CN106237751B - Particle bed dust removal catalytic unit - Google Patents

Particle bed dust removal catalytic unit Download PDF

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CN106237751B
CN106237751B CN201610752065.0A CN201610752065A CN106237751B CN 106237751 B CN106237751 B CN 106237751B CN 201610752065 A CN201610752065 A CN 201610752065A CN 106237751 B CN106237751 B CN 106237751B
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catalyst
dust
layer
gas
particle
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CN106237751A (en
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杨国华
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Ningbo University
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Ningbo University
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D46/00—Filters or filtering processes specially modified for separating dispersed particles from gases or vapours
    • B01D46/56—Filters or filtering processes specially modified for separating dispersed particles from gases or vapours with multiple filtering elements, characterised by their mutual disposition
    • B01D46/62—Filters or filtering processes specially modified for separating dispersed particles from gases or vapours with multiple filtering elements, characterised by their mutual disposition connected in series
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D46/00—Filters or filtering processes specially modified for separating dispersed particles from gases or vapours
    • B01D46/30—Particle separators, e.g. dust precipitators, using loose filtering material
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/86—Catalytic processes
    • B01D53/8621—Removing nitrogen compounds
    • B01D53/8625—Nitrogen oxides
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/86—Catalytic processes
    • B01D53/8678—Removing components of undefined structure
    • B01D53/8687—Organic components
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/70—Organic compounds not provided for in groups B01D2257/00 - B01D2257/602
    • B01D2257/708—Volatile organic compounds V.O.C.'s
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2258/00—Sources of waste gases
    • B01D2258/02—Other waste gases
    • B01D2258/0283—Flue gases
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2267/00—Multiple filter elements specially adapted for separating dispersed particles from gases or vapours
    • B01D2267/30—Same type of filters

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  • Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Environmental & Geological Engineering (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Health & Medical Sciences (AREA)
  • Biomedical Technology (AREA)
  • Analytical Chemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Filtering Of Dispersed Particles In Gases (AREA)
  • Exhaust Gas Treatment By Means Of Catalyst (AREA)

Abstract

The invention discloses a particle bed dust removal catalytic device, which comprises an outer shell and at least one layer of particle bed filtering catalytic device arranged in an inner cavity of the outer shell along the vertical direction, wherein the upper part of the outer shell is provided with a dust-containing gas inlet, the lower part of the outer shell is provided with a dust discharge port, each layer of particle bed filtering catalytic device comprises at least one filtering catalytic unit, each filtering catalytic unit is provided with a dust-containing gas vent and a gas purifying vent, and each filtering catalytic unit consists of a dust-containing gas chamber, an upper particle filtering layer, a lower particle filtering layer, a current stabilizing layer, a catalyst layer and a gas purifying chamber which are sequentially arranged from top to bottom; has the advantages that on the premise of not changing the reasonable structure of the existing granular bed dust remover, the low-resistance high-activity monolithic catalyst can be adopted to remove tar gas or organic waste gas or NO under the catalysis of effective dust removalxAnd the like.

Description

Particle bed dust removal catalytic unit
Technical Field
The invention relates to a dust removal catalysis technology, in particular to a particle bed dust removal catalysis device.
Background
Some coal gas or flue gas not only needs to remove dust, but also needs to remove some harmful gases, such as tar gas in hot coal gas, organic waste gas (VOC) in industrial waste gas, and NO in flue gasxEtc. it is technically feasible and economically reasonable to remove dust and harmful gases simultaneously in one device using a high-temperature dust removal technique. The granular bed filter dust remover adopts a high-temperature resistant granular filter material, and has unique advantages in the field of high-temperature gas dust removal.
The invention patent "a kind of particle bed filters the dust catcher" (publication number is CN101036846A, patent number is ZL200710067109.7), it discloses a kind of particle bed filters the dust catcher, including the outer casing and at least one deck of filter equipment set up in the outer casing along the direction of height, the upper portion of the outer casing has dust-laden gas inlet, the bottom end of the outer casing has dust outlets, the filter equipment has independent gas reversing devices, connect with clean gas manifold and blowback gas manifold on the gas reversing device, the characteristic is that the filter equipment includes at least one filter unit, the filter unit includes the inner casing, there are air vent and breather pipe on the inner casing, there are granulometric layer and air distribution plate in the inner casing, the air vent is set up above the granulometric layer, the breather pipe is set up below the granulometric layer, the breather pipe is crossed the outer casing and connected with gas; the advantage is when filtering and removing dust, and the inner shell body is surrounded by the hot gas stream, and each part of inner shell body expends with heat and contracts with cold evenly, and anti thermal deformation performance is good, makes this dust remover can be used to high temperature and the changeable occasion of temperature, and temperature strong adaptability, application scope is wide. When the filtering device in the particle bed filtering dust remover comprises a plurality of filtering units which are arranged in parallel, the continuous filtering of gas can be realized, the dust removing effect is better, but the particle bed filtering dust remover can only effectively remove dust, and harmful gas can not be removed.
