CN111676042A - Novel continuous thermal cracking reaction system and treatment method thereof - Google Patents
Novel continuous thermal cracking reaction system and treatment method thereof Download PDFInfo
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- 238000006243 chemical reaction Methods 0.000 title claims abstract description 285
- 238000004227 thermal cracking Methods 0.000 title claims abstract description 103
- 238000000034 method Methods 0.000 title claims abstract description 48
- 238000000197 pyrolysis Methods 0.000 claims abstract description 282
- 239000002994 raw material Substances 0.000 claims abstract description 77
- 239000007789 gas Substances 0.000 claims abstract description 68
- 238000007599 discharging Methods 0.000 claims abstract description 65
- 239000007790 solid phase Substances 0.000 claims abstract description 48
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 32
- 239000003546 flue gas Substances 0.000 claims abstract description 32
- 238000001816 cooling Methods 0.000 claims abstract description 27
- 238000009833 condensation Methods 0.000 claims abstract description 23
- 230000005494 condensation Effects 0.000 claims abstract description 23
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- 238000010438 heat treatment Methods 0.000 claims description 26
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- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 11
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Classifications
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- 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
- C10B53/07—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form of solid raw materials consisting of synthetic polymeric materials, e.g. tyres
-
- 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
- C10B57/02—Multi-step carbonising or coking processes
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
- C10G1/10—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal from rubber or rubber waste
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/10—Feedstock materials
- C10G2300/1003—Waste materials
-
- 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
- Y02P20/141—Feedstock
- Y02P20/143—Feedstock the feedstock being recycled material, e.g. plastics
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- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Organic Chemistry (AREA)
- Materials Engineering (AREA)
- Life Sciences & Earth Sciences (AREA)
- Wood Science & Technology (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Separation, Recovery Or Treatment Of Waste Materials Containing Plastics (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The invention provides a novel continuous thermal cracking reaction system and a treatment method thereof, belonging to the field of waste resource utilization. The system comprises a reaction raw material feeding device, a three-stage continuous step pyrolysis device and a flue gas purification device, wherein the reaction raw material feeding device, the three-stage continuous step pyrolysis device and the flue gas purification device are sequentially arranged, and the three-stage continuous step pyrolysis device is communicated with a discharge hole of the reaction raw material feeding device. The three-stage continuous cascade pyrolysis device comprises a first pyrolysis reaction unit, a second pyrolysis reaction unit communicated with a discharge port (I) of the first pyrolysis reactor, and a third pyrolysis reaction unit communicated with a discharge port (II) of the second pyrolysis reactor. The invention comprises the following steps: the method comprises the steps of raw material feeding, thermal cracking reaction, solid-phase product discharging, hot oil gas condensation and cooling treatment, pyrolysis gas recycling and flue gas treatment. The reaction system and the treatment method thereof can be used for preparing the carbon black or oil product with less impurities and good quality.
Description
Technical Field
The invention belongs to the field of waste resource utilization, and particularly relates to a novel continuous thermal cracking reaction system and a treatment method thereof.
Background
With the development of global economy, the vigorous development of the automobile and rubber-plastic industry is driven, a large amount of waste rubber-plastic solid wastes are generated every year, and particularly, waste tires are more prominent. However, the natural degradation time of the waste tires exceeds hundreds of years, and if proper treatment methods are not adopted or recycling is carried out, not only is the waste of resources caused, but also great harm is caused to safety, health, land and ecological environment. The main raw material rubber (including natural rubber and synthetic rubber) of the waste tire is hydrocarbon polymer, which contains about 88% of carbon component, and the carbon black in the tire formula accounts for about 30-40% of the total mass of the tire and belongs to 99% of pure carbon, so that the carbon content in the waste tire is extremely high, about twice of that of coal, and the waste tire has better utilization potential and value.
At present, thermal cracking is generally considered in the industry as a final means for recycling waste tires, so that not only is the ecological problem effectively solved, but also the full components of the waste tires can be recycled. However, the conventional single-stage continuous thermal cracking method has the defects of uncontrollable reaction process, complex components of thermal cracking products, low flash point, poor quality and the like, so that the development of a novel thermal cracking reaction system with high efficiency and high quality of the thermal cracking products is an urgent issue to be solved by those skilled in the art.
