CN101757827A - Gas-solid phase reaction separation system and separation method thereof - Google Patents
Gas-solid phase reaction separation system and separation method thereof Download PDFInfo
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- CN101757827A CN101757827A CN201010105677A CN201010105677A CN101757827A CN 101757827 A CN101757827 A CN 101757827A CN 201010105677 A CN201010105677 A CN 201010105677A CN 201010105677 A CN201010105677 A CN 201010105677A CN 101757827 A CN101757827 A CN 101757827A
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- 238000003746 solid phase reaction Methods 0.000 title claims abstract description 19
- 239000007789 gas Substances 0.000 claims abstract description 91
- 239000012528 membrane Substances 0.000 claims abstract description 81
- 239000000428 dust Substances 0.000 claims abstract description 57
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 21
- 239000003546 flue gas Substances 0.000 claims abstract description 21
- 238000006243 chemical reaction Methods 0.000 claims abstract description 19
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- 239000012065 filter cake Substances 0.000 claims description 7
- 230000000717 retained effect Effects 0.000 claims description 7
- PNEYBMLMFCGWSK-UHFFFAOYSA-N Alumina Chemical compound [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 claims description 6
- 108091006146 Channels Proteins 0.000 claims description 6
- 229910045601 alloy Inorganic materials 0.000 claims description 5
- 239000000956 alloy Substances 0.000 claims description 5
- 238000012805 post-processing Methods 0.000 claims description 5
- MCMNRKCIXSYSNV-UHFFFAOYSA-N Zirconium dioxide Chemical compound O=[Zr]=O MCMNRKCIXSYSNV-UHFFFAOYSA-N 0.000 claims description 4
- 239000007769 metal material Substances 0.000 claims description 4
- 229910010271 silicon carbide Inorganic materials 0.000 claims description 3
- 229910015372 FeAl Inorganic materials 0.000 claims description 2
- 108090000862 Ion Channels Proteins 0.000 claims description 2
- 102000004310 Ion Channels Human genes 0.000 claims description 2
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- 238000010410 dusting Methods 0.000 claims description 2
- 239000011148 porous material Substances 0.000 claims description 2
- 230000015572 biosynthetic process Effects 0.000 claims 1
- 238000000034 method Methods 0.000 description 25
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- 239000003595 mist Substances 0.000 description 12
- 238000005516 engineering process Methods 0.000 description 11
- 239000003054 catalyst Substances 0.000 description 9
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 8
- 239000008246 gaseous mixture Substances 0.000 description 8
- 238000006555 catalytic reaction Methods 0.000 description 7
- 239000003245 coal Substances 0.000 description 6
- 238000002309 gasification Methods 0.000 description 6
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- 150000001367 organochlorosilanes Chemical class 0.000 description 4
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- 239000000126 substance Substances 0.000 description 4
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 3
- 238000002474 experimental method Methods 0.000 description 3
- 239000012530 fluid Substances 0.000 description 3
- 229910000041 hydrogen chloride Inorganic materials 0.000 description 3
- IXCSERBJSXMMFS-UHFFFAOYSA-N hydrogen chloride Substances Cl.Cl IXCSERBJSXMMFS-UHFFFAOYSA-N 0.000 description 3
- 238000004519 manufacturing process Methods 0.000 description 3
- 229910021420 polycrystalline silicon Inorganic materials 0.000 description 3
- 229920005591 polysilicon Polymers 0.000 description 3
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 description 2
- BZHJMEDXRYGGRV-UHFFFAOYSA-N Vinyl chloride Chemical group ClC=C BZHJMEDXRYGGRV-UHFFFAOYSA-N 0.000 description 2
- 230000004888 barrier function Effects 0.000 description 2
- 238000004140 cleaning Methods 0.000 description 2
- 239000002817 coal dust Substances 0.000 description 2
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- 125000001181 organosilyl group Chemical group [SiH3]* 0.000 description 2
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- 229910000838 Al alloy Inorganic materials 0.000 description 1
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- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical compound [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 description 1
- 239000005977 Ethylene Substances 0.000 description 1
- CWYNVVGOOAEACU-UHFFFAOYSA-N Fe2+ Chemical compound [Fe+2] CWYNVVGOOAEACU-UHFFFAOYSA-N 0.000 description 1
- BLRPTPMANUNPDV-UHFFFAOYSA-N Silane Chemical compound [SiH4] BLRPTPMANUNPDV-UHFFFAOYSA-N 0.000 description 1