As another example, the invention of the chinese publication "granular bed gas purification device and method" (publication No. CN1647847A, patent No. ZL200410084485.3) discloses a granular bed gas purification device and method, comprising a housing, an air distributor disposed in the housing, and a granular bed disposed on the air distributor, wherein the granular bed is composed of at least two layers of filter materials, the particle size of each layer of filter material decreases from top to bottom in layers, the particle density of each layer of filter material increases from top to bottom in layers, and the particle density of the upper layer of filter material is smaller than the bed density formed when the adjacent lower layer of filter material is normally fluidized, and the filter materials of the layers also have a common normal fluidization and immiscible gas velocity range; the device has the advantages that when the device is used for dedusting, the filtering materials on each layer at the upper part are subjected to coarse dedusting, and the filtering materials on the lowest layer are subjected to fine dedusting, namely, the coarse and fine filtering are integrated; when back-blowing is used for removing ash, the filtering materials in each layer are normally fluidized and are not mutually mixed, so that the dust holding capacity of the bed layer can be improved, the filtering efficiency can be improved, and the ash removal is simple. The device considers the material leakage of the lowest layer filter material and the blockage of the air distributor when in use, a flow stabilizing layer which is always in a static state is also laid in the shell between the lowest layer filter material and the air distributor, any one or more layers of all the filter material layers and the flow stabilizing layer have the function of removing harmful gases such as sulfur or chlorine in dust-containing gas, can remove dust and harmful gases such as sulfur or chlorine at the same time, but cannot remove tar gas, organic waste gas or NO at the same timexAnd the like, which require harmful gases to be removed by catalytic reactions.
Like the utility model of the particle layer dust removal and denitration integrated device (with the publication number of CN205287928U and the patent number of ZL201521088838.7) announced in China, the utility model discloses a particle layer dust removal and denitration integrated deviceThe dust collector comprises a shell and a particle layer dust collector, wherein the upper end of the shell is provided with an air inlet, and the lower end of the shell is provided with an ash deposition hopper; a plurality of particle layer dust collectors fixed on the inner wall of the shell are arranged in the shell, and a steady flow catalyst layer, a heavy particle layer and a light particle layer are sequentially arranged on the upper end surface of each particle layer dust collector from bottom to top; the outer wall of the shell is provided with air outlets communicated with the corresponding particle layer dust remover, each air outlet is communicated with a pipeline three and a pipeline four, the pipeline three is provided with a valve one, and the pipeline four is provided with a valve two; the advantage is through in the middle of integrating a casing with granular layer dust remover and denitration, not only remove dust, the denitration is effectual, still can practice thrift many land usable floor areas, and dust removal denitration treatment cost reduces. The device also discloses that the steady flow catalyst layer is ceramic particles with the diameter of 5-20 mm, and the surface of the steady flow catalyst layer is sprayed with V2O5The denitration catalyst comprises metal oxide, a heavy particle layer of 0.5-0.8 mm ceramic particles and a light particle layer of 2-4 mm ceramic particles, and is prepared by spraying denitration catalyst (V) on the surfaces of the ceramic particles in a steady flow catalyst layer2O5Metal oxide) is denitrated while dedusting, but the problems are that the specific surface area of the denitration catalyst sprayed on the surface of the ceramic particles in the steady flow catalyst layer is small, the catalytic activity is low, and if higher denitration efficiency is obtained, the thickness and the pressure drop of the steady flow catalyst layer are increased by times and tens of times, so that the technology is unreasonable in economy.
Therefore, how to adopt the low-resistance high-activity catalyst, not change the reasonable structure of the existing granular bed dust remover, and realize the integration of dust removal and catalytic purification is the problem to be solved.
Disclosure of Invention
The invention aims to solve the technical problem of providing a method for removing tar gas or organic waste gas or NO by catalyzing and removing low-resistance high-activity monolithic catalyst while effectively removing dust on the premise of not changing the reasonable structure of the existing particle bed dust removerxAnd the like, and the dust removal and catalysis device of the particle bed.
