CN112426848A - Rubber waste gas treatment device and operation method thereof - Google Patents
Rubber waste gas treatment device and operation method thereof Download PDFInfo
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- CN112426848A CN112426848A CN201910789909.2A CN201910789909A CN112426848A CN 112426848 A CN112426848 A CN 112426848A CN 201910789909 A CN201910789909 A CN 201910789909A CN 112426848 A CN112426848 A CN 112426848A
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- 239000002912 waste gas Substances 0.000 title claims abstract description 151
- 238000011282 treatment Methods 0.000 title claims abstract description 69
- 229920001971 elastomer Polymers 0.000 title claims abstract description 43
- 238000000034 method Methods 0.000 title claims abstract description 21
- 239000007789 gas Substances 0.000 claims abstract description 145
- 239000000428 dust Substances 0.000 claims abstract description 130
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 claims abstract description 71
- 229910021536 Zeolite Inorganic materials 0.000 claims abstract description 69
- 239000010457 zeolite Substances 0.000 claims abstract description 69
- 238000002485 combustion reaction Methods 0.000 claims abstract description 33
- 239000002245 particle Substances 0.000 claims abstract description 17
- 230000000694 effects Effects 0.000 claims abstract description 13
- 239000010815 organic waste Substances 0.000 claims abstract description 11
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims abstract description 8
- 239000005416 organic matter Substances 0.000 claims abstract description 6
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 5
- 229910002092 carbon dioxide Inorganic materials 0.000 claims abstract description 4
- 239000001569 carbon dioxide Substances 0.000 claims abstract description 4
- VUZPPFZMUPKLLV-UHFFFAOYSA-N methane;hydrate Chemical compound C.O VUZPPFZMUPKLLV-UHFFFAOYSA-N 0.000 claims abstract description 4
- 239000004744 fabric Substances 0.000 claims description 57
- 239000000843 powder Substances 0.000 claims description 57
- 238000001179 sorption measurement Methods 0.000 claims description 51
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 49
- 238000003795 desorption Methods 0.000 claims description 49
- 238000001816 cooling Methods 0.000 claims description 32
- 238000005338 heat storage Methods 0.000 claims description 32
- 235000008733 Citrus aurantifolia Nutrition 0.000 claims description 31
- 235000011941 Tilia x europaea Nutrition 0.000 claims description 31
- 239000004571 lime Substances 0.000 claims description 31
- 239000000919 ceramic Substances 0.000 claims description 27
- 238000005507 spraying Methods 0.000 claims description 26
- 230000001172 regenerating effect Effects 0.000 claims description 24
- 230000003647 oxidation Effects 0.000 claims description 13
- 238000007254 oxidation reaction Methods 0.000 claims description 13
- YXFVVABEGXRONW-UHFFFAOYSA-N Toluene Chemical compound CC1=CC=CC=C1 YXFVVABEGXRONW-UHFFFAOYSA-N 0.000 claims description 11
- 238000010438 heat treatment Methods 0.000 claims description 11
- 238000010926 purge Methods 0.000 claims description 11
- 230000009290 primary effect Effects 0.000 claims description 10
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims description 8
- 230000008569 process Effects 0.000 claims description 8
- 238000001914 filtration Methods 0.000 claims description 7
- 238000004140 cleaning Methods 0.000 claims description 6
- 241000410367 Clerodendrum thomsoniae Species 0.000 claims description 5
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- 229930195733 hydrocarbon Natural products 0.000 claims description 4
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- 238000007599 discharging Methods 0.000 description 7
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- 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
- B01D53/02—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 by adsorption, e.g. preparative gas chromatography
- B01D53/06—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 by adsorption, e.g. preparative gas chromatography with moving adsorbents, e.g. rotating beds
-
- 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
- B01D46/02—Particle separators, e.g. dust precipitators, having hollow filters made of flexible material
- B01D46/023—Pockets filters, i.e. multiple bag filters mounted on a common frame
-
- 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
- B01D46/02—Particle separators, e.g. dust precipitators, having hollow filters made of flexible material
- B01D46/04—Cleaning filters
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
- F23G7/00—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals
- F23G7/06—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals of waste gases or noxious gases, e.g. exhaust gases
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
- F23G2209/00—Specific waste
- F23G2209/14—Gaseous waste or fumes
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- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Environmental & Geological Engineering (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Treating Waste Gases (AREA)
Abstract
本发明涉及一种橡胶废气处理装置及其操作方法，所属工业废气处理技术领域，所述的橡胶废气处理装置包括：废气流动通道、布袋除尘器、干式过滤器、沸石转轮、RTO焚烧炉、废气输入口和气体排放口。本处理装置中，含油性颗粒物的废气先经布袋除尘器，油性颗粒物通过布袋过滤，再通过干式过滤器去除橡胶废气中的细微粉尘，接着通过沸石转轮吸附浓缩有机废气，浓缩后的有机废气进入RTO焚烧炉内，在燃烧室内将橡胶废气中的有机成分氧化成二氧化碳和水，实现废气的净化。本发明通过对废气分层、多级的处理，依次逐步去除废气中的油性颗粒物、细微粉尘和有机物，具有废气处理效果好、效率高等特点，特别适合处理大风量、低浓度的橡胶废气。
The invention relates to a rubber waste gas treatment device and an operation method thereof, belonging to the technical field of industrial waste gas treatment. The rubber waste gas treatment device comprises: a waste gas flow channel, a bag filter, a dry filter, a zeolite runner, and an RTO incinerator , exhaust gas inlet and gas discharge port. In this treatment device, the waste gas containing oily particles is first passed through a bag filter, the oily particles are filtered through a bag, and then the fine dust in the rubber waste gas is removed by a dry filter, and then the organic waste gas is adsorbed and concentrated by a zeolite rotor. The waste gas enters the RTO incinerator, and the organic components in the rubber waste gas are oxidized into carbon dioxide and water in the combustion chamber to realize the purification of the waste gas. The invention gradually removes oily particulate matter, fine dust and organic matter in the exhaust gas by stratifying and multi-stage treatment of the exhaust gas, and has the characteristics of good exhaust gas treatment effect and high efficiency, and is especially suitable for treating rubber exhaust gas with large air volume and low concentration.
