CN110066083B - Sludge pyrolysis recycling system and pyrolysis method - Google Patents
Sludge pyrolysis recycling system and pyrolysis method Download PDFInfo
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- CN110066083B CN110066083B CN201910288836.9A CN201910288836A CN110066083B CN 110066083 B CN110066083 B CN 110066083B CN 201910288836 A CN201910288836 A CN 201910288836A CN 110066083 B CN110066083 B CN 110066083B
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- 238000000197 pyrolysis Methods 0.000 title claims abstract description 182
- 239000010802 sludge Substances 0.000 title claims abstract description 122
- 238000004064 recycling Methods 0.000 title claims abstract description 22
- 238000000034 method Methods 0.000 title claims abstract description 18
- 239000007787 solid Substances 0.000 claims abstract description 100
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 61
- 239000003546 flue gas Substances 0.000 claims abstract description 60
- 238000001035 drying Methods 0.000 claims abstract description 47
- 238000010438 heat treatment Methods 0.000 claims abstract description 47
- 238000006243 chemical reaction Methods 0.000 claims abstract description 19
- 238000003756 stirring Methods 0.000 claims abstract description 18
- 239000000463 material Substances 0.000 claims abstract description 14
- 239000007789 gas Substances 0.000 claims description 93
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 30
- 239000000779 smoke Substances 0.000 claims description 23
- 238000007599 discharging Methods 0.000 claims description 17
- 238000009826 distribution Methods 0.000 claims description 15
- 238000009833 condensation Methods 0.000 claims description 11
- 230000005494 condensation Effects 0.000 claims description 11
- 239000000428 dust Substances 0.000 claims description 11
- 239000007788 liquid Substances 0.000 claims description 11
- 239000002893 slag Substances 0.000 claims description 10
- 238000011282 treatment Methods 0.000 claims description 7
- 238000002485 combustion reaction Methods 0.000 claims description 6
- 239000011343 solid material Substances 0.000 claims description 6
- 239000000446 fuel Substances 0.000 claims description 5
- 239000002994 raw material Substances 0.000 claims description 5
- 239000000969 carrier Substances 0.000 claims description 3
- 238000004891 communication Methods 0.000 claims description 2
- 239000008247 solid mixture Substances 0.000 claims description 2
- 239000003517 fume Substances 0.000 claims 2
- 238000012546 transfer Methods 0.000 abstract description 9
- 238000012545 processing Methods 0.000 abstract description 4
- 238000002156 mixing Methods 0.000 abstract description 3
- 239000002918 waste heat Substances 0.000 abstract description 3
- 239000006004 Quartz sand Substances 0.000 abstract description 2
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 abstract description 2
- 238000004939 coking Methods 0.000 abstract description 2
- 238000005265 energy consumption Methods 0.000 abstract description 2
- 230000007774 longterm Effects 0.000 abstract description 2
- 229910052573 porcelain Inorganic materials 0.000 abstract description 2
- 238000005516 engineering process Methods 0.000 description 7
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 4
- 239000002028 Biomass Substances 0.000 description 4
- 238000010586 diagram Methods 0.000 description 3
- 239000000047 product Substances 0.000 description 3
- 239000006227 byproduct Substances 0.000 description 2
- 239000002737 fuel gas Substances 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 229910052757 nitrogen Inorganic materials 0.000 description 2
- 239000010865 sewage Substances 0.000 description 2
- XURIQWBLYMJSLS-UHFFFAOYSA-N 1,4,7,10-tetrazacyclododecan-2-one Chemical compound O=C1CNCCNCCNCCN1 XURIQWBLYMJSLS-UHFFFAOYSA-N 0.000 description 1
- 239000004215 Carbon black (E152) Substances 0.000 description 1
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 description 1
- 238000013019 agitation Methods 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 229910002091 carbon monoxide Inorganic materials 0.000 description 1
- 239000000567 combustion gas Substances 0.000 description 1
- 238000009264 composting Methods 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 229910001385 heavy metal Inorganic materials 0.000 description 1
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 125000004435 hydrogen atom Chemical class [H]* 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 238000011328 necessary treatment Methods 0.000 description 1
- 235000015097 nutrients Nutrition 0.000 description 1
- 239000012071 phase Substances 0.000 description 1
- 229910052698 phosphorus Inorganic materials 0.000 description 1
- 239000011574 phosphorus Substances 0.000 description 1
- 230000000750 progressive effect Effects 0.000 description 1
- 230000035484 reaction time Effects 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 239000007790 solid phase Substances 0.000 description 1
- 239000012265 solid product Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 238000005979 thermal decomposition reaction Methods 0.000 description 1
- 238000003466 welding Methods 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
- C02F11/10—Treatment of sludge; Devices therefor by pyrolysis
-
- 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
- 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
- C10B49/00—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated
- C10B49/16—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with moving solid heat-carriers in divided form
-
- 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
- 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
- C10B57/00—Other carbonising or coking processes; Features of destructive distillation processes in general
-
- 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
- C10B57/00—Other carbonising or coking processes; Features of destructive distillation processes in general
- C10B57/08—Non-mechanical pretreatment of the charge, e.g. desulfurization
- C10B57/10—Drying
-
- 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
Abstract
The embodiment of the invention provides a sludge pyrolysis recycling system, which adopts solid porcelain balls or quartz sand as a heat carrier to rapidly transfer heat to sludge according to the material and pyrolysis characteristics of the sludge, and comprises a spiral pyrolysis reactor which is specially designed and can realize forced mixing and rapid heat transfer of the sludge. The invention adopts the solid heat carrier and sludge to mix and heat directly, and has high heat efficiency and uniform heating compared with an indirect heating mode; the spiral blades and the stirring blades are reasonably arranged in the pyrolysis reactor, so that the full mixing and the rapid heat transfer of the sludge and the heat carrier can be realized, the pyrolysis reaction rate is high, the system processing capacity is high, the coking problem caused by uneven sludge stirring is effectively solved, and the long-term stable operation of the system is realized; the waste heat flue gas pre-drying sludge is recycled, so that the energy grading utilization is realized, the energy consumption can be effectively reduced, and the energy utilization efficiency of the system is improved. The embodiment of the invention also provides a method for pyrolyzing the sludge by adopting the sludge pyrolysis recycling system.