Disclosure of Invention
The invention provides a novel continuous thermal cracking reaction system with controllable thermal cracking reaction process, high efficiency and good product quality and a treatment method thereof, aiming at the technical problems of uncontrollable reaction process, mixed components of thermal cracking products, low flash point, poor quality and the like of a single-stage continuous thermal cracking method in the prior art.
In order to achieve the purpose, the invention adopts the technical scheme that:
the novel continuous thermal cracking reaction system comprises a reaction raw material feeding device, a three-stage continuous step pyrolysis device and a flue gas purification device, wherein the three-stage continuous step pyrolysis device is communicated with a discharge hole of the reaction raw material feeding device, and the flue gas purification device is communicated with a flue gas outlet of the three-stage continuous step pyrolysis device;
the three-stage continuous cascade pyrolysis device comprises a first pyrolysis reaction unit, a second pyrolysis reaction unit communicated with a first pyrolysis reactor discharge port (I) of the first pyrolysis reaction unit, and a third pyrolysis reaction unit communicated with a second pyrolysis reactor discharge port (II) of the second pyrolysis reaction unit.
Preferably, the reaction raw material feeding device comprises a spiral feeding unit, a spiral cavity-free unit and a reaction raw material feeding device discharge port which are sequentially arranged from front to back;
a raw material feeding hole is formed in the top of the spiral feeding unit; and a spiral shaft and spiral blades are arranged in the spiral feeding unit and used for pushing the reaction raw materials to one side of a discharge port of the reaction raw material feeding device.
Preferably, the first pyrolysis reaction unit comprises a first pyrolysis reactor, a first pyrolysis reactor heating jacket and a first gas-solid two-phase discharging machine which are sequentially arranged from front to back;
the second pyrolysis reaction unit comprises a second solid-phase feeder, a second pyrolysis reactor heating jacket and a second gas-solid two-phase discharging machine which are sequentially arranged from front to back;
the third pyrolysis reaction unit comprises a third solid-phase feeder, a third pyrolysis reactor heating jacket and a third gas-solid two-phase discharging machine which are sequentially arranged from front to back, and a third pyrolysis reactor discharging hole (III) is further formed in the third pyrolysis reactor.
Preferably, the discharge port (I) of the first pyrolysis reactor, the discharge port (II) of the second pyrolysis reactor and the discharge port (III) of the third pyrolysis reactor are respectively arranged at the bottom of the first gas-solid two-phase discharger, the bottom of the second gas-solid two-phase discharger and the bottom of the third gas-solid two-phase discharger.
Preferably, the first pyrolysis reactor discharge port (I) is communicated with a first solid-phase feeder, and the second pyrolysis reactor discharge port (II) is communicated with a second solid-phase feeder.
Preferably, pyrolysis oil gas outlets are formed in the first gas-solid two-phase discharging machine, the second gas-solid two-phase discharging machine and the third gas-solid two-phase discharging machine;
a spiral shaft and spiral blades are further arranged inside the first gas-solid two-phase discharging machine, the second gas-solid two-phase discharging machine and the third gas-solid two-phase discharging machine and are used for respectively pushing the reaction raw materials to one side of the first pyrolysis reactor, one side of the second pyrolysis reactor and one side of the third pyrolysis reactor;
and forward helical blades and reverse helical blades are sequentially arranged and not arranged on the helical shafts of the second gas-solid two-phase discharging machine and the third gas-solid two-phase discharging machine which respectively correspond to the second solid-phase feeding machine and the third solid-phase feeding machine.
Preferably, the system further comprises an oil gas condensation cooling device communicated with the pyrolysis oil gas outlet, a pyrolysis gas recycling device used for providing heat energy for the first pyrolysis reaction unit and the second pyrolysis reaction unit, and a pyrolysis carbon treatment device communicated with the discharge port (III) of the third pyrolysis reactor.