- XUIMIQQOPSSXEZ-UHFFFAOYSA-N Silicon Chemical compound [Si] XUIMIQQOPSSXEZ-UHFFFAOYSA-N 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
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- 239000004568 cement Substances 0.000 description 1
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- 239000003795 chemical substances by application Substances 0.000 description 1
- NEHMKBQYUWJMIP-UHFFFAOYSA-N chloromethane Chemical class ClC NEHMKBQYUWJMIP-UHFFFAOYSA-N 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 229910052878 cordierite Inorganic materials 0.000 description 1
- 230000008021 deposition Effects 0.000 description 1
- JSKIRARMQDRGJZ-UHFFFAOYSA-N dimagnesium dioxido-bis[(1-oxido-3-oxo-2,4,6,8,9-pentaoxa-1,3-disila-5,7-dialuminabicyclo[3.3.1]nonan-7-yl)oxy]silane Chemical compound [Mg++].[Mg++].[O-][Si]([O-])(O[Al]1O[Al]2O[Si](=O)O[Si]([O-])(O1)O2)O[Al]1O[Al]2O[Si](=O)O[Si]([O-])(O1)O2 JSKIRARMQDRGJZ-UHFFFAOYSA-N 0.000 description 1
- 229910052571 earthenware Inorganic materials 0.000 description 1
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- 229910052751 metal Inorganic materials 0.000 description 1
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- 239000002086 nanomaterial Substances 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- RVTZCBVAJQQJTK-UHFFFAOYSA-N oxygen(2-);zirconium(4+) Chemical compound [O-2].[O-2].[Zr+4] RVTZCBVAJQQJTK-UHFFFAOYSA-N 0.000 description 1
- 239000000376 reactant Substances 0.000 description 1
- 230000035807 sensation Effects 0.000 description 1
- 229910000077 silane Inorganic materials 0.000 description 1
- 229910052710 silicon Inorganic materials 0.000 description 1
- 239000010703 silicon Substances 0.000 description 1
- 239000011949 solid catalyst Substances 0.000 description 1
- 238000001694 spray drying Methods 0.000 description 1
- ZDHXKXAHOVTTAH-UHFFFAOYSA-N trichlorosilane Chemical compound Cl[SiH](Cl)Cl ZDHXKXAHOVTTAH-UHFFFAOYSA-N 0.000 description 1
- 239000005052 trichlorosilane Substances 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
- 238000005200 wet scrubbing Methods 0.000 description 1
- 229910001928 zirconium oxide Inorganic materials 0.000 description 1
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- Filtering Of Dispersed Particles In Gases (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
The invention relates to a gas-solid phase reaction separation system and a separation method thereof. The separation method comprises the following steps that: high-temperature flue gas (a) enters an inorganic membrane cross flow filter (II), airflow makes the circular rotation movement from the upper part to the lower part along a rotation channel (5) in a filter (II), partial particles in the airflow are thrown to the filter wall by inertial centrifugal force and collected in a dust collecting chamber (7) at the bottom of the filter, and the gas enters a membrane component (3) from the bottom to the upper part along a central exhaust passage (6) and is subjected to gas-solid separation through the sieving action of an inorganic membrane; the purified clean gas (b) enters an after-treatment (A) section; concentrated dust gas (d) intercepted by the inorganic membrane filter enters a bag-type filter (III) for collecting solid dust; the gas permeating the cloth bag filter enters the after-treatment (A) section; and the dust (e) intercepted by the inorganic membrane filter (II) and the bag-type filter (III) returns to a reactor (I) to take part in reaction.
Description
Technical field
The present invention relates to a kind of gas-solid phase reaction separation system and separation method thereof, relate in particular to the piece-rate system and the separating technology of dust and gas in a kind of product of gas-solid phase reaction, be used for the gentle solid phase uncatalyzed reaction of gas-solid catalysis process process.
Background technology
Gas-solid separation is the separation of gaseous state heterodisperse system; be in the separation process, particularly high-temperature gas that in industries such as chemical industry, metallurgy, coal burning and gasification, cement, environmental protection, all will use solid particles to remove, reclaim be that industrial waste gas is handled, the key subjects of environmental protection always.The recovery of useful powder, the particularly recovery of high added value dust can be created very considerable economic.For example in the petrochemical plant fluid unit, reclaim catalyst, in air-flow conveying and spray-drying process, collect powder, nano material is produced, the collection of silica flour in organosilicon, the polysilicon production process, the recovery of powder etc. during the recovery of non-ferrous metal and other superfine powder are produced in the metallurgy industry.
