CN110818220B - Sludge low-temperature drying coupling pyrolysis system - Google Patents
Sludge low-temperature drying coupling pyrolysis system Download PDFInfo
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- CN110818220B CN110818220B CN201911065734.7A CN201911065734A CN110818220B CN 110818220 B CN110818220 B CN 110818220B CN 201911065734 A CN201911065734 A CN 201911065734A CN 110818220 B CN110818220 B CN 110818220B
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- 239000010802 sludge Substances 0.000 title claims abstract description 196
- 238000000197 pyrolysis Methods 0.000 title claims abstract description 139
- 238000001035 drying Methods 0.000 title claims abstract description 97
- 230000008878 coupling Effects 0.000 title claims abstract description 15
- 238000010168 coupling process Methods 0.000 title claims abstract description 15
- 238000005859 coupling reaction Methods 0.000 title claims abstract description 15
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 112
- 239000003546 flue gas Substances 0.000 claims abstract description 112
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 110
- 239000000779 smoke Substances 0.000 claims abstract description 37
- 239000002918 waste heat Substances 0.000 claims abstract description 23
- 238000000746 purification Methods 0.000 claims abstract description 20
- 239000000428 dust Substances 0.000 claims description 69
- 239000007789 gas Substances 0.000 claims description 56
- 239000008236 heating water Substances 0.000 claims description 18
- 238000006243 chemical reaction Methods 0.000 claims description 16
- 239000000567 combustion gas Substances 0.000 claims description 10
- 238000001816 cooling Methods 0.000 claims description 10
- 239000000498 cooling water Substances 0.000 claims description 10
- 230000003139 buffering effect Effects 0.000 claims description 9
- 238000010438 heat treatment Methods 0.000 claims description 9
- 239000002893 slag Substances 0.000 claims description 9
- 238000003860 storage Methods 0.000 claims description 7
- 238000007599 discharging Methods 0.000 claims description 3
- 238000000034 method Methods 0.000 description 32
- 230000008569 process Effects 0.000 description 27
- 230000001105 regulatory effect Effects 0.000 description 12
- 239000010865 sewage Substances 0.000 description 6
- 238000012546 transfer Methods 0.000 description 6
- 230000008901 benefit Effects 0.000 description 5
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 4
- 239000002956 ash Substances 0.000 description 4
- 229910052799 carbon Inorganic materials 0.000 description 4
- 238000005516 engineering process Methods 0.000 description 4
- 239000013049 sediment Substances 0.000 description 4
- 239000000126 substance Substances 0.000 description 4
- 239000000110 cooling liquid Substances 0.000 description 3
- 238000005265 energy consumption Methods 0.000 description 3
- 238000004064 recycling Methods 0.000 description 3
- 239000002028 Biomass Substances 0.000 description 2
- UIIMBOGNXHQVGW-UHFFFAOYSA-M Sodium bicarbonate Chemical compound [Na+].OC([O-])=O UIIMBOGNXHQVGW-UHFFFAOYSA-M 0.000 description 2
- 238000009825 accumulation Methods 0.000 description 2
- 239000000872 buffer Substances 0.000 description 2
- 239000003795 chemical substances by application Substances 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 230000007613 environmental effect Effects 0.000 description 2
- 239000003337 fertilizer Substances 0.000 description 2
- 239000010881 fly ash Substances 0.000 description 2
- 238000012423 maintenance Methods 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- 238000010926 purge Methods 0.000 description 2
- 238000011403 purification operation Methods 0.000 description 2
- 238000011084 recovery Methods 0.000 description 2
- 238000007789 sealing Methods 0.000 description 2
- 239000002910 solid waste Substances 0.000 description 2
- 238000005406 washing Methods 0.000 description 2
- 206010021143 Hypoxia Diseases 0.000 description 1
- 241000219061 Rheum Species 0.000 description 1
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 description 1
- 241001052560 Thallis Species 0.000 description 1
- XSQUKJJJFZCRTK-UHFFFAOYSA-N Urea Chemical compound NC(N)=O XSQUKJJJFZCRTK-UHFFFAOYSA-N 0.000 description 1
- 230000001133 acceleration Effects 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 230000001580 bacterial effect Effects 0.000 description 1
- 238000005452 bending Methods 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000004566 building material Substances 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 239000004202 carbamide Substances 0.000 description 1
- 230000003749 cleanliness Effects 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 239000000084 colloidal system Substances 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 238000004891 communication Methods 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000001599 direct drying Methods 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 239000004744 fabric Substances 0.000 description 1
- 239000004519 grease Substances 0.000 description 1
- 230000036541 health Effects 0.000 description 1
- 229910001385 heavy metal Inorganic materials 0.000 description 1
- 238000009413 insulation Methods 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 229920002521 macromolecule Polymers 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000000465 moulding Methods 0.000 description 1
- 239000010813 municipal solid waste Substances 0.000 description 1
- 239000003345 natural gas Substances 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 244000052769 pathogen Species 0.000 description 1
- 210000002706 plastid Anatomy 0.000 description 1
- 239000000843 powder Substances 0.000 description 1
- 229910000030 sodium bicarbonate Inorganic materials 0.000 description 1
- 235000017557 sodium bicarbonate Nutrition 0.000 description 1
- 239000007790 solid phase Substances 0.000 description 1
- 238000009834 vaporization Methods 0.000 description 1
- 230000008016 vaporization Effects 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F11/00—Treatment of sludge; Devices therefor
- C02F11/12—Treatment of sludge; Devices therefor by de-watering, drying or thickening
- C02F11/13—Treatment of sludge; Devices therefor by de-watering, drying or thickening by heating
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F11/00—Treatment of sludge; Devices therefor
- C02F11/10—Treatment of sludge; Devices therefor by pyrolysis
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B53/00—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2303/00—Specific treatment goals
- C02F2303/10—Energy recovery
-
- 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
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
- Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
-
- 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
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W10/00—Technologies for wastewater treatment
- Y02W10/40—Valorisation of by-products of wastewater, sewage or sludge processing
Landscapes
- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Life Sciences & Earth Sciences (AREA)
- Hydrology & Water Resources (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Mechanical Engineering (AREA)
- Materials Engineering (AREA)
- Treatment Of Sludge (AREA)
Abstract
The sludge low-temperature drying coupling pyrolysis system comprises a sludge feeding device, a sludge low-temperature drying device, a sludge pyrolysis device, a waste heat utilization device and a smoke purification device, wherein the output end of the sludge feeding device is connected with the sludge low-temperature drying device, the sludge outlet of the sludge low-temperature drying device is connected with the sludge pyrolysis device, the smoke outlet of the sludge pyrolysis device is connected with the waste heat utilization device, the waste heat utilization device is connected with the sludge low-temperature drying device and provides heat drying energy for the sludge low-temperature drying device, and the smoke outlet of the waste heat utilization device is connected with the smoke purification device; the waste heat utilization device is a flue gas-hot water heat exchanger, the flue gas-hot water heat exchanger comprises a flue gas inlet, a flue gas outlet, a water inlet and a water outlet, the flue gas inlet is connected with a flue gas outlet of the sludge pyrolysis device, the flue gas outlet is connected with a flue gas purification device, and the water inlet and the water outlet are both connected with a sludge low-temperature drying device.