Description
Technical Field
The invention relates to the technical field of industrial waste gas treatment, in particular to a rubber waste gas treatment device and an operation method thereof.
Background
The continuous growth of the rubber industry is promoted along with the acceleration of the industrial modernization pace, and meanwhile, a large amount of waste gas is also generated in the rubber mixing process, the waste gas not only contains VOCs, but also contains a large amount of oil mist and dust, and meanwhile, the waste gas in the rubber industry belongs to the waste gas with large air volume and low concentration. With the improvement of awareness of environmental protection of people, the waste gas treatment in the rubber industry becomes the focus of attention of people, and the rubber industry is specially provided with the emission standard of pollutants in the rubber product industry in 2011, and along with the trend, the rubber waste gas treatment technology grows like the breeding of bamboo shoots in spring after rain.
The existing treatment technologies adopted by the waste gas in the rubber industry comprise an activated carbon adsorption method, a low-temperature plasma method, a photocatalytic oxidation method and the like, and the methods generally have the defects of low removal efficiency and unstable operation and cannot meet the overall emission requirement of large-air-volume waste gas treatment in the rubber industry.
Chinese utility model patent CN201520707584.6, granted announcement date 2016 No. 1/6, discloses a rubber waste gas purification device, rubber waste gas passes through the filter equipment at first, realizes the removal of dust, ensures the continuous stable operation of follow-up purification device; then the mixture is conveyed to a photocracking device to primarily degrade pollutants; finally, conveying the waste gas to a spraying device to achieve the aim of thoroughly degrading VOCs in the waste gas, and discharging the clean gas through a fan; under the combined action of the ultraviolet light generated by the ultraviolet light generating device and the oxidant generated by the oxidant storage device, the organic pollutants are removed, and the crystal water is circulated to the spraying device. However, the waste gas purification device has low removal efficiency, large overall energy consumption and poor stability, and the oxidant and the medium in the filter device need to be replaced in the operation process, so that the required operation cost is high, and the waste gas purification device is not suitable for treating large-air-volume waste gas generated in the rubber industry.
Disclosure of Invention
The invention aims to solve the problem of organic waste gas containing oil particles with large air volume and low concentration in the rubber industry, and provides a waste gas treatment device with good treatment effect, high efficiency and stable operation and an operation method thereof.
The technical scheme adopted by the invention for solving the technical problems is as follows: a rubber exhaust treatment device is characterized in that: comprises a waste gas flow channel, a bag-type dust collector, a dry filter, a zeolite rotating wheel, an RTO incinerator and a waste gas discharge port, wherein the bag-type dust collector, the dry filter, the zeolite rotating wheel and the RTO incinerator are sequentially arranged on the waste gas flow channel in the waste gas flow direction, and the front end and the tail end of the waste gas flow channel are respectively provided with the waste gas inlet and the gas.
Further, the bag-type dust collector is an external filter type filter and comprises a gas purifying chamber and a dust removing chamber; the air purifying chamber comprises a pulse device and an air outlet, and the pulse device comprises a pulse valve, an air bag, a compressed air conveying pipe and a small-caliber nozzle; the pulse valve and the air bag are arranged outside one side of the air purifying chamber and are connected through a compressed air conveying pipe; the compressed gas conveying pipe and the small-caliber spray nozzle are arranged at the lower end in the gas purifying chamber, and the small-caliber spray nozzle is arranged on the compressed gas conveying pipe; the air outlet is arranged at the other side of the air purifying chamber and connected with a waste gas flow channel, and an outlet valve is arranged on the waste gas flow channel connected with the air outlet.
Furthermore, the dust chamber comprises an air inlet, a baffle, a cloth bag supporting framework, a cloth bag hanging flower plate, an ash discharge hopper, an ash discharge valve and a dust collector; the lower end of one side of the dust removing chamber is provided with an air inlet which is connected with a waste gas flow channel, the waste gas flow channel connected with the air inlet is provided with a lime powder inlet, the lime powder inlet is connected with an automatic powder spraying device, the automatic powder spraying device comprises a fan, a discharger and a powder tank, and an inlet valve is arranged on the waste gas flow channel which is close to one side of the lime powder inlet and far away from the air inlet; a baffle is arranged beside the air inlet; the bottom of the dust chamber is provided with an ash discharge hopper, an ash discharge valve and a dust collector, the ash discharge valve is arranged at the bottom of the ash discharge hopper, and the dust collector is arranged right below the ash discharge valve; the dust removal chamber in set up the sack of fabric, the sack sets up under small-bore nozzle, connects through hanging the sack card at dust removal chamber top, the sack inside set up sack and support the skeleton.
