CN110152485B - High-temperature denitration dust removal device for flue gas of cement kiln - Google Patents

High-temperature denitration dust removal device for flue gas of cement kiln Download PDF

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Publication number
CN110152485B
CN110152485B CN201910437647.3A CN201910437647A CN110152485B CN 110152485 B CN110152485 B CN 110152485B CN 201910437647 A CN201910437647 A CN 201910437647A CN 110152485 B CN110152485 B CN 110152485B
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box body
gas
flue gas
pipe
ammonia
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CN110152485A (en
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张志刚
李骞
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Ctiec Environmental Protection Research Institute Jiangsu Co ltd
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Ctiec Environmental Protection Research Institute Jiangsu Co ltd
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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
    • B01D46/0002—Casings; Housings; Frame constructions
    • 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
    • B01D46/0002—Casings; Housings; Frame constructions
    • B01D46/0005—Mounting of filtering elements within casings, housings or frames
    • 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
    • B01D46/24—Particle separators, e.g. dust precipitators, using rigid hollow filter bodies
    • B01D46/2403—Particle separators, e.g. dust precipitators, using rigid hollow filter bodies characterised by the physical shape or structure of the filtering element
    • B01D46/2411—Filter cartridges
    • 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
    • B01D46/58—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 parallel
    • B01D46/60—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 parallel arranged concentrically or coaxially
    • 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
    • B01D46/66—Regeneration of the filtering material or filter elements inside the filter
    • B01D46/70—Regeneration of the filtering material or filter elements inside the filter by acting counter-currently on the filtering surface, e.g. by flushing on the non-cake side of the filter
    • B01D46/71—Regeneration of the filtering material or filter elements inside the filter by acting counter-currently on the filtering surface, e.g. by flushing on the non-cake side of the filter with pressurised gas, e.g. pulsed air
    • 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
    • B01D53/8631—Processes characterised by a specific device
    • 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
    • B01D53/88—Handling or mounting catalysts
    • 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
    • B01D53/90—Injecting reactants
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F23/00—Mixing according to the phases to be mixed, e.g. dispersing or emulsifying
    • B01F23/10—Mixing gases with gases
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F23/00—Mixing according to the phases to be mixed, e.g. dispersing or emulsifying
    • B01F23/10—Mixing gases with gases
    • B01F23/14—Mixing gases with gases with moving mixing elements, e.g. with liquid seal
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F33/00—Other mixers; Mixing plants; Combinations of mixers
    • B01F33/80—Mixing plants; Combinations of mixers
    • B01F33/82—Combinations of dissimilar mixers
    • B01F33/821—Combinations of dissimilar mixers with consecutive receptacles
    • B01F33/8212—Combinations of dissimilar mixers with consecutive receptacles with moving and non-moving stirring devices
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F35/00—Accessories for mixers; Auxiliary operations or auxiliary devices; Parts or details of general application
    • B01F35/71—Feed mechanisms
    • B01F35/712—Feed mechanisms for feeding fluids
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F35/00—Accessories for mixers; Auxiliary operations or auxiliary devices; Parts or details of general application
    • B01F35/71—Feed mechanisms
    • B01F35/717—Feed mechanisms characterised by the means for feeding the components to the mixer
    • B01F35/7179—Feed mechanisms characterised by the means for feeding the components to the mixer using sprayers, nozzles or jets
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2251/00—Reactants
    • B01D2251/20—Reductants
    • B01D2251/206—Ammonium compounds
    • B01D2251/2062—Ammonia
    • 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
    • B01D2258/0233—Other waste gases from cement factories
    • 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
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
    • Y02A50/00—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE in human health protection, e.g. against extreme weather
    • Y02A50/20—Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters
    • Y02A50/2351—Atmospheric particulate matter [PM], e.g. carbon smoke microparticles, smog, aerosol particles, dust

Abstract

The invention discloses a high-temperature denitration dust removal device for flue gas of a cement kiln, which comprises a reactor box body and an ammonia spraying device, wherein the inside of the reactor box body is divided into a left box body and a right box body; the ammonia spraying device comprises a gas collecting pipe, two ends of the gas collecting pipe are respectively communicated with the left box body of the reactor box body through gas inlet pipelines, a shell is sleeved on the gas collecting pipe, the gas collecting pipe inside the shell is rotatably connected with a mixed flow cage body structure, one side outside the shell is provided with a smoke spraying pipe, and the other side outside the shell is provided with an ammonia spraying pipe; the invention has the advantages of dust removal rate and denitration rate of the flue gas reaching more than 90 percent, great reduction of pollution to the atmospheric environment, energy saving, environmental protection, high overall operation efficiency and suitability for popularization and application in cement production enterprises.

Description

High-temperature denitration dust removal device for flue gas of cement kiln
Technical Field
The invention relates to a high-temperature denitration and dust removal device for cement kiln flue gas, and belongs to the technical field of cement kiln flue gas treatment.