Description
Technical Field
The invention belongs to the technical field of harmless and recycling of sewage treatment byproduct sludge, and particularly relates to a sludge pyrolysis recycling system. The invention also provides a sludge pyrolysis method using the sludge pyrolysis recycling system.
Background
The sludge is a byproduct of sewage treatment production, has extremely complex composition components, contains a large amount of water, also contains nutrient elements such as nitrogen, phosphorus and the like, heavy metals, organic matters and the like, and can cause harm to the environment if the sludge is directly discharged into the environment, and the organic matters contained in the sludge are not utilized, so that the sludge is seriously wasted. The current sludge treatment technology mainly comprises landfill, composting, drying incineration, pyrolysis and the like. Wherein, the pyrolysis of the sludge is an important means for recycling the sludge. The sludge pyrolysis is to integrate the drying and thermal decomposition of the sludge under certain temperature and anoxic conditions, convert the sludge into gas and solid phases under heating conditions, convert the gas into gas and liquid phases through condensation, finally convert the sludge into three phase substances of gas, liquid and solid, wherein the gas obtained by converting the sludge is rich in combustible gases such as gaseous hydrocarbon, hydrogen, carbon monoxide and the like, and the liquid can obtain oil resources through oil-water separation. Therefore, the sludge pyrolysis technology can effectively realize sludge reduction, harmlessness and recycling, and is increasingly widely applied.
At present, the sludge pyrolysis technology is mainly divided into continuous type and intermittent type, wherein: the intermittent pyrolysis technology has small treatment scale, short running time and limited application range; the continuous pyrolysis process mainly adopts a rotary kiln type or spiral stirring type pyrolysis process with heated outer walls, has strong treatment capacity, is suitable for industrial application, but in the continuous pyrolysis process of sludge, sludge materials are easy to adhere to form blocks, so that the materials are difficult to scatter and transfer heat, uneven heating occurs, insufficient reaction or long reaction time occurs, and the like, and the system efficiency is reduced. In view of the above-mentioned drawbacks of the prior art, there is a need to develop a pyrolysis process that facilitates sludge agitation and heat transfer to achieve efficient and continuous pyrolysis of sludge, meeting the needs of industrial applications.
Disclosure of Invention
The invention aims to solve the problems of uneven heating, low heat efficiency, insufficient system processing capacity and the like in the existing sludge pyrolysis technology, provides a novel sludge pyrolysis reaction system and a pyrolysis method, adopts an internal heating technology, takes a solid heat carrier as a reaction heat transfer carrier, and has the characteristics of uniform heating, high efficiency, low price and easiness in industrialization based on the optimized pyrolysis reactor design.
In order to solve the technical problems, the embodiment of the invention provides a sludge pyrolysis recycling system, which comprises a pre-drying device, a feeding carrier bucket, a discharging carrier bucket, a pyrolysis reactor, a hot smoke furnace, a heating riser, a condenser, an oil-water separator, a cyclone separator and a slag extractor, wherein:
the pyrolysis reactor comprises a reactor cylinder body with a hollow round platform structure, the upper part of which is large and the lower part of which is small, and a rotating shaft is arranged at the center shaft position of the reactor cylinder body; a spiral blade is coiled and fixed on the rotating shaft and is stirred along with the rotation of the rotating shaft; the pre-drying device pre-dries the sludge raw material, and the pre-dried sludge is sent into the pyrolysis reactor; the feeding carrier hopper is positioned above the pyrolysis reactor, a solid outlet in the feeding carrier hopper is connected with the pyrolysis reactor, and a solid heat carrier is fed into the pyrolysis reactor; the sludge and the solid heat carrier are mixed in the pyrolysis reactor to carry out pyrolysis reaction; the pyrolysis gas in the pyrolysis reactor is sent into the condenser, liquid generated by condensation in the condenser is sent into the oil-water separator, and water and oil are separated in the oil-water separator; the discharging carrier hopper is positioned below the pyrolysis reactor, and solid matters in the pyrolysis reactor are sent into the heating riser through the discharging carrier hopper; the lower part of the heating lifting pipe is connected with the hot smoke furnace, and flue gas generated by combustion of fuel gas in the hot smoke furnace is sent into the heating lifting pipe for heating and lifting solid matters; an outlet at the upper part of the heating lifting pipe is connected with an inlet of the feeding carrier bucket, and solid matters and smoke are fed into the feeding carrier bucket; the gas outlet of the feeding carrier hopper is connected with the cyclone separator, and dust-containing flue gas is sent into the cyclone separator; the solid matters separated in the cyclone separator are sent to the slag extractor, and the slag extractor discharges residues.