Description
Technical Field
The invention belongs to the technical field of urban sludge incineration treatment, and relates to a sludge low-temperature drying coupling pyrolysis system.
Background
In recent years, along with the acceleration of the water yield and the treatment rate of urban sewage in China, the increase of the sludge quantity is caused, the sludge is a byproduct after sewage treatment, and the sludge is a non-uniform plastid composed of organic matters, bacterial thalli, pathogens, electrodeless particles, colloid, heavy metals and the like, if the treatment is improper, the health of surrounding people is endangered, secondary pollution is caused to the surrounding environment, the waste water is completely wasted before the sewage treatment is performed, and the environmental benefit and the social benefit of the sewage treatment are greatly reduced. Therefore, the comprehensive treatment of the sludge generated by the urban sewage treatment plant is very necessary to reduce the secondary pollution caused by the urban sludge to the maximum extent.
Sludge itself is a resource that can be utilized. The industrialization of the sludge is to utilize the sludge as a resource by means of advanced and feasible technical means, and can generate certain economic benefit on the basis of solving the problem of environmental impact. Most of sludge produced by urban sewage treatment plants has higher water content, which is basically more than 75%. The water content of the sludge is high, which is not only unfavorable for the transportation of the sludge, but also unfavorable for the subsequent treatment and the recycling. Therefore, the traditional method is that the sludge is dried, so that the volume and the weight are greatly reduced, and the sludge is sent to subsequent treatment; whether the sludge is subjected to low-temperature drying, medium-temperature drying and high-temperature drying, or is subjected to direct drying and indirect drying, a large amount of heat is required for evaporating water in the sludge, the vaporization latent heat of the water is more than 2000kJ/kg, and the method belongs to a high energy consumption process; the method comprises the steps of burning, pyrolysis, building material utilization, garbage synergy and the like, wherein the pyrolysis is used as a common process means of petrochemical industry and coal chemical industry, is transplanted into the sludge disposal process, utilizes the anoxic/anaerobic characteristics of pyrolysis, decomposes organic matters in the sludge into micromolecular substances at the high temperature of 600 ℃ and becomes a pyrolysis gas at the same time, and the pyrolysis gas becomes a relatively clean gas flow containing a certain heat value after being sprayed and dedusted, and can be used as a heat source in the pyrolysis process. However, in the traditional sludge drying pyrolysis treatment process, the pyrolyzed high-temperature flue gas is generally recycled by utilizing a mode of producing low-pressure steam by a waste heat boiler; in the low-temperature drying process, the previous mode cannot directly utilize low-pressure steam due to temperature difference, so that the combination degree of the drying process and the pyrolysis process is insufficient.
Disclosure of Invention
In order to overcome the defects in the prior art, the invention provides a sludge low-temperature drying coupling pyrolysis system which well combines a drying process and a pyrolysis process and well recovers heat of pyrolysis flue gas,
The technical scheme adopted by the invention is as follows:
The utility model provides a mud low temperature desiccation coupling pyrolysis system which characterized in that: the device comprises a sludge feeding device, a sludge low-temperature drying device, a sludge pyrolysis device, a waste heat utilization device and a smoke purification device, wherein the output end of the sludge feeding device is connected with the sludge low-temperature drying device, a sludge outlet of the sludge low-temperature drying device is connected with the sludge pyrolysis device, a smoke outlet of the sludge pyrolysis device is connected with the waste heat utilization device, the waste heat utilization device is connected with the sludge low-temperature drying device and provides heat drying energy for the sludge low-temperature drying device, and a smoke outlet of the waste heat utilization device is connected with the smoke purification device; the waste heat utilization device is a flue gas-hot water heat exchanger, the flue gas-hot water heat exchanger comprises a flue gas inlet, a flue gas outlet, a water inlet and a water outlet, the flue gas inlet is connected with a flue gas outlet of the sludge pyrolysis device, the flue gas outlet is connected with a flue gas purification device, and the water inlet and the water outlet are both connected with a sludge low-temperature drying device. The invention is used for recovering heat in pyrolysis flue gas of the sludge pyrolysis device, transferring the heat to intermediate medium hot water, directly using the heat in the sludge low-temperature drying device, well combining a drying process and a pyrolysis process, and well recovering heat of the pyrolysis flue gas.