Background
At present, a novel dry-method cement production technology is mainly adopted in cement production, the discharged flue gas contains pollutants such as high nitrogen oxides, particulate matters, alkali metals, heavy metals and the like, the SNCR technology commonly used at present is treated at the tail end of the flue gas in the cement industry, and the flue gas discharged after being treated by the technology cannot meet increasingly strict environmental protection requirements in the cement industry, so that the SCR technology with higher denitration efficiency is increasingly applied to the cement industry; the temperature of the cement kiln flue gas passing through the preheater is generally about 350 ℃, the cement kiln flue gas belongs to a high-efficiency denitration temperature window of a traditional SCR catalyst, the SCR catalyst is the denitration catalyst, but pollutants such as high-concentration dust, heavy metal and alkali metal exist in the cement kiln flue gas, the effect of the existing denitration dust removal device in dedusting and filtering the pollutants such as the high-concentration dust, the heavy metal and the alkali metal in the flue gas is not good, so that the pollutants are omitted, the omitted pollutants easily cause blockage, abrasion and poisoning of the SCR catalyst, and the denitration efficiency and the service life of the SCR catalyst are seriously damaged; meanwhile, because pollutants such as high-concentration dust, heavy metals and alkali metals exist in the flue gas of the cement kiln, the flue gas and ammonia gas cannot be fully mixed in a flue pipe, and the denitration effect of the subsequent SCR catalyst on the flue gas is further influenced.
Disclosure of Invention
In order to solve the defects of the prior art, the invention provides a high-temperature denitration dust removal device for flue gas of a cement kiln, which can fully mix the high-temperature flue gas of the cement kiln with ammonia gas, and simultaneously, the invention adopts a plurality of ceramic fiber filter tubes arranged in a three-dimensional array to perform dust removal and filtration on the mixed gas formed by mixing the flue gas and the ammonia gas, thereby effectively filtering pollutants such as particles, alkali metals and the like in the flue gas, preventing the omission of the pollutants, greatly reducing the blockage, abrasion and poisoning of an SCR catalyst, prolonging the service life of the SCR catalyst, and effectively removing nitrogen oxides in the flue gas by the SCR catalyst.
The technical scheme adopted by the invention is as follows:
a high-temperature denitration dust removal device for flue gas of a cement kiln comprises a reactor box body and an ammonia injection device, wherein the inside of the reactor box body is divided into a left box body and a right box body, the tops of the left box body and the right box body are mutually communicated, a denitration catalyst is arranged inside the right box body, a gas outlet pipeline is connected onto the right box body below the denitration catalyst, a filter frame body is arranged inside the left box body, a plurality of ceramic fiber filter tubes are mounted on the filter frame body, a pulse soot blowing device is arranged inside the left box body above the filter frame body, the input end of the pulse soot blowing device is communicated with an external compressed air pipeline, a plurality of injection tubes corresponding to the plurality of ceramic fiber filter tubes are formed on the pulse soot blowing device, an ash bucket is arranged at the bottom of the left box body, and an ash discharge valve is arranged at the outlet; the ammonia spraying device comprises a gas collecting pipe, two ends of the gas collecting pipe are respectively communicated with a left box body of the reactor box body through a gas inlet pipeline, the communicating position of the gas inlet pipeline and the left box body of the reactor box body is positioned between a filter frame body and an ash bucket, a shell is sleeved on the gas collecting pipe, a mixed flow cage body structure is rotatably connected on the gas collecting pipe inside the shell, a plurality of gas collecting holes are formed on the gas collecting pipe inside the mixed flow cage body structure, a smoke spraying pipe is arranged on one side outside the shell, an ammonia spraying pipe is arranged on the other side outside the shell, the smoke spraying pipe and the ammonia spraying pipe are respectively parallel to the horizontal plane, the smoke spraying pipe and the ammonia spraying pipe are not on the same horizontal plane, the smoke spraying pipe is communicated with the inside of the shell through a plurality of smoke spraying branch pipes, the ammonia spraying pipe is communicated with the inside of the shell through a plurality of ammonia spraying branch pipes, and a dust bucket is arranged at the bottom, an ash discharge valve is arranged at the outlet at the bottom of the dust hopper.
As a further preference of the invention, the two gas inlet pipes are not arranged in the right direction at the communicating part of the left box body of the reactor box body, the mixed gas of the flue gas and the ammonia gas flows into the left box body through the two gas inlet pipes, two flowing mixed gases do not influence each other at the moment when just entering the left box body, and the two flowing mixed gases finally meet in the left box body; the static mixer is used for carrying out turbulent mixing on the mixed gas of the flue gas and the ammonia gas flowing in the gas inlet pipeline again so as to ensure the mixing effect of the flue gas and the ammonia gas; the mixed gas of the flue gas and the ammonia gas treated by the static mixer is guided by the guide device to form linear flow and finally flows into the left box body; the flow guide device is arranged in the air inlet pipeline at the tail end of the air inlet pipeline and comprises two transverse plates and two longitudinal plates, and the two transverse plates and the two longitudinal plates are connected in a groined shape; the two transverse plates and the two longitudinal plates which are connected in the shape of the Chinese character jing separate the mixed gas of the flue gas and the ammonia gas in the gas inlet pipeline, so that the mixed gas of the flue gas and the ammonia gas is guided to flow quickly to form linear flow.
As a further preferred aspect of the present invention, the end of the gas inlet pipe is connected to the left box of the reactor box in an inclined manner, and the gas inlet direction at the end of the gas inlet pipe is inclined upward; because the left box intercommunication department of two admission lines and reactor box is not just to setting up, consequently, the gas mixture of flue gas and ammonia upwards flows into left box inside through two admission lines slopes, the gas mixture that two slopes upwards flows crosses at the inside spiral of left box, and make progress the spiral flow, the air current that makes progress the spiral flow contacts with a plurality of ceramic fiber chimney filter of installing on filtering the support body, and the gas mixture keeps the state of flowing in the space between a plurality of ceramic fiber chimney filter, the dust granule is difficult for piling up on ceramic fiber chimney filter surface, effectively improve the filtration efficiency of ceramic fiber chimney filter, guarantee the filter effect of ceramic fiber chimney filter.