The gas-solid phase reaction process is promptly reacted a kind of heterogeneous reaction process that has gas phase and solid phase in the system, comprises the gentle solid phase uncatalyzed reaction of gas-solid catalysis process process.The gas-solid catalysis process is the course of reaction of gaseous component under the solid catalyst effect, is a kind of course of reaction most widely used, largest in the chemical industry.According to statistics, about 90% catalytic reaction process is the gas-solid catalysis process.As organosilyl production, be that silica flour and chloromethanes are reacted the gaseous mixture that generates under the effect of catalyst copper powder be a kind of mixture, multiple silane gas and dust raw material are contained in the inside.In organosilyl production process, the dust in the gaseous mixture need be removed.
Gas-solid phase uncatalyzed reaction process, promptly the solid-phase reactant decomposes generates the reaction of gas-phase product, and as Coal Chemical Industry, coal dust and air gasifying agents such as (perhaps) oxygen gasification in reactor generates coal gas, contains pulverized coal particle in the mist.The coal-burning power plant need be with the particle removal in the mist, and the clean gas that obtains enters next step operation again, the present electrostatic precipitator that adopts, and equipment investment is big, the energy consumption height, the effect of dedusting does not still reach the level of ceramic membrane; The clean combustion new technology of coal---integrated gasification combination circulating generation (IGCC) route promptly needs to carry out the high-temperature gas powder filtering filtration after coal gasification reaction tower and desulfurizer.
As wet dust removal, electrostatic precipitation etc., all more or less there are some shortcomings in some present dust arresters.A kind of organochlorosilane wet dedusting and dry dedusting technology have been announced respectively among open CN1438226A of Chinese patent application and the CN101148453A, wet dedusting technology uses organochlorosilane as cleaning solution, contain 60% the organochlorosilane of having an appointment in the slurries of this method dedusting, the solid matter that extracts in the slurries is difficult, and the consumption of organochlorosilane is very big; The dry method eliminating method adopts extension candle formula ceramic element that the gaseous mixture that contains dust is carried out dedusting, this method is that terminal type filters, gather filter cake at face easily, cause flux to descend rapidly, filtration resistance increases, for keeping the problem that high frequency recoil that flux carries out causes existing in the commercial Application earthenware fracture.Cross-current type filters and has then overcome above-mentioned shortcoming, and its feedstock direction is parallel to face, and face is had good souring, can effectively reduce the filter cake deposition, significantly improves membrane flux, reduces the cleaning frequency (as the recoil frequency) of film.
Summary of the invention
The purpose of this invention is to provide that a kind of technology is simple, efficiency of dust collection is high, the gas-solid phase reaction separation system in the gas-solid phase reaction process of non-environmental-pollution, the present invention also has a purpose to provide a kind of gas-solid phase reaction separation method, this method uses novel inorganic film cross-flow filter and traditional bag filter in conjunction with realizing gas solid separation, simplify existing technology, to solve shortcomings such as wet dedusting complex process, washing process generation contaminated wastewater environment.
Technical scheme of the present invention: a kind of gas-solid phase reaction separation system is characterized in that this piece-rate system is made up of reactor, inoranic membrane cross-flow filter, cloth envelop collector, blower fan and compressor, and connects by the stainless steel pipeline; Wherein, the inoranic membrane cross-flow filter is made up of housing and membrane module, and the top of housing is provided with the high-temperature flue gas import, and the bottom is a back taper, and the bottom is provided with disposal box; The top of membrane module is provided with dense dirt chamber, the bottom is provided with exhaust passage, center fixed film filtering element; The upper end that dense dirt chamber is provided with dense dirt gas vent, membrane module is respectively equipped with clean gas outlet and purge gas import; It between housing and the membrane module gas rotating channel.
Wherein the film filtering element described in the inoranic membrane cross-flow filter is the tubular membrane that pottery or metal material constitute; The average pore size of film is 0.02 μ m～50 μ m; The diameter of membrane channels is 3-100mm.
The preferred aluminium oxide of ceramic material, zirconia, carborundum; The preferred stainless steel of metal material, FeAl alloy, FeCrAl alloy.
