1:7-12, certain homogenization is had at initial segment comparatively speaking after gas can be made like this to enter reactor, reduce gas backstreaming, three is catalytic bed and magnetization center, magnetic field and indirect magnetic field can be formed at inside reactor, the area that the solid catalyst that increase can be magnetized contacts with object gas, reduces the resistance to mass tranfer between gas-solid mutually.
The magnetic pole of the different magnetic of magnetic field generator is fixed on the inside of reactor by the present invention, ensure the stability in magnetic field, on the one hand, object gas is magnetized by highfield, on the other hand, the solid phase micropore again magnetization aspiration being attached to adsorbent (catalyst) is inner, makes adsorbent (catalyst) and then forms certain local magnetized region.Magnetic field generator produce magnetic can long-time stable magnetic field is provided, the adsorbent (catalyst) magnetizing gas before the magnetisable gas newly entered is adsorbed with by bed and these defines magnetic attracting " association ", the uniform performance of object gas in solid absorbent (catalyst) medium is increased greatly, there is provided the means of a kind of " magnetization physical absorption ", for the technological operation promoting fixed bed provides more help.
Beneficial effect of the present invention is:
1, compared with additive method, a lot of method not yet carries out the research of even gas distribution for inside reactor at present, although most method obtains certain effect by the change of air inlet method, is still difficult to solve the uniform problem of inside reactor.Advantage of the present invention is noiseless, and energy consumption is lower, and the magnetic field produced by magnetic co catalysis process, strengthens gas-solid catalysis;
2, compared with other Magnitizing methods, the present invention is according to main containing in CO industrial tail gas, AsH
3, H
2s, HCN, PH
3etc. the feature that foreign gas is easily magnetized, by magnetic co catalysis process, be different from the simple single means increasing magnetic field magnetisation, this method treatment process mechanism is clear.Treated, the adsorption capacity of above-mentioned several foreign gas is strengthened greatly, and purification efficiency reaches more than 98%;
3, structure is simple and make easy fixed bed gas-solid catalysis method, consider the advantage of additive method, propose the thinking of oneself, do not adopt complicated form, ensure that the stability of implementation environment, like this after reactor, the clean-up effect of waste gas is significantly good, and the development for industrial waste gas provides some new thinkings, and real meaning achieves gas-particle two-phase and efficiently mixes, compared with single operating unit, this method can provide more alternative condition.
Accompanying drawing explanation
Fig. 1 is structural representation of the present invention;
The structural representation of Fig. 2 to be apparatus of the present invention magnetic field generator be permanent magnetic iron;
The structural representation of Fig. 3 to be apparatus of the present invention magnetic field generator be electromagnetic generator;
Fig. 4 has magnetic field and does not have magnetic field to PH in the present invention
3, H
2s, AsH
3, HCN detergent power affect result schematic diagram;
In figure: 1-air inlet, 2-pore sieve plate, 3-triangle dividing plate, 4-upper cover, 5-flange, 6-top homogenizing layer, 7-cylindrical shell, 8-catalyst, 9-permanent magnet, 10-cushions packing layer, 11-catalyst discharge port, 12-packing support plate, 13-gas outlet, 14-bottom homogenizing layer, 15-liquid flowing outlet, 16-mechanical vibrator framework, 17-magnetic field generator, 18-electromagnetic generator, 19-electromagnetism fixed head, 20-power supply.
Detailed description of the invention
Below in conjunction with the drawings and specific embodiments, the invention will be further described, but scope is not limited to described content.
embodiment 1:this magnetic helps gas-solid phase reaction to purify PH
3the method of flue gas, 20 DEG C, under the existence condition of magnetic field, will containing PH
3flue gas passes in the reactor that catalyst is housed the PH in gas
3pollutant carries out catalytic oxidation enrichment, and wherein magnetic field intensity is 0.5T, and described catalyst is after copper chloride solution active carbon being placed in concentration 0.1mol/L floods 24h, and dry 10h inside 105 DEG C of drying boxes is obtained activate 4h at 270 DEG C after.