The technical scheme adopted by the invention for solving the technical problems is as follows: the utility model provides a granule bed dust removal catalytic unit, include the shell body and along vertical direction set up in the inner chamber of shell body in at least one deck granule bed filter catalyst ware, the upper portion of shell body be provided with the dust-laden gas import of upper reaches intake pipe intercommunication, the lower part of shell body be provided with the dust discharge port, every layer granule bed filter catalyst ware include at least one filtration catalytic unit, every filtration catalytic unit have dust-laden gas vent and clean gas vent, its characterized in that: the filtering and catalyzing unit consists of a dust-containing gas chamber, an upper particle filtering layer for performing coarse filtering and dust removal on dust-containing gas from the dust-containing gas chamber, a lower particle filtering layer for performing fine filtering and dust removal on the dust-containing gas from the upper particle filtering layer, a flow stabilizing layer capable of uniformly distributing air, a catalyst layer for removing harmful gas in the gas from the flow stabilizing layer by adopting a low-resistance high-activity monolithic catalyst, and a gas purifying chamber, wherein the dust-containing gas vent is arranged on the dust-containing gas chamber, and the gas purifying vent is arranged on the gas purifying chamber; the dust-containing gas enters the inner cavity of the outer shell through the dust-containing gas inlet, the dust-containing gas in the inner cavity of the outer shell enters the dust-containing gas chamber through the dust-containing gas vent, the dust-containing gas in the dust-containing gas chamber sequentially passes through the coarse filtration dust removal of the upper particle filter layer and the fine filtration dust removal of the lower particle filter layer, the obtained gas enters the catalyst layer after passing through the flow stabilizing layer, the purified gas obtained after harmful gas in the gas is removed through the catalyst layer enters the purified gas chamber, the purified gas in the purified gas chamber is output through the purified gas vent, and the dust settled on the lower portion of the outer shell is discharged through the dust discharge port.
The catalyst layer comprises porous support piece and grid that set gradually from bottom to top porous support piece's support down every grid of grid in pack and be equipped with low resistance high activity monolithic catalyst, low resistance high activity monolithic catalyst be honeycomb catalyst or foamed ceramic catalyst, porous support piece set up in the top of air-purifying chamber, the grid set up in the below of stationary flow layer. The grid and the porous support piece are arranged below the flow stabilizing layer, so that the flow stabilizing layer and the lower particle filtering layer and the upper particle filtering layer above the flow stabilizing layer are supported by the grid; supporting the honeycomb catalyst or the foamed ceramic catalyst filled in each grid of the grid through a porous supporting piece, and pre-distributing the back-blowing airflow; the honeycomb catalyst or the foamed ceramic catalyst filled in each grid of the grid can effectively remove harmful gas, the honeycomb catalyst with high pore density is adopted to make the structure more compact, and the mechanical strength of the foamed ceramic catalyst is higher; the honeycomb catalyst or the ceramic foam catalyst is a monolithic catalyst filled in each grid of the grid, has high activity, is compact in structure, can obtain high catalytic efficiency at high space velocity, and is far superior to a granular catalyst with active components sprayed on the surfaces of granules.
The porous supporting piece is a grating plate or a grid plate or a screen. The porous support member can also be other existing plate members with multiple pores, and is used for supporting honeycomb catalysts or ceramic foam catalysts filled in each grid of the grid on one hand, and can be used for carrying out airflow pre-distribution through the small pores of the porous support member during back flushing and ash removal on the other hand, so that the back flushing air velocity among all grids of the grid is self-regulated, and the local over-high air velocity, the local perforation of the upper particle filter layer and the lower particle filter layer and the abnormal fluidization are effectively prevented.
The honeycomb catalyst is made of TiO2NO as carrier with V-W as main active componentxA reduction catalyst (SCR); or the honeycomb catalyst is made of gamma-Al2O3An organic exhaust gas oxidation catalyst which is used as a carrier and takes noble metals platinum and palladium as main active components; or the honeycomb catalyst is made of Al2O3The tar cracking catalyst is used as a carrier and takes nickel as a main active component. Here, NO is usedxThe reduction catalyst can effectively remove NO in dust-containing gasx(ii) a The organic waste gas in the dust-containing gas can be effectively removed by adopting the organic waste gas oxidation catalyst; the tar cracking catalyst can effectively remove tar gas in the dust-containing gas.
The foamed ceramic catalyst is prepared by using 30-100 ppi foamed ceramic as a base material and TiO2Monolithic NO as carrier with V-W as main active componentxReduction catalyst(SCR); or the foamed ceramic catalyst is prepared by using 30-100 ppi foamed ceramic as a base material and gamma-Al2O3An integral organic waste gas oxidation catalyst which is used as a carrier and takes noble metals platinum and palladium as main active components; or the foamed ceramic catalyst is prepared by using 30-100 ppi foamed ceramic as a base material and Al2O3An integral tar cracking catalyst with nickel as main active component as carrier. Here, monolithic NO is usedxThe reduction catalyst can effectively remove NO in dust-containing gasx(ii) a The organic waste gas in the dust-containing gas can be effectively removed by adopting the integral organic waste gas oxidation catalyst; the tar gas in the dust-containing gas can be effectively removed by adopting the integral tar cracking catalyst.