Further, the flue gas-hot water heat exchanger further comprises a first heat exchange channel, a dust buffering channel, a second heat exchange channel and a third heat exchange channel which are sequentially communicated, wherein the first heat exchange channel is internally provided with the first heat exchanger, the second heat exchange channel is internally provided with the second heat exchanger, the third heat exchange channel is internally provided with the third heat exchanger, the bottom of the dust buffering channel is provided with a dust collector, the flue gas inlet is arranged at the inlet of the first heat exchange channel, and the flue gas outlet is arranged at the outlet of the third heat exchange channel; the cold water ports of the first heat exchanger, the second heat exchanger and the third heat exchanger are communicated with the water inlet, and the hot water ports of the first heat exchanger, the second heat exchanger and the third heat exchanger are communicated with the water outlet.
Further, the first heat exchange channel, the second heat exchange channel and the third heat exchange channel are all arranged side by side, the smoke inlet is formed in the top of the first heat exchange channel, the bottom of the second heat exchange channel of the first heat exchange channel is communicated through the dust buffering channel, the tops of the second heat exchange channel and the third heat exchange channel are communicated, and the smoke outlet is formed in the bottom of the third heat exchange channel.
Further, a bypass adjusting channel is arranged between the bottoms of the second heat exchanging channel and the third heat exchanging channel, a temperature adjusting valve is arranged on the bypass adjusting channel, and dustproof nets are arranged at two ports of the bypass adjusting channel. When the temperature in the dust-retarding channel is too low, the opening of the temperature regulating valve is controlled, so that part of flue gas does not pass through the second heat exchange channel, the third heat exchange channel and directly enter the flue outlet, and the temperature of the flue outlet is ensured. The dustproof net is used for protecting the temperature regulating valve, preventing the regulating valve from excessively accumulating ash and ensuring the regulating valve to be normally opened and closed; timely, the regulating valve needs to be opened and closed, dust accumulation in the bypass channel pair is removed, and when the channel is opened in an emergency, a great amount of smoke dust cannot be generated at the smoke outlet.
Further, the first heat exchanger and the second heat exchanger are vertically arranged in the corresponding heat exchange channels, and the third heat exchanger is horizontally arranged in the third heat exchange channel; the first heat exchanger, the second heat exchanger and the third heat exchanger are all fixed in the corresponding heat exchange channels through fixing ribs, wherein semicircular sheets and triangular sheets for dust collection in flue gas are arranged on the fixing ribs of the first heat exchanger and the second heat exchanger.
Further, the smoke inlet and the smoke outlet are both provided with temperature control nozzles for cooling.
Further, the sludge feeding device comprises a sludge storage bin and a sludge conveying device, and the sludge storage bin is communicated with the sludge low-temperature drying device through the sludge conveying device.
Further, the sludge low-temperature drying device comprises a sludge forming machine, a belt dryer, a gas-cold water heat exchanger and a gas-hot water heat exchanger, wherein a sludge inlet of the sludge forming machine is communicated with a sludge feeding device, a square bucket for caching sludge is arranged on the sludge forming machine, and a sludge outlet of the sludge forming machine is positioned above a top layer conveying belt of the belt dryer; the air-cooling water heat exchanger is internally provided with a circulating water cooling channel, the air inlet of the air-cooling water heat exchanger is communicated with the cold and wet air outlet of the belt drier, the air outlet of the air-cooling water heat exchanger is communicated with the air inlet of the air-heating water heat exchanger, the air outlet of the air-heating water heat exchanger is communicated with the hot dry air inlet of the belt drier, the hot water inlet of the air-heating water heat exchanger is communicated with the water outlet of the flue gas-heating water heat exchanger, and the cold water outlet of the air-heating water heat exchanger is communicated with the water inlet of the flue gas-heating water heat exchanger.
Further, mud pyrolysis device includes pyrolysis device, pyrolysis gas purifier, pyrolysis gas combustor, pyrolysis device is the pyrolysis oven of bilayer parcel structure, and its inlayer is the pyrolysis reaction chamber, and the skin is pyrolysis gas combustion gas heating chamber, the residue export and the cold sediment device intercommunication of pyrolysis reaction chamber, cold sediment device and slag charge storehouse intercommunication, the pyrolysis gas export and the pyrolysis gas purifier intercommunication of pyrolysis reaction chamber, the pyrolysis gas export and the pyrolysis gas combustor intercommunication of pyrolysis gas purifier, pyrolysis gas combustor and pyrolysis gas combustion gas heating chamber intercommunication, the pyrolysis gas export and the inlet intercommunication of pyrolysis gas combustion gas heating chamber.
Further, the flue gas purification device comprises a deacidification device and a dust removal device, the dust removal device comprises a primary dust remover and a secondary dust remover, a flue gas inlet of the primary dust remover is communicated with a flue gas outlet, a flue gas outlet of the primary dust remover is communicated with the deacidification device, a flue gas outlet of the deacidification device is communicated with a chimney for discharging flue gas through a secondary dust remover, and a dust outlet of the primary dust remover and a dust outlet of the secondary dust remover are communicated with a slag bin.
The invention has the beneficial effects that:
1. The sludge low-temperature drying technology and the sludge pyrolysis technology are coupled in terms of energy utilization, heat of flue gas generated by sludge pyrolysis in the cooling and purifying process is used in the sludge low-temperature drying process, the problem that a large amount of dust is generated by directly drying sludge by the flue gas is effectively avoided, the whole process of the sludge drying process is less than 70 ℃, almost no odor is generated in the sludge drying process, and the odor problem of sludge drying is avoided. The flue gas energy in the sludge pyrolysis process is recycled, so that the energy consumption of the sludge in the drying process can be greatly reduced, and the whole process is energy-saving compared with the traditional sludge drying process.