Furthermore, the dry filter comprises three parts, namely a primary treatment area, an activated carbon treatment area and an intermediate treatment area; a primary effect filter bag is arranged in the primary effect treatment area and is connected through a dry filter hanging cloth bag pattern plate at the top of the primary effect treatment area; active carbon is arranged in the active carbon treatment area; the middle-effect treatment is internally provided with a middle-effect filter bag which is connected through a dry filter hanging cloth bag pattern plate at the top of the middle-effect treatment area.
Furthermore, the lower end of one side of the dry filter is provided with a dry filter air inlet which is connected with an exhaust gas flow channel, one side close to the dry filter air inlet is provided with a dry filter baffle plate, the exhaust gas flow channel connected with the dry filter air inlet is provided with an inlet valve, the upper end of the other side of the dry filter is provided with a dry filter air outlet which is connected with the exhaust gas flow channel, and the exhaust gas flow channel connected with the dry filter air outlet is provided with an outlet valve; the upper end of the dry filter is provided with a dry filter pulse device which comprises a dry filter pulse valve, a dry filter air bag, a dry filter compressed gas conveying pipe and a dry filter small-caliber nozzle, the dry filter pulse valve, the dry filter air bag and the dry filter small-caliber nozzle are connected through the dry filter compressed gas conveying pipe, and the bottom of the dry filter is provided with a dry filter dust collector.
Furthermore, the zeolite rotating wheel mainly comprises an adsorption area, a desorption area and a cooling area, and the zeolite rotating wheel is driven by a motor to rotate at a constant speed to sequentially pass through the adsorption area, the desorption area and the cooling area; one side of the adsorption area is provided with an adsorption area air inlet which is connected with a waste gas flow channel, and the other side of the adsorption area is provided with an adsorption area air outlet which is connected with the waste gas flow channel.
Furthermore, one side of the cooling area is provided with a fresh air inlet through which fresh air is blown in by a blower, the other side of the cooling area is provided with an air outlet which is connected with a preheating device for heating air, the heated air is connected into the desorption area through a pipeline, and the other side of the desorption area is connected into the RTO incinerator through a waste gas flow channel.
Furthermore, the RTO incinerator adopts a fixed three-chamber regenerative incinerator and mainly comprises a regenerative chamber A, a regenerative chamber B, a regenerative chamber C and a combustion chamber, wherein a combustor is arranged in the combustion chamber, and honeycomb regenerative ceramics are arranged on the inner wall of the regenerative chamber.
Furthermore, the lower end of the RTO incinerator is provided with three air inlet pipes, three exhaust pipes and three purging air pipes, the air inlet pipes, the exhaust pipes and the purging air pipes are all provided with valves, and the air inlet pipes and the exhaust pipes are all connected with a waste gas flow channel.
Furthermore, all set up the draught fan on sack cleaner, dry-type filter, zeolite runner and the RTO burns burning furnace's the waste gas flow path, the zeolite runner sets up two draught fans, respectively on the waste gas flow path of connecting behind adsorption zone and desorption zone.
A rubber exhaust treatment device is characterized in that: the method is characterized in that a pretreatment, adsorption concentration and heat storage incineration device is adopted, and a bag-type dust remover of the pretreatment device is used for preventing impurities containing oil dust particles, dust and the like in rubber waste gas from entering a zeolite rotating wheel and depositing in a honeycomb structure of zeolite to influence the adsorption capacity of the zeolite on organic matters and even influence the normal operation of the zeolite rotating wheel; meanwhile, the dry filter is arranged behind the bag-type dust collector, so that particle dust with smaller particle size can be effectively filtered, and the service life of the zeolite rotating wheel is prolonged;
the pretreatment equipment is provided with a pulse device, the active carbon treatment area of the dry filter is provided with a dry filter pulse device, once the active carbon is in a saturated state, the dry filter pulse device is started to desorb the active carbon, so that the active carbon can be recycled, and the operation cost of the rubber waste gas treatment device is reduced.