Every layer granule bed filter catalyst ware include two filter catalytic unit, filter catalytic unit symmetrical arrangement in the both sides of the inner chamber of shell body, symmetrical arrangement two filter catalytic unit relative one side between the space with dust-containing gas vent intercommunication. The filtering and catalyzing units on the same layer are oppositely and symmetrically arranged, so that the back blowing gas generated when one filtering and catalyzing unit on the lowest layer performs back blowing and ash removal can be more easily received by the filtering and catalyzing units on the same layer, the back blowing gas cannot flow upwards in a reverse mode to prevent dust from settling, and an air suction opening arranged at the lower portion of the outer shell for forcibly sucking the back blowing gas to flow downwards can be omitted.
The steady flow layer comprises an upper slotted screen, a particle layer and a lower slotted screen which are sequentially arranged from top to bottom, the upper slotted screen and the lower slotted screen clamp the particle layer, and the slot clearance between the upper slotted screen and the lower slotted screen is smaller than the particle size of the particles adopted by the particle layer. The particle layer clamped by the upper slotted screen and the lower slotted screen cannot be overturned at any air speed (including local high air speed when abnormal occurs), so that the particle layer is always stable and disordered, the uniform air distribution of the steady flow layer is effectively ensured, dust-containing air from top to bottom flows through the upper particle filter layer and the lower particle filter layer uniformly during filtering, and particularly, the lower particle filter layer and the upper particle filter layer can be fluidized by back flushing air from bottom to top during back flushing for ash removal; in order to ensure that the upper and lower slotted screens can clamp the particle layer, the gap between the slots of the upper and lower slotted screens is required to be smaller than the particle size of the particles used in the particle layer.
The particle size of the particles adopted in the upper particle filtering layer is larger than that of the particles adopted in the lower particle filtering layer, and the density of the particles in the upper particle filtering layer is smaller than that of the particles in the lower particle filtering layer. The particle size of the particles adopted in the upper particle filtering layer is required to be larger than that of the particles adopted in the lower particle filtering layer, and the density of the particles in the upper particle filtering layer is required to be smaller than that of the particles in the lower particle filtering layer, so that the dust-containing gas can be coarsely filtered and then finely filtered, the filtering and dust removing effects are better, and the lower particle filtering layer and the upper particle filtering layer are not mixed with each other after back flushing and dust removing.
The air purification vent is connected with an air purification vent pipe, the air purification vent pipe extends out of the outer shell and is respectively connected with an air purification branch pipe and a back flushing branch pipe through a switching valve; when the filtering catalytic unit filters, the purified gas vent pipe is communicated with the purified gas branch pipe through the switching valve, and purified gas obtained by filtering is led out to the purified gas main pipe; when the filtering and catalyzing unit performs back flushing to remove ash, the clean gas vent pipe is communicated with the back flushing branch pipe through the switching valve, and back flushing gas is blown into the filtering and catalyzing unit, so that the lower particle filtering layer and the upper particle filtering layer perform back flushing fluidization to remove ash.
The lower part of the shell body is provided with an air suction opening, the air suction opening is communicated with the upstream air inlet pipe through a gas circulation pipeline and a circulating fan, and the upstream air inlet pipe is provided with a filter aid powder injection opening. The dust-containing gas in the inner cavity of the outer shell can be forced to be guided to the lower part of the outer shell by arranging the air exhaust port, so that dust sedimentation is promoted, and the temperature difference between the upper part and the lower part of the particle bed dust removal catalytic device is reduced; when the dust contained in the dust-containing gas is submicron particles, the filter-aid powder can be injected from a filter-aid powder injection port arranged on the upstream air inlet pipe, the filter-aid powder not only can play a filter-aid role of dust filtration, but also the submicron particles are adhered to the filter-aid powder to be beneficial to settling in the outer shell and being smoothly discharged; the filter-aid powder can be lime or fly ash or other micron-sized powder.
The particle bed dust removal catalytic device further comprises a hopper, wherein the hopper is arranged at the lower part of the outer shell, the hopper is communicated with the dust discharge port, and a discharge port is formed in the bottom of the hopper. Here, the hopper is provided to collect the dust discharged from the dust discharge port more easily.
Compared with the prior art, the invention has the advantages that:
1) the invention realizes dust removal by arranging an independent catalyst layer between the flow stabilizing layer and the air purifying chamber without changing the original stacking structure of the upper particle filter layer, the lower particle filter layer and the flow stabilizing layer, and effectively removes harmful gases in the gases such as tar gas or organic waste gas or NO at high airspeed by utilizing the catalyst layer adopting the low-resistance high-activity catalystxAnd the like.