As a further preferred aspect of the present invention, the smoke spraying pipe is located outside the casing obliquely above the left side of the gas collecting pipe, and the ammonia spraying pipe is located outside the casing obliquely below the right side of the gas collecting pipe, so that the smoke and ammonia sprayed into the casing by the smoke spraying pipe and the ammonia spraying pipe are respectively located above and below the gas collecting pipe; the smoke spraying branch pipe and the ammonia spraying branch pipe are respectively provided with an electromagnetic valve; the PLC controller is used for controlling the on-off of a part of electromagnetic valves so as to adjust the working load intensity of the ammonia spraying device; the PLC can also be used for controlling the electromagnetic valves on the plurality of the smoke spraying branch pipes to be alternately switched on and off, or controlling the electromagnetic valves on the plurality of the ammonia spraying branch pipes to be alternately switched on and off, or controlling the electromagnetic valves on the smoke spraying branch pipes and the ammonia spraying branch pipes to be synchronously alternately switched on and off, so that the mode that smoke and ammonia gas enter the shell is changed.
As a further preferred aspect of the present invention, the mixed flow cage structure comprises two parallel end plates, the two end plates are respectively rotatably connected with the gas collecting pipe through bearings, a plurality of blades are connected between the two end plates, and the plurality of blades uniformly surround the end plates for one circle in the circumferential direction; the flue gas is through spouting the tobacco pipe, the ammonia is spout the ammonia pipe simultaneously and is spouted when inside into the casing, gas flow drives the mixed flow cage body structure that end plate and blade constitute and rotates along the discharge circumferencial direction, the mixed flow cage body structure rotates and makes flue gas and ammonia flow and mix along the casing circumferencial direction in the casing is inside, at the flue gas and the mixed in-process that flows of ammonia, when flue gas and ammonia flow the dust fill position that sets up bottom the casing, because space volume grow, flue gas and ammonia flow pressure reduce, heavier particulate matter sinks in the flue gas, fall into the dust fill, thereby realize the preliminary dust fall processing to the flue gas, indirectly improve subsequent ceramic fiber chimney filter efficiency.
As a further preferable mode of the invention, the end plates and the blades are made of aluminum alloy materials, the thickness of each blade is 2-3mm, each blade comprises a straight edge part and an oblique edge part, two ends of the straight edge part of each blade are fixedly connected with the two end plates respectively, an included angle between the straight edge part of each blade and a radial axis of each end plate is 135 degrees, and an included angle between the oblique edge part of each blade and the straight edge part of each blade is 135 degrees; the end plate and the blades made of the aluminum alloy material are light in weight, so that a mixed flow cage body structure formed by the end plate and the blades can conveniently rotate along the circumferential direction of the gas collecting pipe; the inside flue gas or the ammonia reposition of redundant personnel of the inside flue gas or the ammonia of casing will be got into to the straight limit portion and the hypotenuse portion of blade, slows down the flow velocity of flue gas or ammonia, changes the flow direction of flue gas or ammonia, is convenient for get into the inside flue gas of casing and ammonia and mixes.
As a further preferred aspect of the invention, a rake type soot blower is arranged inside the right box body above the denitration catalyst, a reserved catalyst bed layer is arranged inside the right box body above the rake type soot blower, a maintenance opening is arranged on the right box body corresponding to the denitration catalyst and the reserved catalyst bed layer, and a maintenance cover plate is connected to the maintenance opening in a sealing manner; the rake type soot blower is used for performing soot blowing treatment on the denitration catalyst to prevent the denitration catalyst from being blocked due to dust accumulation; a reserved catalyst bed layer is used for installing a second denitration catalyst or a spare denitration catalyst under emergency; the maintenance opening is convenient for maintaining and replacing the denitration catalyst.
As a further preferred aspect of the present invention, the denitration catalyst is a plate-type denitration catalyst, and the pore diameter of the plate-type denitration catalyst is 7 mm; the surface of the plate-type denitration catalyst facing to the gas coming direction is a plane or a spherical surface; the plate-type denitration catalyst with the aperture of 7mm can effectively remove nitrogen oxides in flue gas, and the surface of the plate-type denitration catalyst facing the gas coming direction is a spherical surface, so that the contact surface of the plate-type denitration catalyst and the flue gas can be effectively increased, and the denitration rate of the flue gas is improved.
As a further preferred aspect of the present invention, an electric block is mounted on the top of the outer side of the right tank body of the reactor tank body; when the denitration catalyst or the ceramic fiber filter tube needs to be maintained and replaced, the electric hoist is used for hoisting the denitration catalyst or the ceramic fiber filter tube; install the vibrator on the outside wall of ash bucket, the quick discharge of the dust particulate matter of being convenient for.
As a further preferred aspect of the present invention, the filter frame body is a hollow conical structure, the outer circumferential surface of the filter frame body with the hollow conical structure is a continuous annular step structure, a plurality of ceramic fiber filter tubes are installed on the step surface of each annular step structure, and a plurality of ceramic fiber filter tubes installed on the step surface of each annular step structure are uniformly arranged in the circumferential direction; the filtering frame body is of a hollow conical body structure, the outer circumferential surface of the filtering frame body of the hollow conical body structure is of a continuous annular step structure, and a plurality of ceramic fiber filtering pipes are arranged on the step surface of each annular step structure, so that the ceramic fiber filtering pipes form a three-dimensional array arrangement, and the integral filtering surface is effectively increased; moreover, the ceramic fiber filter tubes are mutually arranged in a stepped and staggered manner, so that the surrounding gas of each ceramic fiber filter tube has better fluidity, and the filtering efficiency of the ceramic fiber filter tubes is effectively improved; meanwhile, when the pulse soot blower performs soot blowing treatment on the ceramic fiber filter tube, dust falling off from the surface of the ceramic fiber filter tube can also fall rapidly.