The invention also provides a novel continuous thermal cracking treatment method, which comprises the following steps:
a raw material feeding step of adding reaction raw materials into a feeding device of the thermal cracking reaction system;
a thermal cracking reaction step, namely adding the reaction raw materials into the feeding device, and then feeding the reaction raw materials into a thermal cracking device to perform three-stage continuous cascade thermal cracking reaction to finally obtain a pyrolysis product;
a solid-phase product discharging step, namely cooling the solid-phase product generated in the thermal cracking reaction step of the reaction raw material to obtain pyrolytic carbon for recycling;
a step of condensation and cooling treatment of hot oil gas, in which the hot oil gas generated in the step of thermal cracking reaction of the reaction raw material is cooled, and condensed oil is obtained and then recovered;
a pyrolysis gas recycling step, namely recycling pyrolysis gas generated in the thermal cracking reaction step of the reaction raw materials to provide heat energy for the thermal cracking reaction step;
and a flue gas treatment step, wherein the flue gas generated in the thermal cracking reaction step of the reaction raw material is treated and discharged after reaching the standard.
Preferably, the three-stage continuous cascade thermal cracking reaction in the thermal cracking reaction step includes: a first-stage pyrolysis reaction, a second-stage pyrolysis reaction and a third-stage pyrolysis reaction;
wherein the reaction conditions of the first-stage pyrolysis reaction, the second-stage pyrolysis reaction and the third-stage pyrolysis reaction are respectively 220-280 ℃ and-50-5 kPa, 360-420 ℃ and-50-5 kPa, and 450-550 ℃ and-50-5 kPa.
Preferably, the reaction raw material is selected from any one or a combination of a plurality of waste tires, waste rubber products, waste plastic products or oil sludge waste.
Compared with the prior art, the invention has the advantages and positive effects that:
1. the invention provides a novel continuous thermal cracking reaction system and a treatment method thereof, wherein three stages of continuous cascade pyrolysis reactions are arranged, three pyrolysis processes of waste tires are respectively and independently arranged into reaction sections, and the temperatures are respectively and independently controlled, so that the reaction target is clear, the heat energy consumption is lower, the reaction is more sufficient, and the reaction product has the advantages of less impurities, high quality and the like; in addition, the pyrolysis reactor selected by the invention is a liner-free rotary reactor, so that the reaction temperature field is more uniformly distributed compared with other fixed bed reactors, and the coking phenomenon caused by using a single temperature in other reactors is avoided;
2. by utilizing the novel continuous thermal cracking reaction system and the treatment method thereof provided by the invention, the energy consumption is saved, for example, the comprehensive energy consumption is 156kWh when 1t of waste tires are treated, and the energy is saved by more than 20% compared with other cracking technologies in the industry;
3. the reaction products generated by the novel continuous thermal cracking reaction system and the treatment method thereof provided by the invention are more stable in distribution and higher in quality, and 0.4t of pyrolysis oil, 0.35t of pyrolysis carbon, 0.15t of steel wire and 0.1t of gas can be produced when 1t of waste tires are treated;
the distribution is about the same as that of the products of other technologies, but the distribution is more stable. However, performance tests and practice verification show that the pyrolytic carbon produced by the technical scheme can be reused in tire manufacturing, commercial carbon black with specifications of N660 and the like can be replaced in a large proportion or completely, the pyrolytic carbon produced by other cracking technologies can only be used in industries with low requirements on carbon black, such as rubber tubes, adhesive tapes, printing ink and the like, and the market value is only one third of that of products produced by the technical scheme at most.
Drawings
FIG. 1 is a diagram of an overall apparatus of a novel continuous thermal cracking reaction system according to an embodiment of the present invention;
fig. 2 is an apparatus diagram of a first pyrolysis reactor provided in an embodiment of the present invention.