2) The invention adopts the honeycomb catalyst or the foamed ceramic catalyst with high specific surface area and high void ratio, and has the advantages of high activity, compact structure, low cost of the integral structure and small resistance reduction.
Drawings
FIG. 1 is a schematic diagram of the particle bed dust removal catalyst assembly of the present invention;
FIG. 2 is a schematic view showing the composition of the upper particle filtration layer, the lower particle filtration layer, the flow stabilizing layer and the catalyst layer in the particulate bed dust removal catalyst device of the present invention.
Detailed Description
The invention is described in further detail below with reference to the accompanying examples.
The first embodiment is as follows:
the embodiment provides a particle bed dust removal catalytic device, as shown in fig. 1 and fig. 2, which comprises an outer shell 1, six layers of particle bed filtering catalytic devices and a hopper 3, wherein the six layers of particle bed filtering catalytic devices are arranged in an inner cavity of the outer shell 1 along the vertical direction, the upper part of the outer shell 1 is provided with a dust-containing gas inlet 11 communicated with an upstream air inlet pipe (not shown in the figure), the lower part of the outer shell 1 is provided with a dust outlet 12, the hopper 3 is arranged at the lower part of the outer shell 1, the hopper 3 is communicated with the dust outlet 12, the bottom of the hopper 3 is provided with a discharge opening 31, each layer of particle bed filtering catalytic device comprises two filtering catalytic units 2, each filtering catalytic unit 2 is provided with a dust-containing gas vent 21 and a clean gas vent 22, the two filtering catalytic units 2 are symmetrically arranged at two sides of the inner cavity of the outer shell 1, a space between opposite, the filtering and catalyzing units 2 in the same layer are oppositely and symmetrically arranged, so that the back blowing gas generated when one filtering and catalyzing unit 2 in the lowest layer performs back blowing and ash removal can be more easily received by the filtering and catalyzing units 2 in the same layer, the back blowing gas cannot flow upwards and reversely to hinder dust settlement, and an air suction opening arranged at the lower part of the outer shell 1 for forcibly sucking the back blowing gas to flow downwards can be omitted; the filtering and catalyzing unit 2 consists of a dust-containing air chamber 23, an upper particle filtering layer 24 for performing coarse filtering and dust removal on dust-containing air from the dust-containing air chamber 23, a lower particle filtering layer 25 for performing fine filtering and dust removal on dust-containing air from the upper particle filtering layer 24, a steady flow layer 26 capable of uniformly distributing air, a catalyst layer 27 adopting low-resistance high-activity monolithic catalyst for removing harmful gas in the gas from the steady flow layer 26, and a gas purifying chamber 28, wherein the steady flow layer 26 is directly laid on the catalyst layer 27, the lower particle filtering layer 25 is directly laid on the steady flow layer 26, the upper particle filtering layer 24 is directly laid on the lower particle filtering layer 25, the dust-containing air chamber 23 is arranged above the upper particle filtering layer 24, the gas purifying chamber 28 is arranged below the catalyst layer 27, the dust-containing air vent 21 is arranged on the dust-containing air chamber 23, the gas purifying air vent 22 is arranged on the gas purifying chamber 28, dust-containing gas enters the inner cavity of the outer shell 1 through the dust-containing gas inlet 11, the dust-containing gas in the inner cavity of the outer shell 1 enters the dust-containing gas chamber 23 through the dust-containing gas vent 21, the dust-containing gas in the dust-containing gas chamber 23 sequentially passes through the coarse filtration dust removal of the upper particle filter layer 24 and the fine filtration dust removal of the lower particle filter layer 25 to obtain gas, the gas passes through the flow stabilizing layer 26 and then enters the catalyst layer 27, the clean gas obtained after the harmful gas in the gas is removed through the catalyst layer 27 enters the clean gas chamber 28, the clean gas in the clean gas chamber 28 is output through the clean gas vent 22, and the dust settled at the lower part of the outer shell 1 is discharged through the dust discharge port 12.