As the preference of pyrolysis reactor, be fixed with a plurality of stirring leaves on the spiral leaf along blade extending direction in proper order, stirring leaf is square or circular bellied rib.
As the preference of the pyrolysis reactor, one side of the upper end of the reactor cylinder is provided with the heat carrier inlet and the sludge inlet, the opposite side is provided with the pyrolysis gas outlet, the position of the heat carrier inlet is higher than that of the sludge inlet, and the side part of the lower end of the reactor cylinder is also provided with a solid outlet; the sludge outlet of the pre-drying device is connected with the sludge inlet, and sludge is fed into the pyrolysis reactor; the solid outlet of the feeding carrier hopper is connected with the heat carrier inlet, and solid heat carriers are fed into the pyrolysis reactor; the pyrolysis gas outlet is connected with the inlet of the condenser, and pyrolysis gas after pyrolysis reaction is sent into the condenser; the solid outlet is connected with the discharge carrier bucket, and the solid mixture after the pyrolysis reaction is discharged into the discharge carrier bucket. Further preferably, the pyrolysis gas outlet of the pyrolysis reactor is communicated with a plurality of side exhaust ports, and the side exhaust ports extend into the reactor cylinder body and are used for collecting pyrolysis gas inside and guiding the collected pyrolysis gas to the pyrolysis gas outlet for discharging.
As the preference of heating riser, the heating riser is from bottom to top in proper order feed section, expansion section and hoisting section, the feed section includes solid feed inlet, hot flue gas pipeline, outer tube, interior sleeve pipe, swift current material mouth and solid distributor, wherein:
the solid feed inlet is arranged on the upper side part of the outer sleeve; the inner sleeve is sleeved in the outer sleeve, the material sliding opening is arranged between the lower end of the inner sleeve and the lower bottom of the outer sleeve, and solid materials in the outer sleeve can enter the inner sleeve through the material sliding opening; the hot flue gas pipeline is inserted from the bottom of the outer sleeve and extends into the inner sleeve from the lower part, and a gap is reserved between the hot flue gas pipeline and the inner sleeve; the solid distributor is positioned at the position of the feed chute and surrounds the outer wall of the hot flue gas pipeline, a high-pressure gas inlet and a plurality of distribution gas nozzles uniformly distributed along the circumferential direction are arranged on the solid distributor, and the distribution gas is introduced into the solid distributor from the high-pressure gas inlet and is sprayed upwards through the distribution gas nozzles.
Preferably, a gas outlet of the cyclone separator is connected with a gas inlet of the pre-drying device, and the flue gas in the cyclone separator is sent into the pre-drying device to be used as a heat source for drying sludge; and the flue gas subjected to heat exchange in the pre-drying device is sent into a tail gas induced draft fan through a flue gas outlet and is discharged from the tail gas induced draft fan.
Preferably, a gas outlet of the condenser is connected with the hot smoke furnace, and non-condensable gas in the condenser is fed into the hot smoke furnace as fuel.
The embodiment of the invention also provides a sludge pyrolysis method, which uses the sludge pyrolysis recycling system provided by the technical scheme to carry out pyrolysis treatment on sludge, and comprises the following steps:
1. the sludge containing water is sent into a pre-drying device for pre-drying;
2. the sludge after pre-drying is sent into a pyrolysis reactor to be mixed with a solid heat carrier, and pyrolysis reaction is carried out to obtain pyrolysis gas and solid matters containing the solid heat carrier;
3. sending the high-temperature pyrolysis gas in the pyrolysis reactor into a condenser, and condensing to obtain liquid and non-condensable gas;
4. separating water and oil from the liquid obtained by condensation in the condenser in an oil-water separator;
5. feeding the solids in the pyrolysis reactor into a heating riser where the solids are heated by flue gas from a hot flue gas furnace and lifted into a feed carrier hopper;
6. feeding the solid heat carrier in the feeding carrier hopper into a pyrolysis reactor to be mixed with the pre-dried sludge;
7. and sending the dust-containing flue gas in the feeding carrier hopper into a cyclone separator to separate solids and flue gas, and discharging the solids as residues.
Preferably, the non-condensable gas obtained after condensation in the condenser in the step 3 is sent into the hot smoke furnace to be used as fuel.
Preferably, the flue gas separated from the dust-containing flue gas in the step 7 is sent into the pre-drying device to be used as a heat source for drying the sludge.