The gas-solid completing said method magnetizes catalytic reactor mutually for the structure shown in Fig. 2, it comprises triangle dividing plate 3, upper cover 4, cylindrical shell 7, magnetic co catalysis layer 8, upper cover 4 is arranged on cylindrical shell 7 by flange 5, cylindrical shell 7 top is provided with air inlet 1, air inlet 1 lower end is provided with pore sieve plate 2, triangle dividing plate 3 is provided with below pore sieve plate 2, cylindrical shell 7 top is provided with top homogenizing layer 6, top homogenizing layer 6 volume: magnetic co catalysis layer 8 volumes=1:7, cylindrical shell 7 bottom is provided with bottom homogenizing layer 14, magnetic co catalysis layer 8 is arranged between top homogenizing layer 6 and bottom homogenizing layer 14 by packing support plate 12, homogenizing layer 14 side, bottom has gas outlet 13, liquid flowing outlet 15 is provided with bottom bottom homogenizing layer 14, cylindrical shell 7 bottom is provided with catalyst discharge port 11, wherein magnetic co catalysis layer 8 comprises permanent magnet 9, catalyst, zeolite, buffering packing layer 10(glass dregs), permanent magnet 9 in the vertical direction is spaced formation magnetic and helps layer, magnetic helps the magnet poles of arranged adjacent in layer different, catalyst and zeolite by volume 1 ︰ 2 ratio mixing after be filled between adjacent permanent 9, the magnetic that is of five storeys is set in magnetic co catalysis layer 8 and helps layer, buffering packing layer 10 is arranged on magnetic and helps interlayer (layer is identical with the pole orientation of the permanent magnet that interlayer is arranged), the magnetic direction that whole magnetic co catalysis layer 8 produces is parallel with airflow direction.
It is 30cm that catalytic reactor height is magnetized in gas-solid mutually, and diameter is 8cm, and cylindrical shell 7 outer setting has electric jacket to carry out heated constant temperature.During use, PH
3flue gas enters reactor by air inlet 1 with 1000mL/min flow velocity, the effect of thin mouth sieve plate 2 strengthens air stream turbulence, the design of triangle dividing plate 3 is to reduce the local return straight up and down caused by air inlet pipe, cause the problem of inside reactor distribution of gas inequality, gas enters the gas homogenization layer 6 on cylindrical shell top, can better realize even gas distribution, then gas carries out catalytic oxidation enrichment and obtains phosphate in magnetic co catalysis layer 8, and after purification, gas is discharged by gas outlet 13.
Reaction unit top cover of cylinder body flange 5, when cleaning and regeneration reactor, opens upper cover 4, carries out flushing catalyst or adds catalyst.Catalyst discharge port 11 be catalyst in reactor regeneration efficiency lower than 80% time, take out catalyst time open.The effect of liquid flowing outlet 15 is in catalyst regeneration process, passes in reactor by superheated steam from air inlet 1, and the soluble-salt adhered in solid catalyst surface rinses by steaming liquid, enters liquid phase, and liquid is discharged from liquid flowing outlet 15.
Meanwhile, be active carbon with adsorbent, by PH
3gas is passed into from air inlet 1 and does not arrange magnetic and help the reaction unit of layer, and measure object gas without magnetized change in concentration trend curve, multilevel iudge response difference, the results are shown in Table 1;
Table 1: have magnetic field and do not have magnetic field to PH
3the impact of detergent power
As can be seen from the above table: having the PH under the existent condition of magnetic field
3detectable concentration is low, illustrates when there being magnetic field, PH
3absorption property obviously strengthen, if according to detectable concentration: initial concentration >5% is calculated as active carbon and is penetrated, so result shows, without under magnetic field condition, active carbon penetrates after 7h, relatively, under having magnetic field condition, active carbon penetrates after 11h, shows that magnetic history can improve the adsorption capacity of catalyst to gas greatly.
embodiment 2:this magnetic helps gas-solid phase reaction to purify H
2s, PH
3the method of flue gas, 140 DEG C, under the existence condition of magnetic field, will containing (H
2s, PH
3) flue gas passes in the reactor that catalyst is housed the H in gas
2s pollutant carries out catalytic oxidation enrichment, wherein magnetic field intensity is 0.1T, described catalyst is that zeolite to be placed in the iron chloride of concentration 0.05mol/L and concentration be after the cobalt nitrate solution of 0.02mol/L floods 24h, and dry 10h inside 105 DEG C of drying boxes is obtained activate 4h at 250 DEG C after.