In this embodimentThe catalyst layer 27 is composed of a porous support 271 and a grid 272 which are sequentially arranged from bottom to top, each grid of the grid 272 under the support of the porous support 271 is filled with a low-resistance high-activity monolithic catalyst which is a honeycomb catalyst, the porous support 271 is arranged above the air purifying chamber 28, and the grid 272 is arranged below the flow stabilizing layer 26. Here, the grid 272 and the porous support 271 are provided below the flow stabilizer layer 26 in order to support the flow stabilizer layer 26 and the upper and lower particle filtration layers 25 and 24 above it by the grid 272; the honeycomb catalyst filled in each grid of the grid 272 is supported by a porous support 271, and the back-blowing airflow is pre-distributed; the honeycomb catalyst filled in each cell of the lattice 272 can effectively remove harmful gas, and the structure is more compact by using the honeycomb catalyst having a high cell density. Here, the porous support 271 may be a grid plate, a mesh plate, a screen, or the like; the honeycomb catalyst is made of TiO2NO as carrier with V-W as main active componentxReduction catalyst (SCR), NOxAnd NH3Catalytic reduction of NOxReduction to N2Effective removal of NO from dust-laden gasesxThe cell density of the honeycomb catalyst was cpsi 86. Here, the thickness of the catalyst layer 27 is designed to be 100 mm.
In this embodiment, the steady flow layer 26 includes an upper slotted screen 261, a particle layer 262 and a lower slotted screen 263, which are sequentially arranged from top to bottom, the upper slotted screen 261 and the lower slotted screen 263 clamp the particle layer 262, and the slot gaps of the upper slotted screen 261 and the lower slotted screen 263 are smaller than the particle size of the particles adopted by the particle layer 262. The particle layer 262 clamped by the upper slotted screen 261 and the lower slotted screen 263 cannot be overturned at any air speed (including local high air speed when abnormal occurs), so that the particle layer 262 is always stable and disorderly, the steady flow layer 26 can be effectively ensured to uniformly distribute air, dust-containing air from top to bottom during filtering can uniformly flow through the upper particle filtering layer 24 and the lower particle filtering layer 25, and particularly, blowback air from bottom to top can uniformly fluidize the lower particle filtering layer 25 and the upper particle filtering layer 24 during blowback ash removal; to ensure that the upper slotted screen 261 and the lower slotted screen 263 can sandwich the granular layer 262, it is required that the slotted clearance of the upper slotted screen 261 and the lower slotted screen 263 is smaller than the grain size of the granules used for the granular layer 262. Here, the particles in the particle layer 262 are sea sand having an average particle diameter of 1.5 to 3 mm.
In this particular embodiment, the particles employed in the upper particle filtration layer 24 have a larger particle size than the particles employed in the lower particle filtration layer 25, and the density of the particles in the upper particle filtration layer 24 is less than the density of the particles in the lower particle filtration layer 25. Here, the particle size of the particles used in the upper particle filtration layer 24 is required to be larger than the particle size of the particles used in the lower particle filtration layer 25, and the density of the particles in the upper particle filtration layer 24 is required to be smaller than the density of the particles in the lower particle filtration layer 25, so that the dust-containing gas can be roughly filtered and then finely filtered, the filtering and dust removing effects are better, and the lower particle filtration layer and the upper particle filtration layer are not mixed with each other after the dust is removed by blowback. Here, the particles used in the upper particle filtration layer 24 are expanded perlite particles having an average particle size of 1 to 3 mm, and the particles used in the lower particle filtration layer 25 are sea sand having an average particle size of 0.3 to 0.8 mm.
In this embodiment, the clean air vent 22 is connected to a clean air vent pipe 4, the clean air vent pipe 4 extends out of the outer casing 1, and is connected to a clean air branch pipe (not shown) and a blowback branch pipe (not shown) through a switching valve (not shown). When the filtering catalytic unit 2 filters, the purified gas vent pipe 4 is communicated with the purified gas branch pipe through a switching valve, and purified gas obtained by filtering is led out to the purified gas main pipe; when the filtering and catalyzing unit 2 performs back-blowing ash removal, the clean air vent pipe 4 is communicated with the back-blowing branch pipe through the switching valve, and back-blowing air is blown into the filtering and catalyzing unit 2, so that the lower particle filter layer 25 and the upper particle filter layer 24 perform back-blowing fluidization ash removal.
In this embodiment, the lower portion of the outer casing 1 is provided with an air exhaust port 13, the air exhaust port 13 is communicated with an upstream air inlet pipe through a gas circulation pipeline (not shown) and a circulation fan (not shown), and the upstream air inlet pipe is provided with a filter aid powder injection port (not shown). The dust-containing gas in the inner cavity of the outer shell 1 can be forced to be guided to the lower part of the outer shell 1 by arranging the air exhaust port, so that the dust sedimentation is promoted, and the temperature difference between the upper part and the lower part of the particle bed dust removal catalytic device is reduced; when the dust contained in the dust-containing gas is submicron particles, the filter aid powder can be injected from a filter aid powder injection port arranged on the upstream air inlet pipe, the filter aid powder can not only play a filter aid role of filtering the dust, but also the submicron particles are adhered to the filter aid powder, so that the submicron particles are beneficial to settling in the outer shell 1 and can be smoothly discharged; the filter-aid powder can be lime or fly ash or other micron-sized powder.