The technical scheme of the embodiment of the invention has the beneficial effects that:
1. according to the material and pyrolysis characteristics of the sludge, a solid heat carrier is adopted to transfer heat to the sludge, so that the method has the advantages of high heat efficiency, uniform heating and the like compared with an indirect heating mode in the prior art;
2. the spiral blades and the stirring blades are reasonably arranged in the pyrolysis reactor, so that the full mixing and rapid heat transfer of the sludge and the heat carrier can be realized, the pyrolysis reaction rate is high, the system processing capacity is high, the coking problem caused by uneven sludge stirring is effectively solved, and the long-term stable operation of the system is realized;
3. the secondary pyrolysis of pyrolysis products is reduced through the rapid heating of the sludge and the rapid export of oil gas, so that the high yield of pyrolysis oil yield is realized, and the sludge recycling is realized to the maximum extent;
4. the sludge pre-drying device is adopted, the water in the sludge is primarily removed by utilizing the waste heat flue gas, the energy consumption of the pyrolysis device is reduced, the energy grading utilization is realized, and the energy utilization efficiency of the system is improved.
Drawings
FIG. 1 is a system diagram of a sludge pyrolysis recycling system provided by an embodiment of the invention;
FIG. 2 is a schematic diagram of a pyrolysis reactor in a sludge pyrolysis recycling system according to an embodiment of the present invention;
FIG. 3 is a schematic diagram of a heating riser in a sludge pyrolysis recycling system according to an embodiment of the present invention;
fig. 4 is a schematic flow chart of steps of a sludge pyrolysis method according to an embodiment of the present invention.
[ description of the Main element symbols ]
1-a pre-drying device; 11-a tail gas induced draft fan; 12-a dust remover;
a 2-pyrolysis reactor; 21-a reactor cylinder; 22-a rotation axis; 23-helix leaf; 231-stirring blade; 24-heat carrier inlet; 25-sludge inlet; 26-solids outlet; 27-pyrolysis gas outlet; 271-side exhaust ports;
31-a feed carrier hopper; 32-a discharge carrier bucket;
41-carrier-out spiral; 42-feeding a carrier screw;
5-a hot smoke furnace; 51-air distribution fan;
6-heating the riser; 61-a feed section; 611-a solid feed port; 612-hot flue gas duct; 613-outer sleeve; 614-inner sleeve; 615-a chute; 616—a solids distributor; 616 a-a high pressure gas inlet; 616 b-distribution gas nozzles; a 6L-solid material line; 62-expanding section; 63-a lifting section;
71-a condenser; 72-an oil-water separator;
8-cyclone separator;
9-slag extractor.
Detailed Description
In order to make the technical problems, technical solutions and advantages to be solved more apparent, the following detailed description will be given with reference to the accompanying drawings and specific embodiments.
Aiming at the problems of uneven heating, low heat efficiency, insufficient system processing capacity and the like in the existing sludge pyrolysis technology, the invention provides a novel sludge pyrolysis reaction system and a pyrolysis method, which have the characteristics of uniform heating, high efficiency, low price, easy industrialization and the like.
In order to achieve the above technical solution, an embodiment of the present invention provides a sludge pyrolysis recycling system, as shown in fig. 1, which is a basic structure thereof, and includes a pre-drying device 1, a feed carrier bucket 31, a discharge carrier bucket 32, a pyrolysis reactor 2, a hot smoke furnace 5, a heating riser 6, a condenser 71, an oil-water separator 72, a cyclone separator 8, and a slag extractor 9, wherein:
the sludge raw material to be treated is sent into the system from the pre-drying device 1, the sludge raw material is pre-dried in the pre-drying device 1, and the pre-dried sludge is sent into the pyrolysis reactor 2.
The feeding carrier hopper 31 is positioned above the pyrolysis reactor 2, a solid outlet in the feeding carrier hopper 31 is connected with the pyrolysis reactor 2, and a high-temperature solid heat carrier is fed into the pyrolysis reactor 2, so that the feeding carrier hopper 31 can be used for conveying the solid heat carrier into the pyrolysis reactor 2 through the feeding carrier screw 42, wherein the solid heat carrier can be porcelain balls or quartz sand, and other materials can be selected according to requirements; after the sludge and the solid heat carrier are mixed in the pyrolysis reactor 2, the solid heat carrier transfers heat to the sludge to carry out pyrolysis reaction; the discharging carrier hopper 32 is positioned below the pyrolysis reactor 2, and the solid matters in the pyrolysis reactor 2 are sent into the heating riser 6 through the discharging carrier hopper 32, and as a better embodiment, a discharging carrier screw 41 is connected between the discharging carrier hopper 32 and the heating riser 6, and the solid matters containing solid heat carriers are conveyed into the heating riser 6 through the discharging carrier screw 41; the lower part of the heating lifting pipe 6 is connected with a hot smoke furnace 5, the hot smoke furnace 5 can be connected with an air distribution fan 51 to inject air for supporting combustion, and flue gas generated by gas combustion in the hot smoke furnace 5 is sent into the heating lifting pipe 6 for heating and lifting solid matters; an outlet at the upper part of the heating lifting pipe 6 is connected with an inlet of a feeding carrier bucket 31, and solid matters and flue gas are fed into the feeding carrier bucket 31 together; the solid heat carrier circulates in the feed carrier hopper 31, pyrolysis reactor 2, discharge carrier hopper 32 and heated riser 6.