2. The device has simple structure and good energy heat exchange effect, can directly utilize the heat of the flue gas to generate hot water for a low-temperature drying process, such as a gas-gas heat exchange device, the heat exchange area required by the process flow is very large, the volume of equipment is very large, the manufacturing cost of corresponding equipment is increased, meanwhile, the temperature difference of a cold side is only about 30-40 ℃ during gas-gas heat exchange, the temperature fluctuation of the hot side is up to 400 ℃, and the temperature fluctuation of the cold side is relatively unstable during operation, so that the sludge low-temperature drying process is not facilitated. The gas-hot water heat exchange device uses hot water as a medium to transfer the heat of the flue gas into water, and then transfers the hot water into low-temperature drying hot air, so that the equipment investment is reduced and the operation is controllable although part of energy loss exists.
3. Compared with traditional medium-temperature drying and high-temperature drying, the low-temperature drying method for sludge is low in drying temperature, low in odor volatilization rate and small in odor volatilization amount, and can avoid odor problem which is difficult to treat by traditional drying by being assisted by a certain sealing and replacing means.
4. Compared with the traditional sludge incineration process, the sludge pyrolysis treatment process has the advantages that the generated flue gas is low in dust content and relatively pure, the purging and maintenance times of the flue gas waste heat recovery device are facilitated, the difficulty of the subsequent flue gas purification treatment process is reduced, and the flue gas purification operation cost is reduced. Meanwhile, organic matters in the sludge are effectively utilized, and after the organic matters are thermally cracked into combustible gas, the combustible gas is used for maintaining the pyrolysis reaction, so that energy utilization is reasonably carried out; when pyrolysis reaction occurs, fixed carbon in the sludge is locked in the residues, so that the sludge becomes a biomass fertilizer with high carbon content, and a good condition and foundation are laid for recycling the follow-up residues. Meanwhile, the embarrassing situation that ash and fly ash generated by the sludge drying and incinerating method can only be used as common solid waste for landfill is solved, and the pressure of a local landfill site and the urgent need for constructing a new landfill site are reduced.
Drawings
Fig. 1 is a schematic structural view of the present invention.
Fig. 2 is a schematic view of the structure of the flue gas-hot water heat exchanger of the present invention.
Fig. 3 is a schematic structural view of a first two-heat exchanger fixing rib of the present invention.
Fig. 4 is a schematic view of the bypass adjustment channel of the present invention.
Detailed Description
The invention will be further illustrated with reference to the following specific examples, without limiting the invention to these specific embodiments. It will be appreciated by those skilled in the art that the invention encompasses all alternatives, modifications and equivalents as may be included within the scope of the claims.
In the description of the present invention, it should be understood that the terms "center", "longitudinal", "lateral", "length", "width", "thickness", "upper", "lower", "front", "rear", "left", "right", "vertical", "horizontal", "top", "bottom", "inner", "clockwise", "counterclockwise", etc. indicate orientations or positional relationships based on the orientations or positional relationships shown in the drawings are merely for convenience in describing the present invention and simplifying the description, and do not indicate or imply that the device or element referred to must have a specific orientation, be configured and operated in a specific orientation, and thus should not be construed as limiting the present invention. Furthermore, the terms "first," "second," and the like, are used for descriptive purposes only and are not to be construed as indicating or implying a relative importance or implicitly indicating the number of technical features indicated. Thus, a feature defining "a first" or "a second" may explicitly or implicitly include one or more such feature. In the description of the present invention, unless otherwise specified, the meaning of "a plurality" is two or more, unless otherwise clearly defined.
In the present invention, unless explicitly specified and limited otherwise, the terms "mounted," "connected," "secured," and the like are to be construed broadly and may be, for example, fixedly connected, detachably connected, or integrally connected; can be mechanically or electrically connected; can be directly connected or indirectly connected through an intermediate medium, and can be communication between two elements. The specific meaning of the above terms in the present invention can be understood by those of ordinary skill in the art according to the specific circumstances.
In the present invention, unless expressly stated or limited otherwise, a first feature "above" or "below" a second feature may include both the first and second features being in direct contact, as well as the first and second features not being in direct contact but being in contact with each other through additional features therebetween. Moreover, a first feature being "above," "over" and "on" a second feature includes the first feature being directly above and obliquely above the second feature, or simply indicating that the first feature is higher in level than the second feature. The first feature being "under", "below" and "beneath" the second feature includes the first feature being directly under and obliquely below the second feature, or simply means that the first feature is less level than the second feature.
Referring to fig. 1, the embodiment provides a sludge low-temperature drying coupling pyrolysis system, which comprises a sludge feeding device, a sludge low-temperature drying device, a sludge pyrolysis device, a waste heat utilization device and a flue gas purification device, wherein the output end of the sludge feeding device is connected with the sludge low-temperature drying device, the sludge outlet of the sludge low-temperature drying device is connected with the sludge pyrolysis device, the flue gas outlet of the sludge pyrolysis device is connected with the waste heat utilization device, and the waste heat utilization device is connected with the sludge low-temperature drying device and provides heat drying energy for the sludge low-temperature drying device, and the flue gas outlet of the waste heat utilization device is connected with the flue gas purification device.