The present invention also provides a kind of gas-solid phase reaction separation method that utilizes above-mentioned gas-solid phase reaction separation system, and its concrete steps are as follows:
A) high-temperature flue gas that comes out in the reactor tangentially feeds the inoranic membrane cross-flow filter through the high-temperature flue gas import under the effect of centrifugal blower, air-flow is done the circumgyration campaign from top to bottom along rotating channel in the inoranic membrane cross-flow filter, particle in the air-flow is thrown to wall by centrifugal inertial force, and come together in the disposal box of filter conical lower portion, carry out one-time dedusting, gas then upwards enters membrane module from the bottom along the exhaust passage, sieving actoion by inoranic membrane realizes gas solid separation, carries out final dusting;
B) clean gas through the inoranic membrane cross-flow filter enters treatment and finishing section; The dense dirt gas that film is held back side escapes and enter from dense dirt gas vent and carries out third dedusting the bag filter, and the gas that sees through cloth envelop collector enters treatment and finishing section;
C) the dust Returning reactor that is retained down by inoranic membrane cross-flow filter and bag filter participates in reaction.
High-temperature flue gas is parallel to face among the preferred steps A, when high-temperature flue gas enters the inoranic membrane cross-flow filter, and control transmembrane pressure 0.01MPa-1.0Mpa; Face gas flow rate 1m/s-100m/s.
Above-mentioned inoranic membrane cross-flow filter is equipped with the purge gas import, when membrane flux drops to the 40-60% of initial flux, automatically adopt clean gas (b) the interval backflushing membrane separator of inorganic membrane filtration device outlet, to come off attached to the filter cake on the face, be deposited to the bottom of separator, thereby prevent that effectively film from polluting.
The present invention adopts conventional reactor, cloth envelop collector, blower fan and compressor.
The present invention is coupled in the separation process of gas-solid phase reaction process and dust in the same system, effectively the continuity of implementation procedure.The present invention is applicable to the Reaction Separation system in the gas-solid phase reaction process, as dedusting in the dust arrester in organic silicon technology, the coal gasification course, polysilicon tail gas handle and fluid bed catalytic reaction preparing chloroethylene flow process in the recovery etc. of catalyst.Inoranic membrane mechanical strength height, chemical stability is good, and is high temperature resistant, can effectively remove the dust in the gaseous mixture.
Beneficial effect:
(1) the present invention does not change original reaction condition on the technology basis of gas-solid phase reaction, novel inorganic film cross-flow filter is combined with bag filter purify dusty gas and reclaim useful powder, finishes gas solid separation in continuous flow procedure.
(2) technology of the present invention is simple, and the temperature of recoil gas is suitable with the temperature of filtration system, and when being applied in the separation of High Temperature Gas solid phase reaction, purge gas does not need other heating.
(3) the present invention does not have the wet scrubbing dust removal step, and the water for industrial use requirement is few, non-wastewater discharge, and environmental pollution is little.
(4) the present invention is used for the design of inorganic membrane filtration device with the principle of cyclone separator, be provided with bag filter and carry out dust collection after the inoranic membrane cross-flow filter, so the present invention is to dust clearance height, and separative efficiency surpasses 99.8%.
Description of drawings
Fig. 1 is the flow chart of dust separation technology in the gas-solid phase reaction process of the present invention;
Wherein I-reactor, II-inoranic membrane cross-flow filter, III-cloth envelop collector, IV-blower fan, V-compressor; The A-post processing;
Fig. 2 is an inoranic membrane cross-flow filter structural representation of the present invention;
Wherein 1-high-temperature flue gas import, 2-housing, 3-membrane module, 4-film filtering element, 5-rotating channel, 6-exhaust passage, 7-disposal box, the outlet of 8-clean gas, the dense dirt gas vent of 9-, the dense dirt of 10-chamber, the import of 11-purge gas;
Fig. 3 is the vertical view of inoranic membrane cross-flow filter of the present invention.