The pyrolysis gas generated in the pyrolysis reactor 2 is sent to a condenser 71, the liquid generated by condensation in the condenser 71 is sent to an oil-water separator 72, and water and oil are separated in the oil-water separator 72 and can be sent out; the non-condensable gas remained after the pyrolysis gas is condensed in the condenser 71 can be sent out as fuel, and as a more preferable embodiment, the gas outlet of the condenser 71 can be connected with the hot smoke furnace 5, and the discharged non-condensable gas can be sent into the hot smoke furnace 5 to be used as fuel gas.
The gas outlet of the feeding carrier bucket 31 is connected with the cyclone separator 8, and the dust-containing flue gas is sent into the cyclone separator 8; the solid matters separated in the cyclone separator 8 are sent to a slag extractor 9, and then are discharged by the slag extractor 9 as system residues; the flue gas separated in the cyclone separator 8 can be directly discharged after necessary treatment, as a better embodiment, as shown in fig. 1, a gas outlet of the cyclone separator 8 can also be connected with the pre-drying device 1, the flue gas is led into the pre-drying device 1 to be used as a heat source for drying sludge, a tail gas induced draft fan 11 is connected with a flue gas outlet of the pre-drying device 1, and the flue gas after heat exchange with the water-containing sludge is sent into a dust remover 12 to be treated and then discharged.
As shown in fig. 2, the pyrolysis reactor 2 includes a reactor cylinder 21, a heat carrier inlet 24, a sludge inlet 25 and a pyrolysis gas outlet 27 which are arranged on the reactor cylinder 21, wherein the reactor cylinder 21 has a hollow round platform structure with a large top and a small bottom, and a rotation shaft 22 is arranged at the center axis position of the reactor cylinder 21; a spiral blade 23 is coiled and fixed on the rotating shaft 22, and the spiral blade 23 rotates along with the rotating shaft 22 to stir; a heat carrier inlet 24 and a sludge inlet 25 are arranged on one side of the upper end of the reactor cylinder 21, a pyrolysis gas outlet 27 is arranged on the opposite side, and the position of the heat carrier inlet 24 is higher than that of the sludge inlet 25; the side of the lower end of the reactor vessel 21 is also provided with a solids outlet 26 for discharging solid heat carrier and pyrolysis solid products.
The pyrolysis reactor 2 may take the following arrangement as a more preferred embodiment:
the included angle alpha between the side elevation and the lower bottom surface of the reactor cylinder 21 is more than 90 degrees, preferably not more than 135 degrees; the side part of the reactor cylinder 21 can be provided with a plurality of side exhaust ports 271 communicated with the pyrolysis gas outlet 27, preferably three to five side exhaust ports 271, and the side exhaust ports 271 extend into the reactor cylinder 21 and are used for collecting the pyrolysis gas in the reactor cylinder 21 and collecting and guiding the pyrolysis gas to the pyrolysis gas outlet 27 for discharge; the side exhaust port 271 can be circular or square, and horizontally extends out of the inner wall of the reactor cylinder 21 by 4-95 mm;
the rotating shaft 22 is arranged at the center axis position of the reactor cylinder 21 and vertically penetrates through the reactor cylinder 21 from top to bottom; the spiral blades 23 are coiled and fixed on the rotating shaft 22, the spiral blades 23 can be fixed with the rotating shaft 22 in a welding mode, and when the rotating shaft 22 rotates, the spiral blades 23 stir by taking the rotating shaft 22 as an axis to stir and push biomass in the reactor cylinder 21; the distance between adjacent blades of the spiral blade 23 is 300-500 mm, and the distance between the edge of the spiral blade 23 and the inner side wall of the reactor cylinder 21 is 5-100 mm; for further improving stirring effect, a plurality of ribs can be welded and fixed in proper order along the extending direction of the blades on the spiral blade 23 to serve as stirring blades 231, the ribs are square or round protrusions, the height of the protrusions can be set to be 50-100 mm, and the distance between every two adjacent ribs can be set to be 200-300 mm.
In the sludge pyrolysis recycling system, aiming at the heating and lifting requirement of a solid heat carrier, a heating lifting pipe adopts an example shown in fig. 3, and the specific structure and arrangement are as follows:
the heating riser 6 comprises a feeding section 61, an expanding section 62 and a lifting section 63 from bottom to top, wherein the feeding section 61 comprises a solid feeding hole 611, a hot flue gas pipeline 612, an outer sleeve 613, an inner sleeve 614, a chute 615 and a solid distributor 616. The solid feed port 611 is provided at the upper side of the outer sleeve 613; the inner sleeve 614 is sleeved in the outer sleeve 613, a chute 615 is arranged between the lower end of the inner sleeve 614 and the lower bottom of the outer sleeve 613, and solid materials in the outer sleeve 613 can enter the inner sleeve 614 through the chute 615; the hot flue gas pipeline 612 is inserted from the bottom of the outer sleeve 613 and extends into the inner sleeve 614 from below, and a gap is formed between the hot flue gas pipeline 612 and the inner sleeve 614; the solid distributor 616 is located at the position of the chute 615 and surrounds the outer wall of the hot flue gas pipeline 612, the solid distributor 616 is provided with a high-pressure gas inlet 616a and a plurality of distribution gas nozzles 616b uniformly distributed along the circumferential direction, and the distribution gas is introduced into the solid distributor 616 from the high-pressure gas inlet 616a and is sprayed upwards through the distribution gas nozzles 616 b.