The dust content in the purified gas obtained after the dust-containing flue gas is treated by the granular bed dust removal catalytic device of the embodiment is less than 10mg/Nm3The temperature is 300-400 ℃, and the space velocity is 10000h-1～15000h-1Of (i) is NOxThe removal rate is 85-93%.
Example two:
the structure of the granular-bed dust-removal catalytic device proposed in this example is substantially the same as that of the granular-bed dust-removal catalytic device of example one, except that: the honeycomb catalyst filled in each cell of the lower grid 272 supported by the porous support 271 is made of gamma-Al2O3The organic waste gas oxidation catalyst is used as a carrier and takes noble metals platinum and palladium as main active components, and the organic waste gas oxidation catalyst can effectively remove organic waste gas in dust-containing gas.
The dust content in the purified gas obtained after the dust-containing industrial waste gas is treated by the particle bed dust removal catalytic device of the embodiment is less than 10mg/Nm3The temperature is 300-350 ℃, and the space velocity is 10000h-1～20000h-1The removal rate of chlorobenzene is 90-92%.
Example three:
the structure of the granular-bed dust-removal catalytic device proposed in this example is substantially the same as that of the granular-bed dust-removal catalytic device of example one, except that: the honeycomb catalyst filled in each cell of the lower grid 272 supported by the porous support 271 is Al2O3The tar cracking catalyst is used as a carrier and takes nickel as a main active component, and the tar cracking catalyst can effectively remove tar gas in dust-containing gas.
Dust-containing hot gas is subjected to dust removal catalysis by the granular bed in the embodimentThe dust content in the purified gas obtained after the treatment is less than 10mg/Nm3The temperature is 800-850 ℃, and the space velocity is 10000h-1～15000h-1The removal rate of the tar simulant is 85-90%.
Example four:
the structure of the granular-bed dust-removal catalytic device proposed in this example is substantially the same as that of the granular-bed dust-removal catalytic device of example one, except that: filled in each of the cells of the lower support grid 272 of the porous support 271 is a mechanically stronger ceramic foam catalyst based on 45ppi ceramic foam and TiO2Monolithic NO as carrier with V-W as main active componentxReduction catalyst (SCR) with monolithic NOxThe reduction catalyst can effectively remove NO in dust-containing gasx(ii) a The thickness of the catalyst layer was designed to be 120 mm.
The dust content in the purified gas obtained after the dust-containing flue gas is treated by the granular bed dust removal catalytic device of the embodiment is less than 10mg/Nm3The temperature is 300-400 ℃, and the space velocity is 8000h-1～12000h-1Of (i) is NOxThe removal rate is 84-91%.
Example five:
the structure of the granular-bed dust-removal catalyst device proposed in this example is substantially the same as that of the granular-bed dust-removal catalyst device of example four, except that: the ceramic foam catalyst filled in each cell of the lower grid 272 of the support of the porous support 271 was a 45ppi ceramic foam as a base material and γ -Al2O3The monolithic organic waste gas oxidation catalyst is used as a carrier and takes noble metals platinum and palladium as main active components, and the monolithic organic waste gas oxidation catalyst can effectively remove organic waste gas in dust-containing gas.
The dust content in the purified gas obtained after the dust-containing industrial waste gas is treated by the particle bed dust removal catalytic device of the embodiment is less than 10mg/Nm3The temperature is 300-350 ℃, and the space velocity is 10000h-1～18000h-1The removal rate of chlorobenzene is 88-92%.
Example six:
the structure of the granular-bed dust-removal catalyst device proposed in this example is substantially the same as that of the granular-bed dust-removal catalyst device of example four, except that: the ceramic foam catalyst filled in each cell of the lower grid 272 supported by the porous support 271 was a 45ppi ceramic foam as a base material and Al2O3The integral tar cracking catalyst is used as a carrier and takes nickel as a main active component, and the integral tar cracking catalyst can effectively remove tar gas in dust-containing gas.
The dust content in the purified gas obtained after the dust-containing hot coal gas is treated by the particle bed dust removal catalytic device of the embodiment is less than 10mg/Nm3The temperature is 800-850 ℃, and the space velocity is 8000h-1～12000h-1The removal rate of the tar simulant is 83-90%.