The gas-solid completing said method magnetizes catalytic reactor mutually for the structure shown in Fig. 2, it comprises triangle dividing plate 3, upper cover 4, cylindrical shell 7, magnetic co catalysis layer 8, upper cover 4 is arranged on cylindrical shell 7 by flange 5, cylindrical shell 7 top is provided with air inlet 1, air inlet 1 lower end is provided with pore sieve plate 2, triangle dividing plate 3 is provided with below pore sieve plate 2, cylindrical shell 7 top is provided with top homogenizing layer 6, top homogenizing layer 6 volume: magnetic co catalysis layer 8 volumes=1:12, cylindrical shell 7 bottom is provided with bottom homogenizing layer 14, magnetic co catalysis layer 8 is arranged between top homogenizing layer 6 and bottom homogenizing layer 14 by packing support plate 12, homogenizing layer 14 side, bottom has gas outlet 13, liquid flowing outlet 15 is provided with bottom bottom homogenizing layer 14, cylindrical shell 7 bottom is provided with catalyst discharge port 11, wherein magnetic co catalysis layer 8 comprises permanent magnet 9, catalyst, zeolite, buffering packing layer 10(glass dregs), permanent magnet 9 in the vertical direction is spaced formation magnetic and helps layer, magnetic helps the magnet poles of arranged adjacent in layer different, catalyst and zeolite by volume 1 ︰ 0.5 ratio mixing after be filled between adjacent permanent 9, be provided with 6 layers of magnetic in magnetic co catalysis layer and help layer, buffering packing layer 10 is arranged on magnetic and helps interlayer (layer is identical with the pole orientation of the permanent magnet that interlayer is arranged), the magnetic direction that whole magnetic co catalysis layer 8 produces is parallel with airflow direction, in magnetic co catalysis layer 8, mechanical vibrator framework 16 is set, external frequency regulation device, mechanical vibrator framework 16 be designed with two effects, one is the structure change in order to prevent adsorbent (catalyst) from causing because of local magnetized, two be in order to adsorbent (catalyst) regenerate time, promote adsorb (catalysis) impurity removal in solid phase microcellular structure.
It is 30cm that catalytic reactor height is magnetized in gas-solid mutually, and diameter is 8cm, during use, and H
2s flue gas enters reactor by air inlet 1 with 800mL/min flow velocity, and the effect of thin mouth sieve plate 2 strengthens air stream turbulence, and be provided with gas-heating apparatus below pore sieve plate 2, design temperature is 163 DEG C, and the inner set temperature detector of cylindrical shell 7, detected temperatures is 140 DEG C.The design of triangle dividing plate 3 is to reduce the local return straight up and down caused by air inlet pipe, cause the problem of inside reactor distribution of gas inequality, gas enters the gas homogenization layer 6 on cylindrical shell top, even gas distribution can better be realized, then gas carries out catalytic oxidation enrichment sulphur and phosphate in magnetic co catalysis layer 8, and after purification, gas is discharged by gas outlet 13.
After catalytic reaction completes, mechanical vibrator framework 16 rapping intensity adjusts to 100g, rapping time 1min, rapping stroke 30mm, rapping frequency 50 times/min.After rapping completes, reaction unit top cover of cylinder body flange 5, when cleaning and regeneration reactor, opens upper cover 4, carries out flushing catalyst or adds catalyst.Catalyst discharge port 11 be catalyst in reactor regeneration efficiency lower than 80% time, take out catalyst time open.The effect of liquid flowing outlet 15 is in catalyst regeneration process, is passed into by superheated steam in reactor, and the soluble-salt adhered in solid catalyst surface rinses by steaming liquid, enters liquid phase, and liquid is discharged from liquid flowing outlet 15.