The invention has the beneficial effects that: the ammonia spraying device is additionally arranged before dedusting and filtering the flue gas, so that the high-temperature flue gas of the cement kiln and the ammonia gas can be fully mixed, and the ammonia spraying device has a certain buffering and dust-settling effect on the flue gas; the filtering frame body is of a hollow conical body structure, the outer circumferential surface of the filtering frame body of the hollow conical body structure is of a continuous annular step structure, and a plurality of ceramic fiber filtering pipes are arranged on the step surface of each annular step structure, so that the ceramic fiber filtering pipes form a three-dimensional array arrangement, and the integral filtering surface is effectively increased; moreover, the ceramic fiber filter tubes are mutually arranged in a stepped and staggered manner, so that the surrounding gas of each ceramic fiber filter tube has better fluidity, and the filtering efficiency of the ceramic fiber filter tubes is effectively improved; meanwhile, when the pulse soot blower performs soot blowing treatment on the ceramic fiber filter tube, dust falling off from the surface of the ceramic fiber filter tube can also fall rapidly; the invention realizes the dust removal and filtration of the mixed gas formed by mixing the flue gas and the ammonia gas by adopting the ceramic fiber filter tubes arranged in the three-dimensional array, effectively filters particulate matters, alkali metals and other pollutants in the flue gas, prevents the omission of the pollutants, greatly reduces the blockage, abrasion and poisoning of the SCR catalyst, prolongs the service life of the SCR catalyst, and can effectively remove nitrogen oxides in the flue gas by the SCR catalyst.
Description of the drawings;
FIG. 1 is a schematic structural view of the present invention;
FIG. 2 is a schematic top view of the ammonia injection apparatus of the present invention;
FIG. 3 is a schematic cross-sectional view of an ammonia injection device according to the present invention;
FIG. 4 is an enlarged schematic view of a portion of the ammonia injection apparatus of the present invention;
FIG. 5 is a schematic view of a blade configuration according to the present invention;
FIG. 6 is a schematic view of the structure of the flow guiding device of the present invention;
FIG. 7 is a schematic view of the connection of the inlet duct of the present invention to the left box of the reactor box;
FIG. 8 is a schematic view of the structure of the filter frame of the present invention;
the main reference numerals in the figures have the following meanings:
1-ammonia injection device, 2-gas inlet pipeline, 3-filter frame body, 4-ceramic fiber filter tube, 5-pulse soot blower, 51-injection tube, 6-reactor box body, 7-rake soot blower, 8-denitration catalyst, 9-ash bucket, 10-gas outlet pipeline, 11-smoke injection tube, 12-ammonia injection tube, 13-smoke injection branch tube, 14-ammonia injection branch tube, 15-electromagnetic valve, 16-mixed flow cage body structure, 161-end plate, 162-blade, 1621-straight edge part, 1622-inclined edge part, 17-gas collecting tube, 18-gas collecting hole, 19-bearing, 20-axial fan, 21-static mixer, 22-flow guide device, 221-transverse plate, 222-longitudinal plate, 23-dust bucket, 24-shell, 25-reserved catalyst bed, 26-electric hoist, 27-vibrator, and 28-ash discharge valve.
A specific embodiment;
the present invention will be described in detail with reference to the accompanying drawings and examples.
As shown in fig. 1-3: the embodiment is a high-temperature denitration and dust removal device for flue gas of a cement kiln, which comprises a reactor box body 6 and an ammonia spraying device 1, wherein the interior of the reactor box body 6 is divided into a left box body and a right box body, the top parts of the left box body and the right box body are communicated with each other, a denitration catalyst 8 is arranged in the right box body, an air outlet pipeline 10 is connected on the right box body below the denitration catalyst 8, a filter frame body 3 is arranged in the left box body, a plurality of ceramic fiber filter tubes 4 are arranged on the filter frame body 3, a pulse soot blower 5 is arranged in the left box body above the filter frame body 3, the input end of the pulse soot blower 5 is communicated with an external compressed air pipeline, a plurality of blowing pipes 51 corresponding to a plurality of ceramic fiber filter pipes 4 are formed on the pulse soot blower 5, an ash bucket 9 is arranged at the bottom of the left box body, and an ash discharge valve 28 is arranged at the bottom outlet of the ash bucket 9; the ammonia spraying device 1 comprises a gas collecting pipe 17, two ends of the gas collecting pipe 17 are respectively communicated with a left box body of a reactor box body 6 through a gas inlet pipeline 2, the communicating position of the gas inlet pipeline 2 and the left box body of the reactor box body 6 is positioned between a filter frame body 3 and an ash bucket 9, a shell body 24 is sleeved on the gas collecting pipe 17, a mixed flow cage body structure 16 is rotatably connected on the gas collecting pipe 17 in the shell body 24, a plurality of gas collecting holes 18 are formed on the gas collecting pipe 17 in the mixed flow cage body structure 16, a smoke spraying pipe 11 is arranged on one side of the outer part of the shell body 24, an ammonia spraying pipe 12 is arranged on the other side of the outer part of the shell body 24, the smoke spraying pipe 11 and the ammonia spraying pipe 12 are respectively parallel to a horizontal plane, the smoke spraying pipe 11 and the ammonia spraying pipe 12 are not on the same horizontal plane, the smoke spraying pipe 11 is communicated with the inner part of the shell body 24 through a plurality of smoke spraying branch pipes 13, the ammonia, the bottom of the shell 24 is provided with a dust hopper 23, and the bottom outlet of the dust hopper 23 is provided with an ash discharge valve 28.