Referring to fig. 2, the waste heat utilization device is a flue gas-hot water heat exchanger, the flue gas-hot water heat exchanger comprises a flue gas inlet 1, a flue gas outlet 7, a water inlet and a water outlet, the flue gas inlet 1 is connected with a flue gas outlet of the sludge pyrolysis device, the flue gas outlet 7 is connected with a flue gas purification device, and the water inlet and the water outlet are both connected with a sludge low-temperature drying device. The invention is used for recovering heat in pyrolysis flue gas of the sludge pyrolysis device, transferring the heat to intermediate medium hot water, directly using the heat in the sludge low-temperature drying device, well combining a drying process and a pyrolysis process, and well recovering heat of the pyrolysis flue gas. The flue gas-hot water heat exchanger further comprises a first heat exchange channel 2, a dust buffering channel 3, a second heat exchange channel 5 and a third heat exchange channel 6 which are sequentially communicated, wherein a first heat exchanger 8 is arranged in the first heat exchange channel 2, a second heat exchanger 9 is arranged in the second heat exchange channel 5, a third heat exchanger 10 is arranged in the third heat exchange channel 6, a dust collector 4 is arranged at the bottom of the dust buffering channel 3, so that dust settled to the bottom in the flue gas heat exchange process enters the dust collector 4, is discharged out of the heat exchange device, and ensures the cleanliness in the channels; the smoke inlet 1 is arranged at the inlet of the first heat exchange channel 2, and the smoke outlet 7 is arranged at the outlet of the third heat exchange channel 6; the cold water ports of the first heat exchanger 8, the second heat exchanger 9 and the third heat exchanger 10 are communicated with the water inlet, and the hot water ports of the first heat exchanger 8, the second heat exchanger 9 and the third heat exchanger 10 are communicated with the water outlet. Specifically, the first heat exchange channel 2, the second heat exchange channel 5 and the third heat exchange channel 6 are all arranged side by side, the smoke inlet 1 is arranged at the top of the first heat exchange channel 2, the bottom of the second heat exchange channel 5 of the first heat exchange channel 2 is communicated through the dust buffering channel 3, the tops of the second heat exchange channel 5 and the third heat exchange channel 6 are communicated, and the smoke outlet 7 is arranged at the bottom of the third heat exchange channel 6.
In the embodiment, a flue gas inlet temperature control nozzle 13 (the included angle between the nozzle and the channel is generally 30-60 ℃) is arranged at the flue gas inlet 1, cooling liquid (generally deoxidized water, particularly urea solution can be used for denitration treatment) is sprayed, so that the temperature of inlet flue gas is prevented from being too high; a flue gas outlet temperature control nozzle 14 (generally horizontally arranged) is arranged at the flue gas outlet 7, and a human cooling liquid (generally deoxidized water, especially small soda water, is used for deacidifying treatment) is sprayed to prevent the temperature of the flue gas at the outlet from being high.
Referring to fig. 4, a bypass adjusting channel is disposed between the bottoms of the second heat exchanging channel 5 and the third heat exchanging channel 6 in this embodiment, a temperature adjusting valve 15 is installed on the bypass adjusting channel, the temperature adjusting valve 15 may be a pneumatic adjusting valve or an electromagnetic valve, and two ports of the bypass adjusting channel are provided with dust-proof nets 18. When the temperature in the dust-retarding channel 3 is too low, the opening of the temperature regulating valve 15 is controlled, so that part of flue gas does not pass through the second heat exchange channel and the third heat exchange channel and directly enters the flue outlet 7, and the temperature of the flue outlet 7 is ensured. The dustproof net 18 is used for protecting the temperature regulating valve 15, preventing the regulating valve from excessively accumulating ash and ensuring the normal opening and closing of the regulating valve; timely, the regulating valve needs to be opened and closed, dust accumulation in the bypass channel pair is removed, and when the channel is opened in an emergency, a great amount of smoke dust cannot be generated at the smoke outlet 7.
In this embodiment, the first heat exchanger 8 and the second heat exchanger 9 are vertically arranged in the corresponding heat exchange channels, and the third heat exchanger 6 is horizontally arranged in the third heat exchange channel 10; the first heat exchanger 8, the second heat exchanger 9 and the third heat exchanger 10 are all fixed in the corresponding heat exchange channels through fixing ribs, wherein the first heat exchanger 8 and the second heat exchanger 9 are fixedly connected with the channels through a first two-heat-exchanger fixing rib 11, a semi-circular sheet and a triangular sheet for dust collection in flue gas are arranged on the first two-heat-exchanger fixing rib 11, see fig. 3, and particularly, the arrangement of the semi-circular sheet 16 and the triangular sheet 17 can be freely combined according to practical conditions. The third heat exchanger 10 is fixedly connected with the channel in the channel by a third heat exchanger fixing rib 12. The first, second and third heat exchangers 8, 9 and 10 are bent-tube heat exchangers, and the bending times are determined according to actual working conditions.
The sludge feeding device 20 in this embodiment includes a sludge storage bin and a sludge conveying device, and the sludge storage bin is communicated with the sludge low-temperature drying device through the sludge conveying device.
The sludge low-temperature drying device 21 comprises a sludge forming machine, a belt dryer, a gas-cold water heat exchanger and a gas-hot water heat exchanger, wherein a sludge inlet of the sludge forming machine is communicated with a sludge feeding device, a square bucket for caching sludge is arranged on the sludge forming machine, and a sludge outlet of the sludge forming machine is positioned above a top layer conveying belt of the belt dryer; the air-cooling water heat exchanger is internally provided with a circulating water cooling channel, the air inlet of the air-cooling water heat exchanger is communicated with the cold and wet air outlet of the belt drier, the air outlet of the air-cooling water heat exchanger is communicated with the air inlet of the air-heating water heat exchanger, the air outlet of the air-heating water heat exchanger is communicated with the hot dry air inlet of the belt drier, the hot water inlet of the air-heating water heat exchanger is communicated with the water outlet of the flue gas-heating water heat exchanger, and the cold water outlet of the air-heating water heat exchanger is communicated with the water inlet of the flue gas-heating water heat exchanger.
The embodiment the mud pyrolysis device includes pyrolysis oven 22, pyrolysis gas purifier 24, pyrolysis gas combustor 23, pyrolysis oven 22 is bilayer parcel structure, and its inlayer is pyrolysis reaction chamber, and the skin is pyrolysis gas combustion gas heating chamber, the residue export and the cold sediment device 31 intercommunication of pyrolysis reaction chamber, cold sediment device 31 and slag charge storehouse 30 intercommunication, the pyrolysis gas export and the pyrolysis gas purifier 24 intercommunication of pyrolysis reaction chamber, the pyrolysis gas export and the pyrolysis gas combustor 23 intercommunication of pyrolysis gas purifier 24, pyrolysis gas combustor 23 and pyrolysis gas combustion gas heating chamber intercommunication, the pyrolysis gas export and the inlet 1 intercommunication of pyrolysis gas combustion gas heating chamber.