Meanwhile, be active carbon with adsorbent, by PH
3gas is passed into from air inlet 1 and does not arrange magnetic and help the reaction unit of layer, and measure object gas without magnetized change in concentration trend curve, multilevel iudge response difference, the results are shown in Table 2 and table 3;
Table 2: have magnetic field and do not have magnetic field to H
2the impact of S detergent power
Table 3: have magnetic field and do not have magnetic field to PH
3the impact of detergent power
As can be seen from the above table: having magnetic field than the H not having magnetic field
2s, PH
3detectable concentration is low, illustrates when there being magnetic field, H
2s, PH
3absorption property obviously strengthen, if according to detectable concentration: initial concentration >5% is calculated as active carbon and is penetrated, so result shows, without under magnetic field condition, active carbon penetrates after 7 ~ 8h, relatively, under having magnetic field condition, active carbon penetrates after 11 ~ 14h, shows that magnetic history can improve gas absorption efficiency greatly.
embodiment 3:this magnetic helps gas-solid phase reaction to purify AsH
3the method of flue gas, 80 DEG C, under the existence condition of magnetic field, will containing AsH
3flue gas passes in the reactor that catalyst is housed the AsH in gas
3pollutant carries out catalytic oxidation enrichment, wherein magnetic field intensity is 1T, described catalyst is after acid permanganate soln alundum (Al2O3) being placed in concentration 0.1mol/L floods 24h, dry 10h inside 105 DEG C of drying boxes, then in the cerous nitrate solution of 0.05mol/L, 24h is flooded, dry 10h inside 105 DEG C of drying boxes, obtained after finally activating 4h at 300 DEG C.
The gas-solid completing said method magnetizes catalytic reactor structure mutually for the reactor shown in Fig. 3, it comprises triangle dividing plate 3, upper cover 4, cylindrical shell 7, magnetic co catalysis layer 8, power supply 20, cylindrical shell 7 top is provided with air inlet 1, air inlet 1 lower end is provided with pore sieve plate 2, triangle dividing plate 3 is provided with below pore sieve plate 2, cylindrical shell 7 top is provided with top homogenizing layer 6, top homogenizing layer 6 volume: magnetic co catalysis layer 8 volumes=1:10, cylindrical shell 7 bottom is provided with bottom homogenizing layer 14, magnetic co catalysis layer 8 is arranged between top homogenizing layer 6 and bottom homogenizing layer 14 by packing support plate 12, homogenizing layer 14 side, bottom has gas outlet 13, liquid flowing outlet 15 is provided with bottom bottom homogenizing layer 14, cylindrical shell 7 bottom is provided with catalyst discharge port 11, wherein magnetic co catalysis layer 8 comprises electromagnetic generator 18, electromagnetism fixed head 19, catalyst, electromagnetic generator 18 is arranged in the middle part of magnetic co catalysis layer 8 by electromagnetism fixed head 19, in electromagnetism fixed head 19, vertical direction carries out trisection, trisection point position arranges 2 electromagnetic generators 18, packed catalyst is in magnetic co catalysis layer 8, electromagnetic generator 18 is connected with power supply 20.
Reaction unit bed is 25cm, and diameter is 6cm, during use, AsH
3flue gas enters reactor by air inlet 1 with 600mL/min flow velocity, the effect of thin mouth sieve plate 2 strengthens air stream turbulence, the design of triangle dividing plate 3 is to reduce the local return straight up and down caused by air inlet pipe, cause the problem of inside reactor distribution of gas inequality, gas enters the gas homogenization layer 6 on cylindrical shell top, even gas distribution can better be realized, cylindrical shell 7 outer setting has electric jacket to carry out heated constant temperature, setting electric jacket temperature 90 DEG C, in bed body, temperature is 72 DEG C, then gas carries out catalytic oxidation enrichment and obtains arsenate in magnetic co catalysis layer 8, after purification, gas is discharged by gas outlet 13.
Reaction unit top cover of cylinder body flange 5, when cleaning and regeneration reactor, opens upper cover 4, carries out flushing catalyst or adds catalyst.Catalyst discharge port 11 be catalyst in reactor regeneration efficiency lower than 80% time, take out catalyst time open.The effect of liquid flowing outlet 15 is in catalyst regeneration process, passes in reactor by superheated steam from air inlet 1, and the soluble-salt adhered in solid catalyst surface rinses by steaming liquid, enters liquid phase, and liquid is discharged from liquid flowing outlet 15.