As shown in fig. 2, in this embodiment, the two air inlet pipes 2 are not arranged in the right direction at the communicating position with the left box of the reactor box 6, the mixture of the flue gas and the ammonia gas flows into the left box through the two air inlet pipes 2, the two flowing mixtures do not affect each other at the moment when entering the left box, and the two flowing mixtures finally meet in the left box; the air inlet pipeline 2 is sequentially provided with an axial flow fan 20, a static mixer 21 and a flow guide device 22 according to the air flowing direction, the two axial flow fans 20 on the two air inlet pipelines 2 work synchronously, the two axial flow fans 20 work synchronously to suck the mixed gas of the flue gas and the ammonia gas in the shell 24 of the ammonia spraying device 1, and the static mixer 21 carries out turbulent mixing on the mixed gas of the flue gas and the ammonia gas flowing in the air inlet pipeline 2 again so as to ensure the mixing effect of the flue gas and the ammonia gas; the mixed gas of the flue gas and the ammonia gas treated by the static mixer 21 is guided by the guide device 22 to form linear flow and finally flows into the left box body; in this embodiment, the flow guiding device 22 is disposed inside the air intake duct 2 at the end of the air intake duct 2, and the flow guiding device 22 includes two transverse plates 221 and two longitudinal plates 222, as shown in fig. 6, the two transverse plates 221 and the two longitudinal plates 222 are connected in a groined shape; the two transverse plates 221 and the two longitudinal plates 222 connected in a # -shape separate the mixed gas of the flue gas and the ammonia gas in the gas inlet pipeline 2, so that the mixed gas of the flue gas and the ammonia gas can be guided quickly to flow in a linear shape.
In practical application, as shown in fig. 7, the tail end of the air inlet pipeline 2 is obliquely connected with the left box body of the reactor box body 6, and the air inlet direction of the tail end of the air inlet pipeline 2 is obliquely upward; because two admission line 2 are not just to setting up with the left box intercommunication department of reactor box 6, therefore, the gas mixture of flue gas and ammonia upwards flows into left box inside through two admission line 2 slopes, two slopes upwards flowing gas mixture cross at the inside spiral of left box, and upwards spiral flow, upwards spiral flow's air current and the contact of a plurality of ceramic fiber chimney filter 4 of installing on filtering support body 3, and the gas mixture keeps the state of flow in the space between a plurality of ceramic fiber chimney filter 4, dust particle is difficult for piling up on ceramic fiber chimney filter 4 surface, effectively improve ceramic fiber chimney filter 4's filtration efficiency, guarantee ceramic fiber chimney filter 4's filter effect.
As shown in fig. 1-3, in the present embodiment, the smoke-spraying pipe 11 is located outside the casing 24 obliquely above the left side of the gas collecting pipe 17, and the ammonia-spraying pipe 12 is located outside the casing 24 obliquely below the right side of the gas collecting pipe 17, so that the smoke and ammonia gas sprayed into the casing 24 by the smoke-spraying pipe 11 and the ammonia-spraying pipe 12 are respectively located above and below the gas collecting pipe 17; the smoke spraying branch pipe 13 and the ammonia spraying branch pipe 14 are respectively provided with an electromagnetic valve 15; the PLC controller is used for controlling the opening and closing of a part of electromagnetic valves 15 so as to adjust the working load intensity of the ammonia spraying device 1; the PLC can also be used for controlling the electromagnetic valves 15 on the plurality of the smoke spraying branch pipes 13 to be alternately switched on and off alternately, or controlling the electromagnetic valves 15 on the plurality of the ammonia spraying branch pipes 14 to be alternately switched on and off alternately, or controlling the electromagnetic valves 15 on the smoke spraying branch pipes 13 and the ammonia spraying branch pipes 14 to be alternately switched on and off synchronously so as to change the mode of the smoke and the ammonia gas entering the shell 24.
As shown in fig. 2-4, in the present embodiment, the flow mixing cage structure 16 includes two parallel end plates 161, the two end plates 161 are respectively rotatably connected to the gas collecting pipe 17 through the bearings 19, a plurality of blades 162 are connected between the two end plates 161, and the plurality of blades 162 uniformly surround the end plates 161 in a circumferential direction; when the flue gas through spraying tobacco pipe 11, the ammonia gas spouts the casing 24 inside through spraying ammonia pipe 12 simultaneously, the gas flow drives mixed flow cage body structure 16 that end plate 161 and blade 162 constitute and rotates along the discharge 17 circumferencial direction, mixed flow cage body structure 16 rotates and makes flue gas and ammonia flow and mix along the circumference direction in the casing 24 inside, at the in-process that flue gas and ammonia mix and flow, when flue gas and ammonia flow to the dust hopper 23 position that the casing 24 bottom set up, because the space volume grow, flue gas and ammonia flow pressure reduce, heavier particulate matter sinks in the flue gas, fall into dust hopper 23, thereby realize the preliminary dust fall of flue gas and handle, indirectly improve subsequent ceramic fiber filter tube 4 filtration efficiency.