The rubber waste gas treatment device comprises the following specific operation steps:
the method comprises the following steps: pretreatment process
The first step is as follows: the following situations require automatic powder spraying: a. before the new cloth bag is used; b. after pulse ash removal; c. re-commissioning after size repair; d. the bag-type dust collector is started after being stopped for 48 hours; pre-spraying lime powder of about 200 meshes by using a bag-type dust remover;
the second step is that: opening an inlet valve and an outlet valve of the bag-type dust collector, and starting an induced draft fan to enable the bag-type dust collector to form a state that an air inlet is filled with air and an air outlet is exhausted from the air outlet;
the third step: opening a discharge valve below the ash discharge hopper, starting a fan, blowing the lime powder falling into a pipeline to a waste gas flow channel connected with an air inlet of a bag-type dust remover, feeding the lime powder into the bag-type dust remover along with the air of the draught fan, so that the lime powder is attached to the surface of a bag, and forming a lime powder layer on the surface of the bag; when the pressure difference between the inlet and the outlet of the bag-type dust collector reaches 200-400 pa, closing the discharger and the fan, and finishing automatic powder spraying;
the fourth step: checking the cloth bag to determine whether leakage of the pattern plate and bag breaking and dropping of the cloth bag occur;
the fifth step: after the dust remover is started, dust-containing waste gas enters from the gas inlet, under the guidance of the baffle plate, large-particle dust is separated and then directly falls into the dust hopper, the dust-containing waste gas enters a cloth bag area in the dust removing chamber along with gas flow, the dust in the waste gas is intercepted outside a cloth bag of a fiber fabric, the waste gas passing through the cloth bag achieves the effect of removing the dust, and the dust enters a waste gas flow channel through the gas purifying chamber and the gas outlet; the lime powder layer formed on the surface of the cloth bag by automatically spraying the powder can prevent oily particles from being adhered to the filtering surface of the cloth bag, so that the bag pasting is avoided;
and a sixth step: when the bag-type dust collector operates for a period of time, the pressure difference of an inlet and an outlet rises, and when the pressure difference reaches a set value (1500 pa), ash is removed by pulse according to a set program; opening the pulse valves one by one, jetting high-pressure gas through a small-caliber nozzle, and blowing dust attached to the surface of the cloth bag into the dust hopper; wherein the pulse time is set to 100 ms, and the blowing interval is set to 1-60 s; after the pulse is finished, automatically spraying powder to form a lime powder layer on the surface of the cloth bag, continuously filtering dust-containing waste gas after the powder is automatically sprayed, and repeating the steps; when the dust in the dust hopper reaches a certain amount, the dust discharging valve is opened to enable the dust to fall into the dust collector, and the dust is periodically cleaned.
The seventh step: starting the dry filter, wherein the waste gas treated by the bag-type dust collector enters from an air inlet of the dry filter, sequentially passes through an effective filter bag of the primary filter area, the active carbon of the active carbon treatment area and an intermediate filter bag of the intermediate filter area, is finally discharged from an air outlet of the dry filter and enters a waste gas flow channel;
eighth step: when the pressure difference of the inlet and the outlet of the dry filter reaches a set value, closing an air inlet valve of the dry filter, opening a pulse valve of the dry filter, spraying compressed gas from a small-caliber nozzle of the dry filter, and blowing off fine dust attached to the surface of the cloth bag and in the active carbon gap structure; after the pulse is finished, continuing filtering the fine dust, and repeating the steps; the dust in the dry filter dust collector is regularly cleaned.
Step two: an adsorption concentration process;
the first step is as follows: starting a zeolite rotating wheel, allowing waste gas to enter from an air inlet of an adsorption area of the zeolite rotating wheel, adsorbing methylbenzene and non-methane total hydrocarbon in the waste gas in a honeycomb structure of zeolite, discharging the adsorbed gas from an air outlet of the adsorption area, connecting the gas to a waste gas flow channel, converging the gas with the gas oxidized by an RTO incinerator, and discharging the gas up to the standard;
the second step is that: fresh air enters a cooling zone through a fresh air inlet, zeolite in the cooling zone is cooled, a part of heat energy is absorbed, the fresh air which absorbs the part of the heat energy is discharged from the cooling zone and enters a preheating device for heating air to heat the fresh air, the fresh air is heated to about 180 ℃, and the heated fresh air is connected to a desorption zone;
the third step: heating and then connecting the heated zeolite to a desorption area, so that organic matters adsorbed in the zeolite in the desorption area are desorbed under the action of high temperature and are taken away by fresh air, and the organic matters are discharged from an air outlet of the desorption area at the other side of the desorption area and are connected to an RTO incinerator through a waste gas flow channel; the ratio of the heated fresh air entering the desorption zone to the waste gas entering the adsorption zone is 1/3-1/10, and the concentration of organic matters in the fresh air connected to the RTO incinerator can reach 10 times of the concentration before treatment.
The fourth step: the zeolite runner is through the constant speed gyration under the drive of motor in proper order through adsorption zone, desorption district and cooling space, and the zeolite that has adsorbed organic matter transfers to the desorption district, carries out high temperature desorption in the desorption district, and the zeolite that has desorbed transfers to the cooling space, cools off in the cooling space, and the zeolite gyration after the cooling is adsorbed to the adsorption space again, and is so repeated.