As a more preferable embodiment, the distance between the position of the solid feed port 611 and the bottom of the outer sleeve 613 is preferably 500-1000 mm, and the fed solid materials are stacked to form an inclined solid material line 6L; the diameter of the inner sleeve 614 is 200-800 mm, the inner sleeve 614 supplies heat to circulate smoke, and the flowing speed of the hot smoke in the inner sleeve 614 is limited to 30-75 m/s; the diameter of the hot flue gas pipeline 612 is 20-50 mm smaller than that of the inner sleeve 614, a gap between the hot flue gas pipeline 612 and the inner sleeve 614 is formed, and the length H of the pipe orifice of the hot flue gas pipeline 612 extending into the inner sleeve 614 is 10-50 mm; the height of the material sliding opening 615 is set to be 50-150 mm, and the material sliding speed is adjusted through the gas distribution speed of the solid distributor 616; the gas distribution of the solid distributor adopts compressed air or nitrogen, the gas pressure range at the high-pressure gas inlet 616a is 0.1-0.6 mpa, the number of the gas distribution nozzles 616b is eight-sixteen, the nozzles can adopt dome blast caps, and the gas outlet speed is controlled to be 30-50 m/s.
The embodiment of the invention also provides a biomass pyrolysis reaction method, which uses the biomass vertical pyrolysis reaction system to treat biomass raw materials, and comprises the following steps:
s1, sending the water-containing sludge into a pre-drying device for pre-drying;
s2, sending the pre-dried sludge into a pyrolysis reactor to be mixed with a solid heat carrier, and obtaining pyrolysis gas and solid matters containing the solid heat carrier through pyrolysis reaction;
s3, sending the high-temperature pyrolysis gas in the pyrolysis reactor into a condenser, and condensing to obtain liquid and non-condensable gas;
s4, separating water and oil from the liquid obtained by condensation in the condenser in an oil-water separator;
s5, conveying the solid matters in the pyrolysis reactor into a heating riser, and heating the solid matters in the heating riser by flue gas from a hot flue gas furnace and lifting the solid matters into a feeding carrier bucket;
s6, conveying the solid heat carrier in the feeding carrier hopper into a pyrolysis reactor to be mixed with the pre-dried sludge;
s7, sending the dust-containing flue gas in the feeding carrier hopper into a cyclone separator to separate out solids and flue gas, and discharging the solids as residues.
A preferred embodiment of the above steps is as follows:
in the step S1, the drying temperature is set to be 100-200 ℃ when the high-moisture sludge is sent into a pre-drying device for pre-drying; in order to improve the energy utilization rate, the waste heat of the high-temperature flue gas is fully utilized, and the flue gas separated from the dust-containing flue gas by the cyclone separator in the step 7 is sent into a pre-drying device to be used as a heat source for drying the sludge, wherein the temperature of the flue gas is controlled at 200-400 ℃.
In the step S2, the pre-dried sludge is sent into a pyrolysis reactor to be mixed with a solid heat carrier, the temperature of the solid heat carrier is controlled to be 600-800 ℃, and according to the properties of different types of sludge, the residence time of the sludge in the pyrolysis reactor can be controlled to be 1-10 min by adjusting the rotating speed of spiral blades in the pyrolysis reactor, so that pyrolysis gas is generated by pyrolysis of the sludge.
In the step S3, when the pyrolysis gas is sent to a condensing device for oil-water condensation, the condensing temperature is 20-50 ℃, and the non-condensable gas obtained after condensation can be sent out as a product or directly sent to a hot smoke furnace to be used as gas, and the non-condensable gas is burnt in the hot smoke furnace to generate high-temperature smoke.
In the step S5, the temperature of the solid matters which are discharged from the pyrolysis reactor and contain the solid heat carrier is 400-500 ℃, and the solid matters are heated by the combustion flue gas at 800-1200 ℃ in the heating lifting pipe and lifted into the feeding carrier hopper.
The following is a specific example of pyrolysis of sludge using the pyrolysis reaction system and pyrolysis method described above:
taking a certain sludge as an example, the main properties of the sludge are as follows:
| project | Unit (B) | Numerical value | Remarks |
| Water content | % | 79.30 | Received base |
| Mud content | % | 20.70 | Received base |
The high-moisture sludge is sent into a pre-drying device for pre-drying, the drying temperature is 180 ℃, the temperature of high-temperature flue gas entering the pre-drying device is 350 ℃, and the moisture content of the sludge is reduced to 21% when the sludge exits the pre-drying device. The pre-dried sludge is sent to a pyrolysis reactor to be mixed with a solid heat carrier, wherein the temperature of the heat carrier is 700 ℃. The included angle alpha of the pyrolysis reactor is 125 degrees, the spiral She Jianju is 250mm, square stirring blades with the height of 50mm are welded on the spiral blades, the distance between the stirring blades is 150mm, three side exhaust ports communicated with the pyrolysis gas outlet are arranged on the side part of the pyrolysis reactor, the distance between the spiral blades and the inner wall of the reactor cylinder is 30mm, and the side exhaust ports horizontally extend into the reactor cylinder for 20mm. The residence time of the sludge is 6min by adjusting the spiral rotating speed of the pyrolysis reactor, and pyrolysis gas generated by pyrolysis is sent into a condensing device for oil-water condensation, wherein the condensing temperature is 40 ℃. The temperature of the solids discharged from the pyrolysis reactor was 500 ℃. The solid heat carrier fed into the heating riser is heated by combustion flue gas with the temperature of 1000 ℃ and lifted to a feeding carrier bucket, and is mixed with sludge after being input into the pyrolysis reactor.