Be simultaneously adsorbent with active carbon, measure object gas when not being energized without magnetized change in concentration trend curve, multilevel iudge response difference, the results are shown in Table 4:
Table 4: have magnetic field and do not have magnetic field to AsH
3the impact of detergent power
As can be seen from the above table: having the PH under the existent condition of magnetic field
3detectable concentration is low, illustrates when there being magnetic field, AsH
3absorption property obviously strengthen, if according to detectable concentration: initial concentration >5% is calculated as active carbon and is penetrated, so result shows, without under magnetic field condition, active carbon penetrates after 7h, relatively, under having magnetic field condition, active carbon not yet penetrates after 24h, shows that magnetic history can improve gas absorption efficiency greatly.
embodiment 4:this magnetic helps gas-solid phase reaction to purify PH
3, H
2s, AsH
3, HCN flue gas method, 200 DEG C, under the existence condition of magnetic field, will containing PH
3, H
2s, AsH
3, HCN flue gas passes in the reactor that catalyst is housed the PH in gas
3, H
2s, AsH
3, HCN pollutant carries out catalytic oxidation enrichment, wherein magnetic field intensity is 10T, described catalyst is after nickel nitrate solution alundum (Al2O3) being placed in concentration 1mol/L floods 24h, dry 10h inside 105 DEG C of drying boxes, then in the lanthanum nitrate hexahydrate of 0.2mol/L, 24h is flooded, dry 10h inside 105 DEG C of drying boxes, obtained after finally activating 4h at 350 DEG C.
The gas-solid completing said method magnetizes catalytic reactor structure mutually for the reactor shown in Fig. 3, it comprises triangle dividing plate 3, upper cover 4, cylindrical shell 7, magnetic co catalysis layer 8, power supply 20, cylindrical shell 7 top is provided with air inlet 1, air inlet 1 lower end is provided with pore sieve plate 2, triangle dividing plate 3 is provided with below pore sieve plate 2, cylindrical shell 7 top is provided with top homogenizing layer 6, top homogenizing layer 6 volume: magnetic co catalysis layer 8 volumes=1:8, cylindrical shell 7 bottom is provided with bottom homogenizing layer 14, magnetic co catalysis layer 8 is arranged between top homogenizing layer 6 and bottom homogenizing layer 14 by packing support plate 12, homogenizing layer 14 side, bottom has gas outlet 13, liquid flowing outlet 15 is provided with bottom bottom homogenizing layer 14, cylindrical shell 7 bottom is provided with catalyst discharge port 11, wherein magnetic co catalysis layer 8 comprises electromagnetic generator 18, electromagnetism fixed head 19, catalyst, electromagnetic generator 18 is arranged in the middle part of magnetic co catalysis layer 8 by electromagnetism fixed head 19, in electromagnetism fixed head 19, vertical direction carries out five deciles, five Along ent positions arrange 4 electromagnetic generators 18, packed catalyst is in magnetic co catalysis layer 8, electromagnetic generator 18 is connected with power supply 20 and is regulated and controled by it, the magnetic direction that whole magnetic co catalysis layer 8 produces is parallel with airflow direction, arrange mechanical vibrator framework 16 in magnetic co catalysis layer 8, external frequency regulation device, rapping design parameter sets according to actual needs, mechanical vibrator framework 16 be designed with two effects, one is the structure change in order to prevent adsorbent (catalyst) from causing because of local magnetized, two be in order to adsorbent (catalyst) regenerate time, promote adsorb (catalysis) impurity removal in solid phase microcellular structure.
Reaction unit bed is 36cm, and diameter is 6cm.During use, mixed flue gas enters reactor by air inlet 1 with 1500mL/min flow velocity, and the effect of thin mouth sieve plate 2 strengthens air stream turbulence, gas-heating apparatus is provided with below pore sieve plate 2, design temperature is 221 DEG C, and the inner set temperature detector of cylindrical shell 7, detected temperatures is 200 DEG C.The design of triangle dividing plate 3 is to reduce the local return straight up and down caused by air inlet pipe, cause the problem of inside reactor distribution of gas inequality, gas enters the gas homogenization layer 6 on cylindrical shell top, even gas distribution can better be realized, then gas carries out catalytic oxidation enrichment and obtains catalysate in magnetic co catalysis layer 8, and after purification, gas is discharged by gas outlet 13.
After catalytic reaction completes, mechanical vibrator framework 16 rapping intensity adjusts to 200g, rapping time 2min, rapping stroke 50mm, rapping frequency 80 times/min.After rapping completes, reaction unit top cover of cylinder body flange 5, when cleaning and regeneration reactor, opens upper cover 4, carries out flushing catalyst or adds catalyst.Catalyst discharge port 11 be catalyst in reactor regeneration efficiency lower than 80% time, take out catalyst time open.The effect of liquid flowing outlet 15 is in catalyst regeneration process, passes in reactor by superheated steam from air inlet 1, and the soluble-salt adhered in solid catalyst surface rinses by steaming liquid, enters liquid phase, and liquid is discharged from liquid flowing outlet 15.