Step three: a regenerative combustion process;
the first step is as follows: opening a valve of the regenerator A, allowing the organic waste gas passing through the desorption region of the zeolite rotating wheel to enter the regenerator A (the honeycomb heat storage ceramic retains the heat of the previous cycle and is in a high-temperature state) through an induced draft fan, allowing the honeycomb heat storage ceramic to release the heat and reduce the temperature, allowing the organic waste gas to absorb the heat and increase the temperature, purging the regenerator A in the next cycle, allowing the residual waste gas in the regenerator A to enter a combustion chamber for oxidation, allowing the waste gas to flow through the regenerator A, then allowing the waste gas to enter the combustion chamber at a higher temperature for preparation for oxidation, and allowing the temperature of the waste gas to depend on the volume of the ceramic body, the flow speed of the waste gas;
the second step is that: in the combustion chamber, the waste gas is heated by a burner to reach an oxidation temperature, wherein the temperature is set to 800-850 ℃, so that the organic components in the waste gas are decomposed into carbon dioxide and water; because the waste gas is preheated in the regenerative chamber A, the fuel consumption is greatly reduced; the combustion chamber has two functions: firstly, ensuring that the waste gas can reach the set oxidation temperature, and secondly, ensuring that enough residence time is available to fully oxidize the organic components in the waste gas;
the third step: the waste gas is oxidized by the combustion chamber to form clean gas, and then the clean gas leaves the combustion chamber and enters a regenerator B blown by the previous cycle (at the moment, the honeycomb heat storage ceramic is in a low temperature state), the clean gas releases a large amount of heat in the regenerator B to the honeycomb heat storage ceramic, the gas is discharged after being cooled, is connected to a waste gas flow channel, is converged with the gas discharged by the zeolite rotating wheel adsorption area and then is discharged after reaching the standard, the honeycomb heat storage ceramic absorbs a large amount of heat and then is heated, and the absorbed heat is used for preheating the waste gas in the next cycle;
the fourth step: the regenerator C is in a cleaning state, when the valve is switched after the previous cycle is finished, a small amount of waste gas is stored between the valve and the honeycomb heat storage ceramic, the fresh air is adopted for blowing, and the waste gas is blown to the combustion chamber, and the regenerator C is used for exhausting gas of the next cycle;
the fifth step: the next circulation waste gas enters from the heat storage chamber B and is discharged from the heat storage chamber C, and the heat storage chamber A is purged; and the next time of circulating waste gas enters from the heat storage chamber C and is discharged from the heat storage chamber A, and the heat storage chamber B is purged and repeatedly and alternately exchanged.
Drawings
The invention will be further described with reference to the accompanying drawings in which:
FIG. 1 is a schematic diagram of the overall structure of an embodiment of the present invention;
FIG. 2 is a schematic structural diagram of a bag-type dust collector in an embodiment of the present invention;
FIG. 3 is a schematic view of a dry filter construction according to an embodiment of the present invention;
FIG. 4 is a schematic structural diagram of a zeolite wheel according to an embodiment of the present invention;
FIG. 5 is a schematic structural view of an RTO incinerator according to an embodiment of the present invention.
In the figure: 1 waste gas flow channel, 2 bag dust collector, 3 dry filter, 4 zeolite rotating wheel, 5RTO incinerator, 6 waste gas input port, 7 induced draft fan, 8 fresh air inlet, 9 gas discharge port, 10 air purification chamber, 11 dust removal chamber, 12 air inlet, 13 lime powder air inlet, 14 baffle, 15 pulse device, 16 pulse valve, 17 air bag, 18 compressed gas delivery pipe, 19 small-bore nozzle, 20 hanging bag pattern board, 21 bag, 22 bag support frame, 23 ash discharge valve, 24 dust collector, 25 ash discharge hopper, 26 automatic powder spraying device, 27 fan, 28 discharger, 29 powder tank, 30 gas outlet, 31 primary effect processing area, 32 active carbon processing area, 33 intermediate effect processing area, 34 dry filter air inlet, 35 dry filter baffle, 36 primary effect filter bag, 37 active carbon, 38 intermediate effect filter bag, 39 dry filter pulse device, 40 dry filter pulse valve, 41 dry filter air bag, 42 dry filter compressed gas delivery pipe, 43 dry filter small-caliber nozzle, 44 dry filter hanging cloth bag card, 45 dry filter dust collector, 46 dry filter air outlet, 47 adsorption zone, 48 desorption zone, 49 cooling zone, 50 preheating device for heating air, 51 adsorption zone air inlet, 52 fresh air inlet, 53 adsorption zone air outlet, 54 fresh air outlet, 55 desorption zone air inlet, 56 desorption zone air outlet, 57 zeolite, 58 motor, 59 combustion chamber, 60 combustor, 61 heat storage chamber A, 62 heat storage chamber B, 63 heat storage chamber C, 64 honeycomb ceramic, 65 air inlet pipe, 66 exhaust pipe, 67 purging air pipe, 68 valve, 69 inlet valve and 70 outlet valve.
Detailed Description
To further illustrate the technical means and effects of the present invention adopted to achieve the predetermined objects, the following description, with reference to fig. 1-5 and preferred embodiments, provides a rubber waste gas treatment device, which mainly comprises a waste gas flow channel 1, and a bag-type dust collector 2, a dry filter 3, a zeolite rotating wheel 4, an RTO incinerator 5, and a waste gas inlet 6 and a gas outlet 9 respectively disposed at the front end and the rear end of the waste gas flow channel 1, which are sequentially disposed on the waste gas flow channel 1 according to the waste gas flow direction.
In the treatment device, waste gas sequentially passes through a bag-type dust collector 2, a dry filter 3, a zeolite rotating wheel 4 and an RTO incinerator 5 through a flow channel 1, and is discharged through a gas discharge port 9 after being purified; the treatment device gradually removes oily particles, fine dust, toluene, non-methane total hydrocarbon and other organic matters in the waste gas in sequence through layered and multistage treatment on the waste gas, has the characteristics of good waste gas treatment effect, high efficiency and the like, and is particularly suitable for treating the rubber waste gas with large air volume and low concentration.