The end plates 161 and the blades 162 in this embodiment are made of aluminum alloy, the thickness of the blades 162 is 2mm, and in practical application, the thickness of the blades 162 may also be 2.5mm or 3mm, as shown in fig. 4 and 5, the blades 162 in this embodiment include a straight edge portion 1621 and a beveled edge portion 1622, both ends of the straight edge portion 1621 of the blades 162 are respectively and fixedly connected with the two end plates 161, and an included angle between the straight edge portion 1621 of the blades 162 and a radial axis of the end plates 161 is 135 degrees, that is, an angle a shown in fig. 4; the angled edge portion 1622 of the blade 162 makes an angle of 135 degrees with the straight edge portion 1621 of the blade 162, i.e., angle B shown in fig. 4; the end plate 161 and the blades 162 made of aluminum alloy material are light in weight, so that the mixed flow cage body structure 16 formed by the end plate 161 and the blades 162 can conveniently rotate along the circumferential direction of the gas collecting pipe 17; the straight edge part 1621 and the inclined edge part 1622 of the blade 162 shunt the flue gas or ammonia gas entering the shell 24, slow down the flow speed of the flue gas or ammonia gas, change the flow direction of the flue gas or ammonia gas, and facilitate the mixing of the flue gas and ammonia gas entering the shell 24.
As shown in fig. 1, in the present embodiment, a rake soot blower 7 is arranged inside the right box above the denitration catalyst 8, a reserved catalyst bed layer 25 is arranged inside the right box above the rake soot blower 7, a maintenance opening is arranged on the right box corresponding to the denitration catalyst 8 and the reserved catalyst bed layer 25, and a maintenance cover plate is connected to the maintenance opening in a sealing manner; the rake type soot blower 7 is used for performing soot blowing treatment on the denitration catalyst 8 to prevent dust from accumulating to block the denitration catalyst 8; the reserved catalyst bed 25 is used for installing a second denitration catalyst or a standby denitration catalyst in an emergency; the maintenance opening is convenient for maintaining and replacing the denitration catalyst 8; in practical application, a maintenance opening can be formed in the left box body corresponding to the ceramic fiber filter tube 4, the maintenance opening is connected with the maintenance cover plate in a sealing mode, and the ceramic fiber filter tube 4 is convenient to maintain and replace.
The denitration catalyst 8 in this embodiment is a plate-type denitration catalyst, and the pore diameter of the plate-type denitration catalyst is 7 mm; the surface of the plate-type denitration catalyst facing to the gas coming direction is a plane, the plate-type denitration catalyst with the pore diameter of 7mm can effectively remove nitrogen oxides in flue gas, and the surface of the plate-type denitration catalyst facing to the gas coming direction can also be set into a spherical surface in practical application; the surface of the plate-type denitration catalyst towards the gas coming direction is a spherical surface, so that the contact surface of the plate-type denitration catalyst and the flue gas can be effectively increased, and the denitration rate of the flue gas is improved.
As shown in fig. 1, in the present embodiment, an electric hoist 26 is mounted on the top of the right box outer side of the reactor box 6; when the denitration catalyst 8 or the ceramic fiber filter tube 4 needs to be maintained and replaced, the electric hoist 26 is used for hoisting the denitration catalyst 8 or the ceramic fiber filter tube 4; a vibrator 27 is mounted on the outer side wall surface of the dust hopper 9 to facilitate rapid discharge of dust particles.
As shown in fig. 1 and 8, the filter frame body 3 in this embodiment is a hollow conical structure, the outer circumferential surface of the filter frame body 3 with the hollow conical structure is a continuous annular step structure, a plurality of ceramic fiber filter tubes 4 are installed on the step surface of each annular step structure, and a plurality of ceramic fiber filter tubes 4 installed on the step surface of each annular step structure are uniformly arranged in the circumferential direction; the filtering frame body 3 is a hollow conical body structure, the outer circumferential surface of the filtering frame body 3 with the hollow conical body structure is a continuous annular step structure, and a plurality of ceramic fiber filtering pipes 4 are arranged on the step surface of each annular step structure, so that the ceramic fiber filtering pipes 4 form a three-dimensional array arrangement, and the integral filtering surface is effectively increased; moreover, the ceramic fiber filter tubes 4 are arranged in a stepped and staggered manner, so that the surrounding gas of each ceramic fiber filter tube 4 has better fluidity, and the filtering efficiency of the ceramic fiber filter tubes 4 is effectively improved; meanwhile, when the pulse soot blower 5 performs soot blowing processing on the ceramic fiber filter tube 4, dust falling off from the surface of the ceramic fiber filter tube 4 can also fall rapidly.