Claims (9)

1. The utility model provides a granule bed dust removal catalytic unit, include the shell body and along vertical direction set up in the inner chamber of shell body in at least one deck granule bed filter catalyst ware, the upper portion of shell body be provided with the dust-laden gas import of upper reaches intake pipe intercommunication, the lower part of shell body be provided with the dust discharge port, every layer granule bed filter catalyst ware include at least one filtration catalytic unit, every filtration catalytic unit have dust-laden gas vent and clean gas vent, its characterized in that: the filtering and catalyzing unit consists of a dust-containing gas chamber, an upper particle filtering layer for performing coarse filtering and dust removal on dust-containing gas from the dust-containing gas chamber, a lower particle filtering layer for performing fine filtering and dust removal on the dust-containing gas from the upper particle filtering layer, a flow stabilizing layer capable of uniformly distributing air, a catalyst layer for removing harmful gas in the gas from the flow stabilizing layer by adopting a low-resistance high-activity monolithic catalyst, and a gas purifying chamber, wherein the dust-containing gas vent is arranged on the dust-containing gas chamber, and the gas purifying vent is arranged on the gas purifying chamber;
every layer granule bed filter catalyst ware include two filter catalytic unit, filter catalytic unit symmetrical arrangement in the both sides of the inner chamber of shell body, symmetrical arrangement two filter catalytic unit relative one side between the space with dust-containing gas vent intercommunication.
2. A particulate bed dust removal catalyst assembly as claimed in claim 1 wherein: the catalyst layer comprises porous support piece and grid that set gradually from bottom to top porous support piece's support down every grid of grid in pack and be equipped with low resistance high activity monolithic catalyst, low resistance high activity monolithic catalyst be honeycomb catalyst or foamed ceramic catalyst, porous support piece set up in the top of air-purifying chamber, the grid set up in the below of stationary flow layer.
3. A particulate bed dust removal catalyst assembly as claimed in claim 2 wherein: the porous supporting piece is a grating plate or a grid plate or a screen.
4. A particulate bed dust removal catalyst assembly as claimed in claim 2 or 3 wherein: the honeycomb catalyst is an NOx reduction catalyst which takes TiO2 as a carrier and V-W as a main active component; or the honeycomb catalyst is an organic exhaust gas oxidation catalyst which takes gamma-Al 2O3 as a carrier and precious metals platinum and palladium as main active components; or the honeycomb catalyst is a tar cracking catalyst which takes Al2O3 as a carrier and takes nickel as a main active component.
5. A particulate bed dust removal catalyst assembly as claimed in claim 2 or 3 wherein: the foamed ceramic catalyst is an integral NOx reduction catalyst which takes 30-100 ppi foamed ceramic as a base material, TiO2 as a carrier and V-W as a main active component; or the foamed ceramic catalyst is an integral organic waste gas oxidation catalyst which takes 30-100 ppi foamed ceramic as a base material, gamma-Al 2O3 as a carrier and precious metals of platinum and palladium as main active components; or the foamed ceramic catalyst is an integral tar cracking catalyst which takes 30-100 ppi foamed ceramic as a base material, Al2O3 as a carrier and nickel as a main active component.
6. A particulate bed dust removal catalyst assembly as claimed in claim 1 wherein: the steady flow layer comprises an upper slotted screen, a particle layer and a lower slotted screen which are sequentially arranged from top to bottom, the upper slotted screen and the lower slotted screen clamp the particle layer, and the slot clearance between the upper slotted screen and the lower slotted screen is smaller than the particle size of the particles adopted by the particle layer.
7. A particulate bed dust removal catalyst assembly as claimed in claim 6 wherein: the particle size of the particles adopted in the upper particle filtering layer is larger than that of the particles adopted in the lower particle filtering layer, and the density of the particles in the upper particle filtering layer is smaller than that of the particles in the lower particle filtering layer.
8. A particulate bed dust removal catalyst assembly as claimed in claim 1 or claim 2 wherein: the air purification vent is connected with an air purification vent pipe, the air purification vent pipe extends out of the outer shell and is respectively connected with an air purification branch pipe and a back flushing branch pipe through a switching valve; the lower part of the shell body is provided with an air suction opening, the air suction opening is communicated with the upstream air inlet pipe through a gas circulation pipeline and a circulating fan, and the upstream air inlet pipe is provided with a filter aid powder injection opening.
9. A particulate bed dust removal catalyst assembly as claimed in claim 1 or claim 2 wherein: the particle bed dust removal catalytic device further comprises a hopper, wherein the hopper is arranged at the lower part of the outer shell, the hopper is communicated with the dust discharge port, and a discharge port is formed in the bottom of the hopper.
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CN107261779A (en) * 2017-06-30 2017-10-20 合肥天翔环境工程有限公司 A kind of aluminium melting furnace flue-gas dust-removing and desulfurization system
CN107158942A (en) * 2017-06-30 2017-09-15 合肥天翔环境工程有限公司 A kind of sintering furnace flue-gas dust-removing and desulfurization system
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CN110523169B (en) * 2019-09-09 2021-02-02 中国科学院过程工程研究所 Movable granular bed dust removal device capable of adjusting thickness of filter material
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