In the above figures: 1. a colloidal particle (block) conveyor belt; 2. a screw feed unit; 3. a non-helical cavity cell; 4. a discharge hole of the reaction raw material feeding device; 5-1, 5-2, 5-3, 5-4, 5-5, 5-6, 5-7, 5-8, 5-9, 5-10, 5-11, 5-12, and a mechanical sealing structure; 6. a first pyrolysis reactor; 6-1, a first pyrolysis reactor heating jacket; 7. a first gas-solid two-phase discharging machine; 8. a discharge port (I) of the first pyrolysis reactor; 9. A second solid phase feeder; 10. a second pyrolysis reactor; 10-1, a second pyrolysis reactor heating jacket; 11. A second gas-solid two-phase discharging machine; 12. a discharge hole (II) of the second pyrolysis reactor; 13. a third solid phase feeder; 14. a third pyrolysis reactor; 14-1, a third pyrolysis reactor heating jacket; 15. a third gas-solid two-phase discharging machine; 16. a discharge hole (III) of the third pyrolysis reactor; 17-1, 17-2, 17-3 and a smoke outlet; 18-1, 18-2, 18-3, flue gas lines; 19. a flue gas purification device; 20-1, 20-2 and 20-3 of pyrolysis oil gas outlet; 21-2, 21-3, pyrolysis oil gas pipeline; 22. an oil gas condensation cooling device; 23. The pyrolysis oil is sent to a refining pipeline; 24-1, 24-2, 24-3, hot flue gas lines; 25. a gas pipeline; 26. Heating furnace; 27. a pyrolytic carbon spiral feeder; 28. a magnetic separator; 29. a pyrolytic carbon pneumatic conveying device; 30. Removing the pyrolytic carbon from the modified granulation pipeline; 31-1, 31-2 and a cooling water pipeline.
Detailed Description
The technical solutions in the embodiments of the present invention will be clearly and completely described below, and it is obvious that the described embodiments are only a part of the embodiments of the present invention, and not all embodiments. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.
The embodiment of the invention provides a novel continuous thermal cracking reaction system which mainly comprises a reaction raw material feeding device, a three-stage continuous step pyrolysis device and a flue gas purification device 19, wherein the reaction raw material feeding device, the three-stage continuous step pyrolysis device and the flue gas purification device are sequentially arranged, the three-stage continuous step pyrolysis device is communicated with a discharge hole 4 of the reaction raw material feeding device, and the flue gas purification device is communicated with flue gas outlets 17-1, 17-2 and 17-3 of the three-stage continuous step pyrolysis device;
the three-stage continuous cascade pyrolysis device comprises a first pyrolysis reaction unit, a second pyrolysis reaction unit communicated with a first pyrolysis reactor discharge port (I)8 of the first pyrolysis reaction unit, and a third pyrolysis reaction unit communicated with a second pyrolysis reactor discharge port (II)12 of the second pyrolysis reaction unit.
The system selected by the invention has the characteristics that three stages of continuous cascade pyrolysis reactions are arranged, the three pyrolysis processes of the waste tire are respectively and independently arranged in the reaction section, and the temperature is respectively and independently controlled, so that the reaction target is clear, the heat energy consumption is lower, the reaction is more sufficient, and the quality of the reaction product is higher. In addition, by selecting the liner-free rotary reactor, compared with other fixed bed reactors, the reaction temperature field distribution is more uniform, and the coking phenomenon caused by using a single temperature in other reactors can be avoided.
In a preferred embodiment, the reaction raw material feeding device comprises a spiral feeding unit 2, a spiral cavity-free unit 3 and a reaction raw material feeding device discharge port 4 which are arranged in sequence from front to back;
a raw material feeding hole is formed in the top of the spiral feeding unit 2; the spiral feeding unit 2 is internally provided with a spiral shaft and a spiral blade and used for pushing the reaction raw materials to one side of a discharge port 4 of the reaction raw material feeding device.
In the above preferred embodiment, the junked tire crumb is conveyed to the screw feeding unit 2 of the reaction raw material feeding device, and under the action of the screw shaft and the screw blade, the crumb material enters the non-screw cavity unit 3 again to form local stacking. The purpose of the spiral-free cavity unit 3 here is to: because the unit is an oxygen-insulated self-sealing structure, the reaction system can be ensured to be in an oxygen-insulated state so as to ensure the safe operation of the whole system.
In a preferred embodiment, the first pyrolysis reaction unit comprises a first pyrolysis reactor 6, a first pyrolysis reactor heating jacket 6-1 and a first gas-solid two-phase discharging machine 7 which are arranged in sequence from front to back;
the second pyrolysis reaction unit comprises a second solid-phase feeder 9, a second pyrolysis reactor 10, a second pyrolysis reactor heating jacket 10-1 and a second gas-solid two-phase discharging machine 11 which are sequentially arranged from front to back;
the third pyrolysis reaction unit comprises a third solid-phase feeder 13, a third pyrolysis reactor 14, a third pyrolysis reactor heating jacket 14-1 and a third gas-solid two-phase discharging machine 15 which are sequentially arranged from front to back, and a third pyrolysis reactor discharging hole (III)16 is further formed in the third pyrolysis reactor.