Be simultaneously adsorbent with active carbon, measure object gas when not being energized without magnetized change in concentration trend curve, multilevel iudge response difference, the results are shown in Figure 4;
As can be seen from above-mentioned Fig. 4: PH under the existence condition of magnetic field
3, HCN, AsH
3, H
2s detectable concentration is low, illustrates when there being magnetic field, PH
3, HCN, AsH
3, H
2catalytic and the absorption property of S are obviously strengthened, if according to detectable concentration: initial concentration >5% is calculated as active carbon and is penetrated, so result shows, without under magnetic field condition, active carbon penetrates after 7 ~ 9h, relatively, under having magnetic field condition, active carbon not yet obviously penetrates after 24h, shows that magnetic history can improve gas absorption efficiency greatly.
Claims (6)
1. magnetic helps a method for gas-solid phase reaction purifying smoke, it is characterized in that: 0 ~ 200 DEG C, under the existence condition of magnetic field, flue gas to be clean is passed in the reactor that catalyst is housed the AsH in gas
3, H
2s, HCN, PH
3in one or more pollutants carry out catalytic oxidation enrichment, wherein magnetic field intensity is 0.05 ~ 10T.
2. magnetic according to claim 1 helps the method for gas-solid phase reaction purifying smoke, it is characterized in that: catalyst is adopt conventional infusion process at the obtained unitary metal ion catalyst of one or both metal ions of supported on carriers or binary metal enhancement mode catalyst, wherein carrier is active carbon, molecular sieve, zeolite, one in alundum (Al2O3), unitary metal ion catalyst is the molysite of 0.01 ~ 1mol/L by concentration, mantoquita, after manganese salt or nickel salt impregnated carrier, dry activation is formed, binary metal enhancement mode catalyst is the cobalt salt of 0.01 ~ 1mol/L by unitary metal ion catalyst in concentration, obtained after impregnation drying in lanthanum salt or cerium salt.
3. the magnetic realized described in claim 1 or 2 helps the gas-solid of the method for gas-solid phase reaction purifying smoke to magnetize catalytic reactor mutually, it is characterized in that: comprise triangle dividing plate (3), upper cover (4), cylindrical shell (7), magnetic co catalysis layer (8), upper cover (4) is arranged on cylindrical shell (7) by flange (5), cylindrical shell (7) top is provided with air inlet (1), air inlet (1) lower end is provided with pore sieve plate (2), triangle dividing plate (3) is provided with in pore sieve plate (2) below, cylindrical shell (7) top is provided with top homogenizing layer (6), cylindrical shell (7) bottom is provided with bottom homogenizing layer (14), magnetic co catalysis layer (8) is arranged between top homogenizing layer (6) and bottom homogenizing layer (14) by packing support plate (12), homogenizing layer (14) side, bottom has gas outlet (13), bottom, bottom homogenizing layer (14) is provided with liquid flowing outlet (15), cylindrical shell (7) bottom is provided with catalyst discharge port (11), wherein magnetic co catalysis layer (8) comprises magnetic field generator (17) and catalyst, magnetic field generator (17) is arranged in the catalyst, and its magnetic direction produced is parallel with airflow direction, cylindrical shell (7) or pore sieve plate (2) are provided with heater.
4. gas-solid according to claim 3 magnetizes catalytic reactor mutually, it is characterized in that: magnetic field generator (17) is permanent magnet (9) or electromagnetic generator (18).
5. gas-solid according to claim 4 magnetizes catalytic reactor mutually, it is characterized in that: the ratio of catalyst and zeolite 1 ︰ 0.5-2 is by volume used in combination in magnetic co catalysis layer (8).
6. gas-solid according to claim 5 magnetizes catalytic reactor mutually, it is characterized in that: magnetic co catalysis layer (8) arranged outside mechanical vibrator framework (16), rapping intensity is 50-200g, rapping time 1-2min, rapping stroke 30-50mm, rapping frequency 20-80 time/min.
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