The flue gas purification device comprises a deacidification device and a dust removal device, wherein the dust removal device comprises a primary dust remover 26 and a secondary dust remover 28, a flue gas inlet of the primary dust remover 26 is communicated with a flue gas outlet 7, a flue gas outlet of the primary dust remover 26 is communicated with the deacidification device, a flue gas outlet of the deacidification device is communicated with a chimney 29 for discharging flue gas through a secondary dust remover 28, and a dust outlet of the primary dust remover 26 and a dust outlet of the secondary dust remover 28 are communicated with a slag bin 30. The deacidification device in this embodiment includes a deacidification tower 27, and the deacidification tower 27 is provided with a deacidification agent inlet.
When the invention is used, the sludge (the water content is 65-80%) stored in the sludge bin is sent to a sludge low-temperature drying device by a sludge conveying device (generally a screw pump or a plunger pump), a sludge forming machine is arranged at the inlet of the sludge low-temperature drying device, and a small bucket is arranged above the forming machine and used for caching the sludge; after being molded by a molding machine, the sludge falls onto a belt drier, is spread on a conveyor belt of the belt drier, and starts from the topmost layer of conveyor belt with multiple layers (generally 2-3 layers) of sludge, and falls into the next layer of conveyor belt in sequence while moving horizontally along with the conveyor belt until the sludge is sent out of the belt drier. On a conveyor belt, sludge and hot dry air (generally 65-80 ℃) fed into a belt dryer by a fan form cross flow, the sludge is directly contacted with the hot dry air, the sludge is heated, moisture contained in the sludge is continuously evaporated, the hot dry air and water vapor are mixed and then are changed into cold wet air (generally 45-60 ℃), the cold wet air and the water vapor leave the belt dryer, the cold wet air and the water vapor enter the belt dryer together, the cold wet air with a large amount of water vapor indirectly exchange heat with circulating cooling water in the belt dryer, the water vapor is condensed, the degree of rheum is reduced, then the cold wet air enters the belt dryer and exchanges heat with hot water (generally 85-90 ℃), and cold air is changed into the hot dry air after being heated to 65-80 ℃, and the cold air enters the belt dryer again by the fan.
The wet sludge is dried in the sludge low-temperature drying device, the water content is reduced to a certain degree (generally below 35%) to become dry sludge, and then the dry sludge is sent to the sludge pyrolysis device. The dry sludge firstly enters a pyrolysis device 22 (generally a pyrolysis furnace, the pyrolysis furnace is generally of a double-layer wrapping structure, the inner layer is filled with sludge and undergoes pyrolysis reaction, the outer layer is filled with pyrolysis gas combustion gas and undergoes heat transfer process), the sludge undergoes pyrolysis reaction under the conditions of oxygen deficiency/oxygen insulation and high temperature (generally 500-600 ℃) in the pyrolysis furnace, organic macromolecules in the sludge are cracked into various micromolecular substances to form pyrolysis gas, the pyrolysis gas is pumped out of the pyrolysis device and enters a pyrolysis gas purifier 24, washing liquid (generally water) is sprayed into the purifier to wash and intercept dust, grease and water-soluble organic micromolecular substances in the pyrolysis gas, the pyrolysis gas enters a pyrolysis gas burner 23 after washing and purification, and is mixed with supplementary gas (generally natural gas) and air to undergo combustion reaction, and the burnt flue gas (generally 850-1000 ℃) is introduced into an outer layer shell of the pyrolysis furnace and is subjected to heat transfer and supply heat required by the pyrolysis reaction; after the temperature of the flue gas is reduced (generally 550-650 ℃), the flue gas enters a flue gas-hot water heat exchanger 25 (generally of a single-stage or multi-stage shell-and-tube type), and in the heat exchanger, the flue gas and hot water exchange heat, the heat of the flue gas is transferred to the hot water, and the hot water is sent to the gas-hot water heat exchanger to provide energy for the low-temperature drying hot air.
Specifically, the high-temperature flue gas (550-600 ℃) from the pyrolysis device 22 sequentially passes through a flue gas inlet channel, a first heat exchange channel 2, a dust buffer channel 3, a second heat exchange channel 5, a third heat exchange channel 6 and a flue gas outlet channel, and then is discharged out of the heat exchange device to enter a subsequent flue gas purification device.
The flue gas in the first heat exchanger channel 2 indirectly exchanges heat with cold water in the pipe of the first heat exchanger 8, part of heat is transferred from the flue gas to the cold water, the flue gas is cooled to 450-500 ℃, the cold water is changed into hot water with the temperature not exceeding 90 ℃, and the hot water is discharged out of the first heat exchanger 8; then the flue gas enters a second heat exchange channel 5 through a dust buffer channel 3, and in the second heat exchange channel 5, indirect heat exchange is carried out on the flue gas and cold water in a pipe of a second heat exchanger 9, part of heat is transferred into the cold water, the flue gas is cooled to 300-350 ℃, the cold water is changed into hot water with the temperature not exceeding 90 ℃, and the hot water is discharged out of the second heat exchanger 9; then the flue gas enters the third heat exchange channel 6 and is subjected to indirect heat exchange with cold water in the pipe of the third heat exchanger 10, part of heat is transferred into the cold water, the temperature of the flue gas is reduced to 180-220 ℃, the cold water is changed into hot water with the temperature not exceeding 90 ℃, the hot water is discharged out of the third heat exchanger 10, and finally the flue gas exits from the flue gas outlet channel.