As a preferred embodiment of the present invention, the bag-type dust collector 2 is an external filter type filter, and comprises an air purifying chamber 10 and a dust removing chamber 11; the gas purifying chamber 10 comprises a pulse device 15 and a gas outlet 30, the pulse device 15 comprises a pulse valve 16, a gas bag 17, a compressed gas conveying pipe 18 and a small-caliber nozzle 19, the pulse valve 16 and the gas bag 17 are arranged outside one side of the gas purifying chamber 10 and are connected through the compressed gas conveying pipe 18, the compressed gas conveying pipe 18 and the small-caliber nozzle 19 are arranged at the lower end inside the gas purifying chamber 10, the small-caliber nozzle 19 is arranged on the compressed gas conveying pipe 18, the gas outlet 30 is arranged on the other side of the gas purifying chamber 10 and is connected with a waste gas flow channel 1, and an outlet valve 70 is arranged on the waste gas flow channel connected with the gas outlet 30; the dust chamber 11 comprises an air inlet 12, a baffle 14, a cloth bag hanging pattern plate 20, a cloth bag 21, a cloth bag supporting framework 22, an ash discharge hopper 25, an ash discharge valve 23 and a dust collector 24; the lower end of one side of the dust removing chamber 11 is provided with an air inlet 12 which is connected with a waste gas flow channel 1, a lime powder inlet 13 is arranged on the waste gas flow channel 1 which is connected with the air inlet 12, the lime powder inlet 13 is connected with an automatic powder spraying device 26, and the automatic powder spraying device 26 comprises a fan 27, a discharger 28 and a powder tank 29; an inlet valve 69 is arranged on the waste gas flowing channel 1 close to the lime powder inlet 13 and far away from the inlet 12; the other baffle 14 that sets up of air inlet 12, 11 bottoms of clean room set up unloading bucket 25, unloading valve 23 and dust arrester 24, unloading valve 23 set up in unloading bucket 25 bottoms, dust arrester 24 sets up under unloading valve 23, clean room 11 in set up fiber fabric's sack 21, sack 21 set up under small-bore nozzle 19, connect through hanging sack card 20 at 11 tops of clean room, sack 21 is inside to set up sack supporting framework 22.
As a preferred embodiment of the present invention, the dry filter 3 includes three parts, a primary treatment zone 31, an activated carbon treatment zone 32, and an intermediate treatment zone 33; a primary effect filter bag 36 is arranged in the primary effect treatment area 31, the primary effect filter bag 36 is connected through a dry filter cloth hanging bag flower plate 44 at the top of the primary effect treatment area 31, active carbon 37 is arranged in the active carbon treatment area 32, a medium effect filter bag 38 is arranged in the medium effect treatment area 33, and the medium effect filter bag 38 is connected through the dry filter cloth hanging bag flower plate 44 at the top of the medium effect treatment area 33; the lower end of one side of the dry filter 3 is provided with a dry filter air inlet 34 which is connected with the waste gas flow channel 1, one side close to the dry filter air inlet 34 is provided with a dry filter baffle 35, the waste gas flow channel 1 connected with the dry filter air inlet 34 is provided with an inlet valve 69, the upper end of the other side of the dry filter 3 is provided with a dry filter air outlet 46 which is connected with the waste gas flow channel 1, and the waste gas flow channel 1 connected with the air outlet is provided with an outlet valve 70; the dry filter 3 is provided with a dry filter pulse device 39 at the upper end thereof, which comprises a dry filter pulse valve 40, a dry filter air bag 41, a dry filter compressed gas delivery pipe 42 and a dry filter small-diameter nozzle 43, the dry filter pulse valve 40, the dry filter air bag 41 and the dry filter small-diameter nozzle 43 are connected by the dry filter compressed gas delivery pipe 42, and the dry filter dust collector 45 is provided at the lower end thereof.
As a preferred embodiment of the present invention, the zeolite rotating wheel 4 mainly comprises an adsorption zone 47, a desorption zone 48 and a cooling zone 49, wherein one side of the adsorption zone 47 is provided with an adsorption zone air inlet 51 connected with the waste gas flow channel 1, and the other side of the adsorption zone 47 is provided with an adsorption zone air outlet 53 connected with the waste gas flow channel 1; a fresh air inlet 52 is arranged on one side of the cooling area 49, fresh air is blown in through a blower, a fresh air outlet 54 is arranged on the other side of the cooling area 49 and is connected with a preheating device 50 for heating air, the heated air is connected into the desorption area 48 through a pipeline, and the other side of the desorption area 48 is connected into the RTO incinerator 5 through a waste gas flow channel 1.
As a preferred embodiment of the present invention, the RTO incinerator 5 is a fixed three-chamber regenerative incinerator, which mainly comprises a regenerative chamber a61, a regenerative chamber B62, a regenerative chamber C63 and a combustion chamber 59, wherein a burner 60 is arranged in the combustion chamber 59, and a honeycomb regenerative ceramic 64 is arranged on the inner wall of the regenerative chamber; the lower end of the RTO incinerator 5 is provided with three air inlet pipes 65, three exhaust pipes 66 and three purging air pipes 67, the air inlet pipes 65, the exhaust pipes 66 and the purging air pipes 67 are all provided with valves 68, and the air inlet pipes 65 and the exhaust pipes 66 are all connected with the waste gas flow channel 1.