The specific embodiment
Embodiment 1: the biomass fermentation electric dust removing system
The present invention will be described in detail below in conjunction with accompanying drawing:
A) whole system is made up of gasifier, inoranic membrane cross-flow filter, cloth envelop collector, blower fan and compressor, gasifier, inoranic membrane cross-flow filter are stainless steel, the inoranic membrane cross-flow filter is provided with high-temperature flue gas import 1, clean gas outlet 8, dense dirt gas vent 9 and purge gas import 11; The gasifier outlet is provided with blower fan, and is connected to high-temperature flue gas import 1 through the stainless steel pipeline; Clean gas outlet 8 is connected to treatment and finishing section through the stainless steel pipeline, connects a mouth on the pipeline and is connected to purge gas import 11 through the stainless steel pipeline through compressor; Dense dirt gas vent 9 is connected to cloth envelop collector through the stainless steel pipeline; The cloth envelop collector outlet is connected to treatment and finishing section through the stainless steel pipeline; The membrane filtration original paper adopts a root hole directly to be the carborundum chimney filter of 20um, single tube, internal diameter 40mm, external diameter 60mm;
B) from the gas that gasifier comes out, contain particle, tar, NO
x, CO
2, the high-temperature flue gas in gasifier exit (a) enters in the inoranic membrane cross-flow filter (II) under centrifugal fan (IV) effect and separates, cross-flow velocity 18m/s, and transmembrane pressure 0.03MPa, feed side dust content are 3.9686g/m
3, filtering the initial moment, film pipe flux is 43.6m
3/ m
2H,, dense dirt gas (d) feeds bag filter (III) under the effect of blower fan (IV), and the mixed total dust content of gas that sees through inoranic membrane cross-flow filter (II) and cloth envelop collector (III) is 3.6mg/m
3
As Fig. 2, shown in 3, the high-temperature flue gas (a) in gasifier (I) exit tangentially enters inoranic membrane cross-flow filter (II) through high-temperature flue gas import 1 under the effect of centrifugal blower (IV), air-flow is done gyration from top to bottom along rotating channel 5, in turning course, dust moves to filter bottom along wall at the acting in conjunction lower edge of downward air-flow and gravity filter wall and enters disposal box 7, dusty gas is in process film filtering element 4 is upwards flowed in exhaust passage 6, clean gas (b) direction that sees through inoranic membrane cross-flow filter (II) perpendicular to former mixed airflow to, discharge through clean gas outlet 8.The dense dirt gas of holding back (d) that is rich in dust enters into cloth envelop collector (III) then through dense dirt gas vent 9 discharge filters.When inoranic membrane cross-flow filter (II) flux significantly is reduced to setting value 17.5m
3/ m
2During h, backpurge system starts automatically, carries out back flush through 11 pairs of diffusion barriers of purge gas import, and filter cake is come off, and is deposited to the bottom of separator and discharges filter residue automatically, and filter residue enters disposal box 7;
B) clean gas (b) that flows out from inoranic membrane cross-flow filter (II) and the gas that sees through bag filter (III) enter post processing (A) workshop section together;
C) dust (e) that is retained down by inorganic membrane filtration device (II) and bag filter (III) returns fluidized-bed reactor (I) and participates in reaction.
In the time of recoil, recoil time 3s, recoil pressure 0.2MPa.Present embodiment reaches 99.91% to the clearance of dust in the mist.
Embodiment 2: the organosilicon dust arrester
The present invention will be described in detail below in conjunction with accompanying drawing:
A) high-temperature flue gas (a) enters in the inoranic membrane cross-flow filter (II) under centrifugal fan (IV) effect and separates, adopting a root hole directly is the zirconium oxide film of 0.2 μ m, 19 passages, passage internal diameter 6mm, cross-flow velocity 30m/s, transmembrane pressure 0.1MPa, feed side gas dust content is 0.9308g/m
3, filtering the initial moment, film pipe flux is 51.5m
3/ m
2H,, the gaseous mixture that contains dense dirt feeds bag filter (III) under the effect of blower fan, and the mixed total dust content of gas that sees through inoranic membrane cross-flow filter (II) and cloth envelop collector (III) is 1.1mg/m
3
As shown in Figure 2, the high-temperature flue gas (a) in fluidized-bed reactor (I) exit tangentially enters inoranic membrane cross-flow filter (II) through high-temperature flue gas import 1 under the effect of centrifugal blower (IV), air-flow is done gyration from top to bottom, in turning course, dust moves to filter bottom along wall at the acting in conjunction lower edge of downward air-flow and gravity filter wall and enters disposal box 7, dusty gas is in process film filtering element 4 is upwards flowed in exhaust passage 6, clean gas (b) direction that sees through the inoranic membrane cross-flow filter perpendicular to former mixed airflow to, discharge through clean gas outlet 8.The dense cloud of dust gas of holding back (d) that is rich in dust enters into bag filter (III) then through dense dirt gas vent 9 discharge filters.When inoranic membrane cross-flow filter (II) flux significantly is reduced to setting value 20.6m
3/ m
2During h, backpurge system starts automatically, carries out back flush through 11 pairs of diffusion barriers of purge gas import, and filter cake is come off, and is deposited to the bottom of separator.Can discharge filter residue automatically when the filter cake amount runs up to a certain degree, filter residue enters disposal box 7;
B) clean gas (b) that flows out from inoranic membrane cross-flow filter (II) and the gas that sees through bag filter enter post processing (A) workshop section together;
C) dust (e) that is retained down by inorganic membrane filtration device (II) and bag filter (III) returns fluidized-bed reactor and participates in reaction.