When the temperature of the smoke inlet 1 is too high or the heat exchange efficiency of the first, second and third heat exchangers is reduced, cooling liquid is sprayed through the temperature control nozzle 13 of the smoke inlet and the temperature control nozzle 14 of the smoke outlet, so that the temperature of the heat exchange device and the temperature of the smoke outlet 7 are kept within a certain range.
When the temperature of the smoke inlet 1 is too low or the heat exchange efficiency of the first heat exchanger, the second heat exchanger and the third heat exchanger is increased, the temperature regulating valve 15 can be opened through the bypass regulating channel, so that part of smoke directly enters the smoke outlet and is mixed with the other part of smoke passing through the second heat exchange channel and the third heat exchange channel and then is discharged out of the heat exchange device.
After the temperature of the flue gas is reduced again (generally 200-220 ℃), the flue gas enters a flue gas purification device, and the flue gas enters a primary dust remover 26 (generally an electrostatic dust remover) to complete primary dust removal; the flue gas enters a deacidification tower 27 after dust removal, deacidification agent (sodium bicarbonate powder is generally used) is sprayed into the deacidification tower 27 to remove acid gas, then the flue gas enters a secondary dust remover 28 (a cloth bag dust remover is generally used), the second-stage dust removal is completed, and the flue gas is sent to a chimney 29 for standard discharge through a fan after dust removal.
Pyrolysis residues are discharged from a solid phase outlet of the pyrolysis device and enter a slag cooling device 31 (generally a slag cooling machine), wherein the residues are cooled from 500-600 ℃ to below 50 ℃ and are sent to a slag bin 30 for storage through a discharge outlet of the slag cooling machine.
Compared with the traditional sludge incineration process, the sludge pyrolysis treatment process has the advantages that the generated flue gas is low in dust content and relatively pure, purging and maintenance times of a flue gas waste heat recovery device are facilitated, the difficulty of a subsequent flue gas purification treatment process is reduced, and the flue gas purification operation cost is reduced.
Meanwhile, organic matters in the sludge are effectively utilized, and after the organic matters are thermally cracked into combustible gas, the combustible gas is used for maintaining the pyrolysis reaction, so that energy utilization is reasonably carried out; when pyrolysis reaction occurs, fixed carbon in the sludge is locked in the residues, so that the sludge becomes a biomass fertilizer with high carbon content, and a good condition and foundation are laid for recycling the follow-up residues. Meanwhile, the embarrassing situation that ash and fly ash generated by the sludge drying and incinerating method can only be used as common solid waste for landfill is solved, and the pressure of a local landfill site and the urgent need for constructing a new landfill site are reduced.
Compared with traditional medium-temperature drying and high-temperature drying, the low-temperature drying method for sludge is low in drying temperature, low in odor volatilization rate and small in odor volatilization amount, and can avoid odor problem which is difficult to treat by traditional drying by being assisted by a certain sealing and replacing means.
The sludge low-temperature drying technology and the sludge pyrolysis technology are coupled in terms of energy utilization, heat of flue gas generated by sludge pyrolysis in the cooling and purifying process is used in the sludge low-temperature drying process, the problem that a large amount of dust is generated by directly drying sludge by the flue gas is effectively avoided, the whole process of the sludge drying process is less than 70 ℃, almost no odor is generated in the sludge drying process, and the odor problem of sludge drying is avoided. The flue gas energy in the sludge pyrolysis process is recycled, so that the energy consumption of the sludge in the drying process can be greatly reduced, and the whole process is energy-saving compared with the traditional sludge drying process.
The device has simple structure and good energy heat exchange effect, can directly utilize the heat of the flue gas to generate hot water for a low-temperature drying process, such as a gas-gas heat exchange device, the heat exchange area required by the process flow is very large, the volume of equipment is very large, the manufacturing cost of corresponding equipment is increased, meanwhile, the temperature difference of a cold side is only about 30-40 ℃ during gas-gas heat exchange, the temperature fluctuation of the hot side is up to 400 ℃, and the temperature fluctuation of the cold side is relatively unstable during operation, so that the sludge low-temperature drying process is not facilitated. The gas-hot water heat exchange device uses hot water as a medium to transfer the heat of the flue gas into water, and then transfers the hot water into low-temperature drying hot air, so that the equipment investment is reduced and the operation is controllable although part of energy loss exists.
The parts of the invention can be purchased, the specific model can be selected according to the sludge incineration amount, and the invention is not limited to a certain model.
Claims (8)
1. The utility model provides a mud low temperature desiccation coupling pyrolysis system which characterized in that: the device comprises a sludge feeding device, a sludge low-temperature drying device, a sludge pyrolysis device, a waste heat utilization device and a smoke purification device, wherein the output end of the sludge feeding device is connected with the sludge low-temperature drying device, a sludge outlet of the sludge low-temperature drying device is connected with the sludge pyrolysis device, a smoke outlet of the sludge pyrolysis device is connected with the waste heat utilization device, the waste heat utilization device is connected with the sludge low-temperature drying device and provides heat drying energy for the sludge low-temperature drying device, and a smoke outlet of the waste heat utilization device is connected with the smoke purification device; the waste heat utilization device is a flue gas-hot water heat exchanger, the flue gas-hot water heat exchanger comprises a flue gas inlet, a flue gas outlet, a water inlet and a water outlet, the flue gas inlet is connected with a flue gas outlet of the sludge pyrolysis device, the flue gas outlet is connected with a flue gas purification device, and the water inlet and the water outlet are both connected with a sludge low-temperature drying device;
The flue gas-hot water heat exchanger further comprises a first heat exchange channel, a dust buffering channel, a second heat exchange channel and a third heat exchange channel which are sequentially communicated, wherein the first heat exchange channel is internally provided with the first heat exchanger, the second heat exchange channel is internally provided with the second heat exchanger, the third heat exchange channel is internally provided with the third heat exchanger, the bottom of the dust buffering channel is provided with a dust collector, the flue gas inlet is arranged at the inlet of the first heat exchange channel, and the flue gas outlet is arranged at the outlet of the third heat exchange channel; the cold water ports of the first heat exchanger, the second heat exchanger and the third heat exchanger are communicated with the water inlet, and the hot water ports of the first heat exchanger, the second heat exchanger and the third heat exchanger are communicated with the water outlet;
the sludge feeding device comprises a sludge storage bin and a sludge conveying device, and the sludge storage bin is communicated with the sludge low-temperature drying device through the sludge conveying device.