The rubber waste gas treatment device comprises: organic waste gas filters oily particles and dust through a cloth bag 21, fine dust which is not removed by a cloth bag dust remover 2 is removed through three treatment areas of a dry filter 3, then the organic waste gas with large air volume and low concentration is concentrated into organic waste gas with small air volume and high concentration through a zeolite rotating wheel 4, the concentrated waste gas enters an RTO incinerator 5, rubber waste gas is oxidized in a combustion chamber 59, organic matters in the rubber waste gas are converted into carbon dioxide and water, the waste gas is purified, and the treated gas is discharged from a gas discharge port 9;
specifically, a pretreatment device, an adsorption concentration device and a heat storage incineration device are adopted, wherein a bag-type dust collector 2 of the pretreatment device is used for preventing oily dust, particulate matters and other impurities in rubber waste gas from entering a zeolite rotating wheel 4 and depositing in a honeycomb structure of zeolite 57, so that the adsorption capacity of the zeolite on organic matters is influenced, and even the normal operation of the zeolite rotating wheel is influenced; meanwhile, the dry filter 3 arranged behind the bag-type dust collector 2 can effectively filter dust with smaller particle size, and the service life of the zeolite rotating wheel 4 is prolonged;
the pretreatment equipment is provided with a pulse device, the active carbon treatment area 32 of the dry filter 3 is provided with a dry filter pulse device 39, once the active carbon 37 is in a saturated state, the dry filter pulse device 39 is started to desorb the active carbon 37, so that the active carbon 37 can be recycled, and the running cost of the rubber waste gas treatment device is reduced.
The rubber waste gas treatment device comprises the following specific operation steps:
the method comprises the following steps: pretreatment process
The first step is as follows: the following situations require automatic powder spraying: a. the new cloth bag 21 is before use; b. after pulse ash removal; c. re-commissioning after size repair; d. the bag-type dust collector 2 is started after being stopped for 48 hours; pre-spraying lime powder of about 200 meshes by using a bag-type dust remover;
the second step is that: firstly, opening an inlet valve 69 and an outlet valve 70 of the bag-type dust collector 2, and starting the induced draft fan 7 to enable the bag-type dust collector 2 to form a state that air enters from an air inlet 12 and air exits from an air outlet 30;
the third step: opening a discharge valve 23 below an ash discharge hopper 25, starting a fan 27, blowing the lime powder falling into a pipeline to a waste gas flow channel 1 connected with an air inlet 12 of a bag-type dust collector 2, feeding the lime powder into the bag-type dust collector 2 along with the air of an induced draft fan 7, and enabling the lime powder to be attached to the surface of a bag 21 to form a lime powder layer on the surface of the bag; when the pressure difference between the inlet and the outlet of the bag-type dust collector 2 reaches 200-400 pa, closing the discharger 28 and the fan 27, and finishing automatic powder spraying;
the fourth step: checking the cloth bag to determine whether leakage of the pattern plate occurs or not and whether the cloth bag 21 breaks or falls;
the fifth step: after the dust remover is started, dust-containing waste gas enters from the air inlet 12, under the guidance of the baffle 35 of the dry filter, large-particle dust is separated and then directly falls into the dust hopper 25, the dust-containing waste gas enters into a cloth bag area in the dust removing chamber 11 along with air flow, dust in the waste gas is intercepted outside a cloth bag 21 of a fiber fabric, the waste gas passing through the cloth bag 21 achieves the effect of removing the dust, and the dust enters the waste gas flowing channel 1 through the air purifying chamber 10 and the air outlet 30; the lime powder layer formed on the surface of the cloth bag 21 by automatically spraying powder can prevent oily particles from being adhered to the filtering surface of the cloth bag 21, so that the bag pasting cannot be caused;
and a sixth step: when the bag-type dust collector 2 operates for a period of time, the pressure difference of an inlet and an outlet rises, and when the pressure difference reaches a set value (1500 pa), ash is removed by pulse according to a set program; the pulse valves 16 are opened one by one, high-pressure gas is sprayed through the small-caliber spray nozzles 19, and dust attached to the surfaces of the cloth bags 21 is blown into the dust discharge hopper 25; wherein the pulse time is set to 100 ms, and the blowing interval is set to 1-60 s; after the pulse is finished, automatically spraying powder to form a lime powder layer on the surface of the cloth bag, continuously filtering dust-containing waste gas after the powder is automatically sprayed, and repeating the steps; when the dust in the hopper 25 reaches a certain amount, the dust discharge valve 23 is opened to drop the dust into the dust collector 24 for periodic cleaning.
The seventh step: starting the dry filter 3, allowing the waste gas treated by the bag-type dust collector 2 to enter from an air inlet 34 of the dry filter, sequentially passing through an effective filter bag 36 of the primary filter area 31, the activated carbon 37 of the activated carbon treatment area 32 and an intermediate filter bag 38 of the intermediate filter area 33, and finally discharging from an air outlet 46 of the dry filter to enter the waste gas flow channel 1;
eighth step: when the pressure difference between the inlet and the outlet of the dry filter 3 reaches a set value, the air inlet valve 69 of the dry filter 3 is closed, the pulse valve 40 of the dry filter is opened, the compressed gas is sprayed from the small-caliber nozzle 19 of the dry filter, and the fine dust attached to the surface of the cloth bag 21 and in the gap structure of the activated carbon 37 is blown off; after the pulse is finished, continuing filtering the fine dust, and repeating the steps; the dust in the dry filter dust collector 45 is periodically cleaned.