In the time of recoil, recoil time 3s, recoil pressure 0.2MPa.Present embodiment reaches 99.89% to the clearance of dust in the mist.
Embodiment 3: the coal gasification dedusting
Coal dust and air gasify in reactor and generate coal gas; During the normal running, high-temperature flue gas tangentially feeds the inoranic membrane cross-flow filter under the effect of centrifugal blower, air-flow is done gyration from top to bottom, in turning course, dust moves to filter bottom along wall at the acting in conjunction lower edge of downward air-flow and gravity filter wall and gathers dust, dusty gas upwards flows through ceramic filter tube from the bottom of filter, a part of dust capture to be removed by inoranic membrane in the gaseous mixture, and inoranic membrane is crossed dense dirt gas that flow filter holds back and entered bag filter and carry out the terminal dedusting; Adopting four root holes directly is the porous Fe Al alloy symmetric membrane of 10 μ m, single tube, and internal diameter 50mm, cross-flow velocity 25m/s, transmembrane pressure 0.07MPa, feed side dust content are 7.9357g/m
3, the mixed total dust content of gas that sees through inoranic membrane cross-flow filter and cloth envelop collector is 5.6mg/m
3Purge gas that flows out from the inoranic membrane cross-flow filter and the gas that sees through bag filter enter treatment and finishing section together; Dust by inorganic membrane filtration device and bag filter are retained down after handling again, returns fluidized-bed reactor and participates in reaction.Experiment is carried out 20h and be need not film is recoiled.Present embodiment reaches 99.93% to the clearance of dust in the mist.
Embodiment 4: polysilicon tail gas is handled
Silica flour and hydrogen chloride enter fluidized-bed reactor, under the catalytic action of catalyst, and the generation mist that reacts, mist is made up of trichlorosilane, hydrogen chloride and silica flour; Mist tangentially feeds the inoranic membrane cross-flow filter under the effect of centrifugal blower, air-flow is done gyration from top to bottom, in turning course, dust moves to filter bottom along wall at the acting in conjunction lower edge of downward air-flow and gravity filter wall and gathers dust, dusty gas upwards flows through ceramic filter tube from the bottom of filter, a part of dust capture to be removed by inoranic membrane in the gaseous mixture, and inoranic membrane is crossed dense dirt gas that flow filter holds back and entered bag filter and carry out the terminal dedusting; Adopting six roots of sensation aperture is the FeCrAl alloy symmetric membrane of 5 μ m, single tube, and internal diameter 50mm, cross-flow velocity 15m/s, transmembrane pressure 0.04MPa, feed side dust content are 4.3856g/m
3, the mixed total dust content of gas that sees through inoranic membrane cross-flow filter and cloth envelop collector is 4.3mg/m
3, Purge gas that flows out from the inoranic membrane cross-flow filter and the gas that sees through bag filter enter treatment and finishing section together; Dust by inorganic membrane filtration device and bag filter are retained down after handling again, returns fluidized-bed reactor and participates in reaction.Experiment is carried out 20h and be need not film is recoiled.Present embodiment reaches 99.90% to the clearance of dust in the mist.