Based on the products of the pyrolysis system, wherein: the yield of pyrolysis oil is 25.3%, the yield of pyrolysis gas is 40.2%, the yield of slag is 11.2%, the yield of pyrolysis water is 23.3%, and the gas component is CH 4 、H 2 CO is mainly, and the calorific value is up to 3750kcal/Nm 3 。
Common sense of the above embodiments of the present invention, such as specific structures and features that are well known in the art, are not described in detail; the embodiments are described in a progressive manner, technical features related to the embodiments can be combined on the premise that the technical features do not form conflict with each other, and the same similar parts of the embodiments are mutually seen.
In the description of the present invention, the terms "upper," "lower," "horizontal," "inner," "outer," and the like indicate an orientation or positional relationship based on that shown in the drawings, merely for convenience of description and to simplify the description, and do not indicate or imply that the apparatus or elements in question must have a specific orientation, be constructed and operate in a specific orientation, and should not be construed as limiting the invention. Unless specifically stated and limited otherwise, the terms "connected," "coupled" and "connected" are to be construed broadly, and may be, for example, fixedly connected, detachably connected, or integrally connected; can be directly connected or indirectly connected through an intermediate medium, and can be communication between two elements.
The above embodiments are only for illustrating the technical solution of the present invention and not for limiting the same, and although the present invention has been described in detail with reference to the above embodiments, one skilled in the art may make modifications and equivalents to the specific embodiments of the present invention, and any modifications and equivalents not departing from the spirit and scope of the present invention are within the scope of the claims of the present invention.
Claims (9)
1. The utility model provides a mud pyrolysis resourceful system, includes predrying unit (1), feed carrier fill (31), ejection of compact carrier fill (32), pyrolysis reactor (2), hot smoke stove (5), heating riser (6), condenser (71), oil-water separator (72), cyclone (8) and scum ware (9), its characterized in that:
the pyrolysis reactor (2) comprises a reactor cylinder body (21) with a hollow round platform structure, the upper part of which is large and the lower part of which is small, and a rotary shaft (22) is arranged at the center axis position of the reactor cylinder body (21); a spiral blade (23) is coiled and fixed on the rotating shaft (22), and the spiral blade (23) rotates along with the rotating shaft (22) to stir;
the pre-drying device (1) pre-dries the sludge raw material, and the pre-dried sludge is sent into the pyrolysis reactor (2); the feeding carrier hopper (31) is positioned above the pyrolysis reactor (2), a solid outlet in the feeding carrier hopper (31) is connected with the pyrolysis reactor (2), and a solid heat carrier is fed into the pyrolysis reactor (2); the sludge and the solid heat carrier are mixed in the pyrolysis reactor (2) to carry out pyrolysis reaction;
the pyrolysis gas in the pyrolysis reactor (2) is sent into the condenser (71), liquid generated by condensation in the condenser (71) is sent into the oil-water separator (72), and water and oil are separated in the oil-water separator (72); the discharging carrier hopper (32) is positioned below the pyrolysis reactor (2), and solid matters in the pyrolysis reactor (2) are sent into the heating riser (6) through the discharging carrier hopper (32); the lower part of the heating riser tube (6) is connected with the hot smoke furnace (5), and flue gas generated by gas combustion in the hot smoke furnace (5) is sent into the heating riser tube (6) for heating and lifting solid matters; an outlet at the upper part of the heating riser (6) is connected with an inlet of the feeding carrier bucket (31) to send solid matters and flue gas into the feeding carrier bucket (31); the gas outlet of the feeding carrier hopper (31) is connected with the cyclone separator (8) and sends dust-containing flue gas into the cyclone separator (8); the solid matters separated in the cyclone separator (8) are sent to the slag extractor (9), and residues are discharged by the slag extractor (9);
the heating riser (6) is from bottom to top in proper order feed section (61), expansion section (62) and hoisting section (63), feed section (61) are including solid feed inlet (611), hot flue gas pipeline (612), outer tube (613), interior sleeve pipe (614), swift current material mouth (615) and solid distributor (616), wherein:
the solid feed inlet (611) is arranged at the upper side part of the outer sleeve (613); the inner sleeve (614) is arranged in the outer sleeve (613), the material sliding opening (615) is arranged between the lower end of the inner sleeve (614) and the lower bottom of the outer sleeve (613), and solid materials in the outer sleeve (613) can enter the inner sleeve (614) through the material sliding opening (615); the hot flue gas pipeline (612) is inserted from the bottom of the outer sleeve (613) and extends into the inner sleeve (614) from below, a gap is reserved between the hot flue gas pipeline (612) and the inner sleeve (614), and the inner sleeve (614) supplies heat and circulates flue gas; the solid distributor (616) is positioned at the position of the material sliding opening (615) and surrounds the outer wall of the hot flue gas pipeline (612), the solid distributor (616) is provided with a high-pressure air inlet (616 a) and a plurality of distribution air nozzles (616 b) which are uniformly distributed along the circumferential direction, and the distribution air is introduced into the solid distributor (616) from the high-pressure air inlet (616 a) and is sprayed upwards through the distribution air nozzles (616 b).