2. The sludge low-temperature drying coupling pyrolysis system according to claim 1, wherein: the first heat exchange channel, the second heat exchange channel and the third heat exchange channel are all arranged side by side, the smoke inlet is formed in the top of the first heat exchange channel, the bottom of the second heat exchange channel of the first heat exchange channel is communicated through the dust buffering channel, the tops of the second heat exchange channel and the third heat exchange channel are communicated, and the smoke outlet is formed in the bottom of the third heat exchange channel.
3. The sludge low-temperature drying coupling pyrolysis system according to claim 2, wherein: a bypass adjusting channel is arranged between the bottoms of the second heat exchange channel and the third heat exchange channel, a temperature adjusting valve is arranged on the bypass adjusting channel, and dustproof nets are arranged at two ports of the bypass adjusting channel.
4. The sludge low-temperature drying coupling pyrolysis system according to claim 2, wherein: the first heat exchanger and the second heat exchanger are vertically arranged in the corresponding heat exchange channels, and the third heat exchanger is horizontally arranged in the third heat exchange channel; the first heat exchanger, the second heat exchanger and the third heat exchanger are all fixed in the corresponding heat exchange channels through fixing ribs, wherein semicircular sheets and triangular sheets for dust collection in flue gas are arranged on the fixing ribs of the first heat exchanger and the second heat exchanger.
5. The sludge low-temperature drying coupling pyrolysis system according to claim 1, wherein: the smoke inlet and the smoke outlet are both provided with temperature control nozzles for cooling.
6. The sludge low-temperature drying coupling pyrolysis system according to claim 1, wherein: the sludge low-temperature drying device comprises a sludge forming machine, a belt dryer, a gas-cold water heat exchanger and a gas-hot water heat exchanger, wherein a sludge inlet of the sludge forming machine is communicated with a sludge feeding device, a square bucket for caching sludge is arranged on the sludge forming machine, and a sludge outlet of the sludge forming machine is positioned above a top layer conveying belt of the belt dryer; the air-cooling water heat exchanger is internally provided with a circulating water cooling channel, the air inlet of the air-cooling water heat exchanger is communicated with the cold and wet air outlet of the belt drier, the air outlet of the air-cooling water heat exchanger is communicated with the air inlet of the air-heating water heat exchanger, the air outlet of the air-heating water heat exchanger is communicated with the hot dry air inlet of the belt drier, the hot water inlet of the air-heating water heat exchanger is communicated with the water outlet of the flue gas-heating water heat exchanger, and the cold water outlet of the air-heating water heat exchanger is communicated with the water inlet of the flue gas-heating water heat exchanger.
7. The sludge low-temperature drying coupling pyrolysis system according to claim 1, wherein: the sludge pyrolysis device comprises a pyrolysis device, a pyrolysis gas purifier and a pyrolysis gas burner, wherein the pyrolysis device is a pyrolysis furnace with a double-layer wrapping structure, the inner layer of the pyrolysis device is a pyrolysis reaction chamber, the outer layer of the pyrolysis device is a pyrolysis gas combustion gas heating chamber, a residue outlet of the pyrolysis reaction chamber is communicated with a cold residue device, the cold residue device is communicated with a residue bin, a pyrolysis gas outlet of the pyrolysis reaction chamber is communicated with the pyrolysis gas purifier, a pyrolysis gas outlet of the pyrolysis gas purifier is communicated with the pyrolysis gas burner, the pyrolysis gas burner is communicated with the pyrolysis gas combustion gas heating chamber, and a pyrolysis gas outlet of the pyrolysis gas combustion gas heating chamber is communicated with a smoke inlet.
8. The sludge low-temperature drying coupling pyrolysis system according to claim 1, wherein: the flue gas purification device comprises a deacidification device and a dust removal device, the dust removal device comprises a primary dust remover and a secondary dust remover, a flue gas inlet of the primary dust remover is communicated with a flue gas outlet, a flue gas outlet of the primary dust remover is communicated with the deacidification device, a flue gas outlet of the deacidification device is communicated with a chimney for discharging flue gas through a secondary dust remover, and a dust outlet of the primary dust remover and a dust outlet of the secondary dust remover are communicated with a slag bin.
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| CN111380353B (en) * | 2020-03-24 | 2021-06-25 | 杭州碳明科技有限公司 | Garbage disposal system and computer-readable storage medium |
| CN111561700A (en) * | 2020-04-01 | 2020-08-21 | 华北电力大学 | Rotary rake type organic solid waste pyrolysis device and pyrolysis method |
| CN113248108A (en) * | 2021-06-28 | 2021-08-13 | 仁天环保科技有限责任公司 | Integrated sludge treatment control system and method |
| CN114853309A (en) * | 2022-03-09 | 2022-08-05 | 广州晟启能源设备有限公司 | Sludge treatment system and sludge treatment method |
| CN114853310A (en) * | 2022-03-09 | 2022-08-05 | 广州晟启能源设备有限公司 | Sludge treatment system and sludge treatment method |
| CN114702226A (en) * | 2022-03-31 | 2022-07-05 | 安徽省通源环境节能股份有限公司 | Sludge classification drying carbonization system |
| CN114835370B (en) * | 2022-04-28 | 2023-03-28 | 杭州真一环保科技有限公司 | Sludge low-temperature drying coupling pyrolysis device |
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