The working principle of the embodiment is as follows:
firstly, high-temperature flue gas of a cement kiln is sprayed into a shell 24 of an ammonia spraying device 1 through a plurality of smoke spraying branch pipes 13 on a smoke spraying pipe 11, ammonia gas is sprayed into the shell 24 of the ammonia spraying device 1 through a plurality of ammonia spraying branch pipes 14 on an ammonia spraying pipe 12, the flue gas and the ammonia gas sprayed into the shell 24 drive a mixed flow cage structure 16 formed by an end plate 161 and blades 162 to rotate along the circumferential direction of a gas collecting pipe 17, the mixed flow cage structure 16 rotates to enable the flue gas and the ammonia gas to flow and mix in the shell 24 along the inner circumferential direction of the shell 24, and in the mixed flow process of the flue gas and the ammonia gas, when the flue gas and the ammonia gas flow to a dust hopper 23 arranged at the bottom of the shell 24, the flow pressure of the flue gas and the ammonia gas is reduced due to the fact that the space volume is enlarged, heavier particles in the flue gas sink and fall into; the PLC is used for controlling the two axial flow fans 20 on the two air inlet pipelines 2 to work synchronously, the two axial flow fans 20 work synchronously to suck mixed gas of smoke and ammonia gas inside a shell 24 of the ammonia spraying device 1, the mixed gas of the smoke and the ammonia gas inside the shell 24 flows into the gas collecting pipe 17 and the air inlet pipelines 2 through gas collecting holes 18 in the gas collecting pipe 17, and the static mixer 21 is used for carrying out turbulent mixing on the mixed gas of the smoke and the ammonia gas flowing in the air inlet pipelines 2 again so as to ensure the mixing effect of the smoke and the ammonia gas; the mixed gas of the flue gas and the ammonia gas treated by the static mixer 21 is guided by the guide device 23 to form linear flow and finally flows into the left box body; after the mixed gas of the flue gas and the ammonia gas flows into the left box body through the two gas inlet pipelines 2, the two flowing mixed gas flow to be intersected and flow upwards in the left box body, the upward flowing gas flow is contacted with the ceramic fiber filter tubes 4 arranged on the filter frame body 3, the mixed gas keeps a flowing state in gaps among the ceramic fiber filter tubes 4, pollutants such as dust particles, alkali metals and the like in the flue gas are intercepted on the surfaces of the ceramic fiber filter tubes 4, the mixed gas filtered by the ceramic fiber filter tubes 4 flows into the right box body of the reactor box body 6, nitrogen oxides in the flue gas are removed through catalysis of a denitration catalyst 8, and finally the mixed gas is discharged through the gas outlet pipeline 10; when the pressure difference between the left box body and the right box body reaches a certain degree or a preset value, the PLC controller is utilized to control the pulse soot blower 5 to start, the ceramic fiber filter tube 4 is subjected to reverse soot blowing treatment, so that dust particles accumulated on the surface of the ceramic fiber filter tube 4 fall off and finally fall into the ash bucket 9 and are discharged through the ash discharge valve 28, and the outer side wall surface of the ash bucket 9 is provided with the vibrator 27, so that the dust particles can be rapidly discharged; meanwhile, the rake type soot blower 7 is arranged in the right box body above the denitration catalyst 8, and the rake type soot blower 7 is started periodically to blow soot on the denitration catalyst 8, so that dust is prevented from being accumulated to block the denitration catalyst 88.
The ammonia spraying device is additionally arranged before dedusting and filtering the flue gas, so that the high-temperature flue gas of the cement kiln and the ammonia gas can be fully mixed, and the ammonia spraying device has a certain buffering and dust-settling effect on the flue gas; the filtering frame body is of a hollow conical body structure, the outer circumferential surface of the filtering frame body of the hollow conical body structure is of a continuous annular step structure, and a plurality of ceramic fiber filtering pipes are arranged on the step surface of each annular step structure, so that the ceramic fiber filtering pipes form a three-dimensional array arrangement, and the integral filtering surface is effectively increased; moreover, the ceramic fiber filter tubes are mutually arranged in a stepped and staggered manner, so that the surrounding gas of each ceramic fiber filter tube has better fluidity, and the filtering efficiency of the ceramic fiber filter tubes is effectively improved; meanwhile, when the pulse soot blower performs soot blowing treatment on the ceramic fiber filter tube, dust falling off from the surface of the ceramic fiber filter tube can also fall rapidly; the invention realizes the dust removal and filtration of the mixed gas formed by mixing the flue gas and the ammonia gas by adopting the ceramic fiber filter tubes arranged in the three-dimensional array, effectively filters particulate matters, alkali metals and other pollutants in the flue gas, prevents the omission of the pollutants, greatly reduces the blockage, abrasion and poisoning of the SCR catalyst, prolongs the service life of the SCR catalyst, and can effectively remove nitrogen oxides in the flue gas by the SCR catalyst.
The above description is only a preferred embodiment of the present patent, and it should be noted that, for those skilled in the art, several modifications and decorations can be made without departing from the inventive concept, and these modifications and decorations should also be regarded as the protection scope of the present patent.

Claims (10)

1. The utility model provides a cement kiln flue gas high temperature denitration dust collector which characterized in that: the denitration device comprises a reactor box body and an ammonia spraying device, wherein the interior of the reactor box body is divided into a left box body and a right box body, the tops of the left box body and the right box body are mutually communicated, a denitration catalyst is arranged in the right box body, an air outlet pipeline is connected onto the right box body below the denitration catalyst, a filtering frame body is arranged in the left box body, a plurality of ceramic fiber filter tubes are arranged on the filtering frame body, a pulse soot blowing device is arranged in the left box body above the filtering frame body, the input end of the pulse soot blowing device is communicated with an external compressed air pipeline, a plurality of blowing pipes corresponding to the plurality of ceramic fiber filter tubes are formed on the pulse soot blowing device, an ash hopper is arranged at the bottom of the left box body, and an ash discharge valve is arranged at the outlet at; the ammonia spraying device comprises a gas collecting pipe, two ends of the gas collecting pipe are respectively communicated with a left box body of the reactor box body through a gas inlet pipeline, the communicating position of the gas inlet pipeline and the left box body of the reactor box body is positioned between a filter frame body and an ash bucket, a shell is sleeved on the gas collecting pipe, a mixed flow cage body structure is rotatably connected on the gas collecting pipe inside the shell, a plurality of gas collecting holes are formed on the gas collecting pipe inside the mixed flow cage body structure, a smoke spraying pipe is arranged on one side outside the shell, an ammonia spraying pipe is arranged on the other side outside the shell, the smoke spraying pipe and the ammonia spraying pipe are respectively parallel to the horizontal plane, the smoke spraying pipe and the ammonia spraying pipe are not on the same horizontal plane, the smoke spraying pipe is communicated with the inside of the shell through a plurality of smoke spraying branch pipes, the ammonia spraying pipe is communicated with the inside of the shell through a plurality of ammonia spraying branch pipes, and a dust bucket is arranged at the bottom, an ash discharge valve is arranged at the outlet at the bottom of the dust hopper.