Step two: an adsorption concentration process;
the first step is as follows: starting the zeolite rotating wheel 4, allowing waste gas to enter from an air inlet 51 of an adsorption area of the zeolite rotating wheel 4, allowing toluene and non-methane total hydrocarbons in the waste gas to be adsorbed in a honeycomb structure of zeolite 57, discharging the adsorbed gas from an air outlet 53 of the adsorption area, connecting the gas to a waste gas flow channel 1, converging the gas oxidized by the RTO incinerator 5, and discharging the gas up to the standard;
the second step is that: fresh air enters the cooling zone 49 through the fresh air inlet 52, cools the zeolite 57 of the cooling zone 49, absorbs a part of heat energy, the fresh air which absorbs a part of the heat energy is discharged from the cooling zone 49 and enters the preheating device 50 for heating air, the fresh air is heated to about 180 ℃, and the heated fresh air is connected to the desorption zone 48;
the third step: heating and then connecting the desorption area 48, so that organic matters adsorbed in the zeolite 57 in the desorption area 48 are desorbed under the action of high temperature and are taken away by fresh air, and the organic matters are discharged from an air outlet 56 of the desorption area at the other side of the desorption area 48 and are connected to the RTO incinerator 5 through a waste gas flow channel 1; the ratio of the heated fresh air entering the desorption zone 48 to the exhaust gas entering the adsorption zone 47 is 1/3-1/10, and the concentration of organic matters in the fresh air introduced into the RTO incinerator can reach 10 times of the concentration before treatment.
The fourth step: the zeolite rotating wheel 4 is driven by a motor 58 to rotate at a constant speed to sequentially pass through the adsorption area 47, the desorption area 48 and the cooling area 49, the zeolite 57 adsorbing organic matters is transferred to the desorption area 48, high-temperature desorption is carried out in the desorption area 48, the desorbed zeolite 57 is transferred to the cooling area 49 and is cooled in the cooling area 49, the cooled zeolite 57 rotates to the adsorption area 47 to be adsorbed again, and the process is repeated.
Step three: a regenerative combustion process;
the first step is as follows: opening a valve 68 of a regenerator A61, allowing the organic waste gas passing through a desorption region 48 of the zeolite rotating wheel 4 to enter a regenerator A61 (the honeycomb heat storage ceramic 64 retains the heat of the previous cycle and is in a high-temperature state), allowing the honeycomb heat storage ceramic 64 to release heat and reduce the temperature, allowing the organic waste gas to absorb heat and increase the temperature, purging the regenerator A61 in the next cycle, allowing the residual waste gas in the regenerator A61 to enter a combustion chamber 59 for oxidation, allowing the waste gas to flow through the regenerator A61 and enter the combustion chamber 59 at a higher temperature for preparation for oxidation, wherein the temperature of the waste gas depends on the volume of the ceramic body, the flow speed of the waste gas and the geometric structure of the ceramic body;
the second step is that: in the combustion chamber 59, the exhaust gas is heated by the burner 60 to reach the oxidation temperature, at which time the temperature is set to 800-; since the exhaust gas has been preheated in regenerator A61, fuel consumption is greatly reduced; the combustion chamber has two functions: firstly, ensuring that the waste gas can reach the set oxidation temperature, and secondly, ensuring that enough residence time is available to fully oxidize the organic components in the waste gas;
the third step: the waste gas is oxidized into clean gas by the combustion chamber 59, then the clean gas leaves the combustion chamber 59, enters the regenerator B62 blown by the previous cycle (at the moment, the honeycomb heat storage ceramic 64 is in a low temperature state), the clean gas releases a large amount of heat in the regenerator B62 to the honeycomb heat storage ceramic 64, the gas is discharged after being cooled, is connected to the waste gas flow channel 1, is converged with the gas discharged from the adsorption area 47 of the zeolite rotating wheel 4 and then is discharged after reaching the standard, the honeycomb heat storage ceramic 64 absorbs a large amount of heat and then is heated, and the absorbed heat is used for preheating the waste gas in the next cycle;
the fourth step: when the valve 68 is switched at the end of the previous cycle, a small amount of waste gas is stored between the valve 68 and the honeycomb heat storage ceramic 64 and is blown to the combustion chamber 59 by adopting fresh air, and the heat storage chamber C63 is in a cleaning state, and the heat storage chamber C63 is used for the exhaust of the next cycle;
the fifth step: the next circulation of waste gas enters from the regenerator B62 and is discharged from the regenerator C63, and the regenerator A61 is purged; the next time of circulating waste gas enters from the heat storage chamber C63 and is discharged from the heat storage chamber A61, and the heat storage chamber B62 is purged, and the circulation and the replacement are repeated.
Although the present invention has been described with reference to a preferred embodiment, it should be understood that various changes, substitutions and alterations can be made herein without departing from the spirit and scope of the invention as defined by the appended claims.
Claims (12)
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| CN114137569A (en) * | 2021-09-26 | 2022-03-04 | 碧空环境科技有限公司 | Pollution traceability system based on laser radar and unmanned aerial vehicle combination |
| CN114151805A (en) * | 2021-09-30 | 2022-03-08 | 碧空环境科技有限公司 | Method for treating coated waste gas by combining air-reducing and thickening system with RTO (regenerative thermal oxidizer) |
| CN116510452A (en) * | 2023-05-29 | 2023-08-01 | 兰溪华能输送设备制造有限公司 | Air box type pulse bag dust collector |
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