2. The sludge pyrolysis recycling system according to claim 1, wherein a plurality of stirring blades (231) are sequentially fixed on the spiral blades (23) of the pyrolysis reactor (2) along the extending direction of the blades, and the stirring blades (231) are square or round raised ribs.
3. The sludge pyrolysis recycling system according to claim 1, characterized in that the upper end side of the reactor cylinder (21) is provided with the heat carrier inlet (24) and the sludge inlet (25), the opposite side is provided with the pyrolysis gas outlet (27), the heat carrier inlet (24) is positioned higher than the sludge inlet (25), the lower end side of the reactor cylinder (21) is further provided with a solid outlet (26), wherein:
the sludge outlet of the pre-drying device (1) is connected with the sludge inlet (25), and sludge is fed into the pyrolysis reactor (2); the solid outlet of the feeding carrier hopper (31) is connected with the heat carrier inlet (24) and is used for feeding solid heat carriers into the pyrolysis reactor (2); the pyrolysis gas outlet (27) is connected with the inlet of the condenser (71), and pyrolysis gas after pyrolysis reaction is sent into the condenser (71); the solid outlet (26) is connected with the discharging carrier bucket (32) and discharges the solid mixture after the pyrolysis reaction into the discharging carrier bucket (32).
4. A sludge pyrolysis recycling system according to claim 3, characterized in that the pyrolysis gas outlet (27) of the pyrolysis reactor (2) is in communication with a number of side exhaust openings (271), which side exhaust openings (271) extend into the reactor cylinder (21) for collecting the pyrolysis gas inside and leading the collected pyrolysis gas to the pyrolysis gas outlet (27) for discharge.
5. Sludge pyrolysis recycling system according to claim 1, characterized in that the gas outlet of the cyclone separator (8) is connected with the gas inlet of the pre-drying device (1), and the flue gas in the cyclone separator (8) is sent into the pre-drying device (1) as a heat source for drying sludge; and the flue gas after heat exchange in the pre-drying device (1) is sent into a tail gas induced draft fan (11) through a flue gas outlet, and is discharged from the tail gas induced draft fan (11).
6. Sludge pyrolysis reclamation system according to any of claims 1 to 5, characterized in that the gas outlet of the condenser (71) is connected to the hot fume furnace (5) and non-condensable gas in the condenser (71) is fed into the hot fume furnace (5) as fuel.
7. A method for pyrolysis of sludge, characterized in that the sludge is subjected to pyrolysis treatment using the sludge pyrolysis recycling system according to any one of claims 1 to 6, comprising the steps of:
step 1: the sludge containing water is sent into a pre-drying device for pre-drying;
step 2: the sludge after pre-drying is sent into a pyrolysis reactor to be mixed with a solid heat carrier, and pyrolysis reaction is carried out to obtain pyrolysis gas and solid matters containing the solid heat carrier;
step 3: sending the high-temperature pyrolysis gas in the pyrolysis reactor into a condenser, and condensing to obtain liquid and non-condensable gas;
step 4: separating water and oil from the liquid obtained by condensation in the condenser in an oil-water separator;
step 5: feeding the solids in the pyrolysis reactor into a heating riser where the solids are heated by flue gas from a hot flue gas furnace and lifted into a feed carrier hopper;
step 6: feeding the solid heat carrier in the feeding carrier hopper into a pyrolysis reactor to be mixed with the pre-dried sludge;
step 7: and sending the dust-containing flue gas in the feeding carrier hopper into a cyclone separator to separate solids and flue gas, and discharging the solids as residues.
8. The sludge pyrolysis method as claimed in claim 7, wherein the non-condensable gas obtained by condensing in the condenser in the step 3 is fed into the hot smoke furnace to be used as fuel.
9. The sludge pyrolysis method as claimed in claim 7, wherein the flue gas separated from the dust-containing flue gas in step 7 is fed into the pre-drying device as a heat source for drying the sludge.
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| CN112063406B (en) * | 2020-10-08 | 2021-12-28 | 王玲娟 | Waste tire pyrolysis reaction furnace |
| CN113501653A (en) * | 2021-07-30 | 2021-10-15 | 重庆文理学院 | Sectional type electromagnetic pyrolysis recycling treatment method and system for sludge |
| CN117105505B (en) * | 2023-10-23 | 2024-01-30 | 清有生态科技(上海)有限公司 | Dewatering pyrolysis gasification device for biological sludge treatment |
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