2. The high-temperature denitration and dust removal device for the flue gas of the cement kiln as claimed in claim 1, wherein the two inlet pipes are not arranged in the right direction of the left box body of the reactor box body, the inlet pipes are sequentially provided with an axial flow fan, a static mixer and a flow guide device in the gas flowing direction, the two axial flow fans on the two inlet pipes work synchronously, the flow guide device is arranged in the inlet pipe at the tail end of the inlet pipe, the flow guide device comprises two transverse plates and two longitudinal plates, and the two transverse plates and the two longitudinal plates are connected in a groined shape.
3. The cement kiln flue gas high-temperature denitration dust removal device as claimed in claim 2, wherein the end of the air inlet pipe is connected with the left box of the reactor box in an inclined manner, and the air inlet direction of the end of the air inlet pipe is inclined upwards.
4. The high-temperature denitration dust removal device for the flue gas of the cement kiln as claimed in claim 1, wherein the smoke spraying pipe is located outside the casing obliquely above the left side of the gas collecting pipe, the ammonia spraying pipe is located outside the casing obliquely below the right side of the gas collecting pipe, and the smoke spraying branch pipe and the ammonia spraying branch pipe are respectively provided with an electromagnetic valve.
5. The high-temperature denitration and dust removal device for the flue gas of the cement kiln as claimed in claim 1, wherein the flow mixing cage structure comprises two parallel end plates, the two end plates are respectively and rotatably connected with the gas collecting pipe through bearings, a plurality of blades are connected between the two end plates, and the plurality of blades uniformly surround the end plates in a circle in the circumferential direction.
6. The high-temperature denitration dust-removing device for the flue gas of the cement kiln as claimed in claim 5, wherein the end plates and the blades are made of aluminum alloy, the thickness of the blades is 2-3mm, the blades comprise a straight edge part and an oblique edge part, two ends of the straight edge part of the blades are respectively and fixedly connected with the two end plates, an included angle between the straight edge part of the blades and a radial axis of the end plates is 135 degrees, and an included angle between the oblique edge part of the blades and the straight edge part of the blades is 135 degrees.
7. The high-temperature denitration dust removal device for the flue gas of the cement kiln as claimed in claim 1, wherein a rake type soot blower is arranged inside the right box body above the denitration catalyst, a reserved catalyst bed layer is arranged inside the right box body above the rake type soot blower, a maintenance opening is arranged on the right box body corresponding to the denitration catalyst and the reserved catalyst bed layer, and a maintenance cover plate is connected to the maintenance opening in a sealing manner.
8. The high-temperature denitration dust removal device for the flue gas of the cement kiln as claimed in claim 1 or 7, wherein the denitration catalyst is a plate-type denitration catalyst, and the pore diameter of the plate-type denitration catalyst is 7 mm; the surface of the plate-type denitration catalyst facing the incoming gas direction is a plane or a spherical surface.
9. The cement kiln flue gas high-temperature denitration dust removal device as claimed in claim 1, wherein an electric hoist is mounted on the top of the outer side of the right box body of the reactor box body, and a vibrator is mounted on the outer side wall surface of the ash bucket.
10. The high-temperature denitration dust-removing device for the flue gas of the cement kiln as claimed in claim 1, wherein the filtering frame body is a hollow conical structure, the outer circumferential surface of the filtering frame body of the hollow conical structure is a continuous annular step structure, a plurality of ceramic fiber filtering pipes are installed on the step surface of each annular step structure, and a plurality of ceramic fiber filtering pipes installed on the step surface of each annular step structure are uniformly arranged in the circumferential direction.
CN201910437647.3A 2019-05-24 2019-05-24 High-temperature denitration dust removal device for flue gas of cement kiln Active CN110152485B (en)

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CN111249881A (en) * 2020-02-25 2020-06-09 四川美富特环境治理有限责任公司 Glass kiln flue gas treatment method and system
CN112138479B (en) * 2020-09-30 2022-04-01 格鼎机电有限公司 Variable air duct dust remover convenient to maintain
CN113083012B (en) * 2021-05-21 2022-10-11 唐山盛通锻造有限公司 Forge and use energy-saving denitration purifier
CN113440938B (en) * 2021-07-16 2022-08-16 扬州工业职业技术学院 Dust removal and filtration device for cement kiln flue gas
CN113457439A (en) * 2021-07-23 2021-10-01 凯盛晶华玻璃有限公司 Integrated technology for dust removal, denitration and desulfurization by coupling fiber pipe and catalyst filtering system
CN113769581A (en) * 2021-09-22 2021-12-10 南京澳博工业智能科技研究院有限公司 Denitration system for improving removal rate of nitrogen oxides in flue gas of cement kiln
CN114432860A (en) * 2021-12-14 2022-05-06 武汉龙净环保工程有限公司 Synergistic removal method for sulfur, nitrate and dust in cement flue gas

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WO2006025900A2 (en) * 2004-08-27 2006-03-09 Cichanowicz J Edward Multi-stage heat absorbing reactor and process for scr of nox and for oxidation of elemental mercury
CN201482419U (en) * 2009-09-04 2010-05-26 中电投远达环保工程有限公司 Pre-dust removal ammonia-injecting mixed flue for SCR denitrification system
CN103120899A (en) * 2013-02-16 2013-05-29 盐城市兰丰环境工程科技有限公司 SCR (silicon controlled rectifier) denitration system of cement kiln gas
CN205055823U (en) * 2015-10-27 2016-03-02 安徽新力电业科技咨询有限责任公司 Use and spout ammonia dust collector in advance in coal fired power plant flue gas

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