Embodiment 5: the recovery of catalyst in the fluid bed catalytic reaction preparing chloroethylene flow process
When carrying out ethylene oxychlorination in the fluidized-bed reactor, adopt finely grained catalyst, raw material ethene, hydrogen chloride and air enter reactor by the bottom respectively, after fully mixing, feed catalyst layer, make catalyst be in fluidized state.The mist that reaction generates is the mixture of multiple gases and catalyst granules; Mist tangentially feeds the inoranic membrane cross-flow filter under the effect of centrifugal blower, air-flow is done gyration from top to bottom, in turning course, dust moves to filter bottom along wall at the acting in conjunction lower edge of downward air-flow and gravity filter wall and gathers dust, dusty gas upwards flows through ceramic filter tube from the bottom of filter, a part of dust capture to be removed by inoranic membrane in the gaseous mixture, and inoranic membrane is crossed dense dirt gas that flow filter holds back and entered bag filter and carry out the terminal dedusting; Adopting a root hole directly is the cordierite chimney filter of 30 μ m, single tube, and internal diameter 40mm, cross-flow velocity 22m/s, transmembrane pressure 0.02MPa, feed side dust content are 3.4892g/m
3, the mixed total dust content of gas that sees through inoranic membrane cross-flow filter and cloth envelop collector is 2.3mg/m
3, Purge gas that flows out from the inoranic membrane cross-flow filter and the gas that sees through bag filter enter treatment and finishing section together; Dust by inorganic membrane filtration device and bag filter are retained down after handling again, returns fluidized-bed reactor and participates in reaction.Experiment is carried out 30h and be need not film is recoiled.Present embodiment reaches 99.93% to the clearance of dust in the mist.
Claims (6)
1. gas-solid phase reaction separation system is characterized in that this piece-rate system is made up of reactor (I), inoranic membrane cross-flow filter (II), cloth envelop collector (III), blower fan (IV) and compressor (V), and connects by the stainless steel pipeline; Wherein, inoranic membrane cross-flow filter (II) is made up of housing (2) and membrane module (3), and the top of housing (2) is provided with high-temperature flue gas import (1), and the bottom is a back taper, and the bottom is provided with disposal box (7); The top of membrane module (3) is provided with dense dirt chamber (10), the bottom is provided with exhaust passage (6), center fixed film filtering element (4); The upper end that dense dirt chamber (10) is provided with dense dirt gas vent (9), membrane module is respectively equipped with clean gas outlet (8) and purge gas import (11); Be gas rotating channel (5) between housing (2) and the membrane module (3).
2. piece-rate system according to claim 1 is characterized in that the tubular membrane of the film filtering element (4) described in the inoranic membrane cross-flow filter (II) for pottery or metal material formation; The average pore size of film is 0.02 μ m～50 μ m; The diameter of membrane channels is 3-100mm.
3. piece-rate system according to claim 1 is characterized in that described ceramic material is aluminium oxide, zirconia or carborundum; Metal material is stainless steel, FeAl alloy or FeCrAl alloy.
4. gas-solid phase reaction separation method, its concrete steps are as follows:
A) high-temperature flue gas (a) that comes out in the reactor (I) tangentially feeds inoranic membrane cross-flow filter (II) through high-temperature flue gas import (1) under the effect of centrifugal blower (IV), air-flow is done the circumgyration campaign from top to bottom along rotating channel (5) in inoranic membrane cross-flow filter (II), particle in the air-flow is thrown to wall by centrifugal inertial force, and come together in the disposal box (7) of filter conical lower portion, carry out one-time dedusting, then (6) upwards enter membrane module (3) to gas from the bottom along the exhaust passage, sieving actoion by inoranic membrane realizes gas solid separation, carries out final dusting;
B) clean gas (b) through inoranic membrane cross-flow filter (II) enters post processing (A) workshop section; The dense dirt gas (d) that film is held back side escapes and enter the bag filter (III) from dense dirt gas vent (9) and carries out third dedusting, and the gas that sees through cloth envelop collector (III) enters post processing (A) workshop section;
C) dust (e) Returning reactor (I) that is retained down by inoranic membrane cross-flow filter (II) and bag filter (III) participates in reaction.
5. separation method according to claim 4 is characterized in that high-temperature flue gas in the steps A (a) is parallel to face, when high-temperature flue gas (a) enters the inoranic membrane cross-flow filter, and control transmembrane pressure 0.01MPa-1.0Mpa; Face gas flow rate 1m/s-100m/s.
6. separation method according to claim 4, it is characterized in that the inoranic membrane cross-flow filter is equipped with purge gas import (11), when membrane flux drops to the 40-60% of initial flux, automatically adopt clean gas (b) the interval backflushing membrane separator of inorganic membrane filtration device outlet, to come off attached to the filter cake on the face, be deposited to the bottom of separator, thereby prevent that effectively film from polluting.
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