In the above preferred embodiment, the first pyrolysis reaction unit, the second pyrolysis reaction unit and the third pyrolysis reaction unit are all micro-tilt-angle rotary reactors, the three pyrolysis reaction units form a cascade pyrolysis system through cascade reaction, the three reaction units are all provided with fixed outer cavity jackets, and a high-performance mechanical sealing structure is arranged between the outer cavity jackets and the reactors. In addition, high-performance mechanical sealing structures 5-1, 5-2, 5-3, 5-4, 5-5, 5-6, 5-7, 5-8, 5-9, 5-10, 5-11 and 5-12 are arranged between the first pyrolysis reactor and the first gas-solid two-phase discharging machine, between the second solid-phase feeding machine and the second pyrolysis reactor, between the second pyrolysis reactor and the second gas-solid two-phase discharging machine, between the third solid-phase feeding machine and the third pyrolysis reactor and between the third pyrolysis reactor and the third gas-solid two-phase discharging machine, so that external gas can be prevented from permeating and gas inside the system can be prevented from escaping in the reaction process, the safe production of the system is ensured, and meanwhile, the environmental pollution caused by the leakage of reactants can be prevented.
It should be further added here that the micro-tilt in the above-mentioned micro-tilt rotary reactor specifically refers to: the inclined angle between the inclined angle and the horizontal plane is 1.2 degrees (adjustable) from the feeding end to the discharging end, the rotating speed is constant 0.3r/min (adjustable), and the included angle and the rotating speed can be adjusted according to actual production requirements.
In a preferred embodiment, the first pyrolysis reactor discharge port (I)8, the second pyrolysis reactor discharge port (II)12, and the third pyrolysis reactor discharge port (III)16 are respectively disposed at the bottom of the first gas-solid two-phase discharging machine 7, the bottom of the second gas-solid two-phase discharging machine 11, and the bottom of the third gas-solid two-phase discharging machine 15.
In a preferred embodiment, the first pyrolysis reactor outlet (I)8 is in communication with a first solid phase feeder 9 and the second pyrolysis reactor outlet (II)12 is in communication with a second solid phase feeder 13.
In the above preferred embodiment, the reaction raw material enters the second pyrolysis reactor through the second solid-phase feeder to perform the second-stage pyrolysis reaction after the first-stage pyrolysis reaction is completed in the first pyrolysis reactor, and the reaction raw material enters the third pyrolysis reactor through the third solid-phase feeder to perform the third-stage pyrolysis reaction after the second-stage pyrolysis reaction is completed in the second pyrolysis reactor.
In a preferred embodiment, pyrolysis oil gas outlets 20-1, 20-2 and 20-3 are respectively arranged on the first gas-solid two-phase discharging machine 7, the second gas-solid two-phase discharging machine 11 and the third gas-solid two-phase discharging machine 15;
a spiral shaft and spiral blades are further arranged inside the first gas-solid two-phase discharging machine 7, the second gas-solid two-phase discharging machine 11 and the third gas-solid two-phase discharging machine 15 and are used for respectively pushing the reaction raw materials to one side of the first pyrolysis reactor 6, one side of the second pyrolysis reactor 10 and one side of the third pyrolysis reactor 14;
wherein, the screw shafts of the second gas-solid two-phase discharging machine 11 and the third gas-solid two-phase discharging machine 15 which respectively correspond to the second solid-phase feeding machine 9 and the third solid-phase feeding machine 13 are sequentially provided with forward helical blades, are not provided with reverse helical blades and are provided with reverse helical blades.
In a preferred embodiment, the system further comprises an oil gas condensation cooling device 22 communicated with the pyrolysis oil gas outlets 20-1, 20-2 and 20-3, a pyrolysis gas recycling device used for providing heat energy for the first pyrolysis reaction unit and the second pyrolysis reaction unit, and a pyrolysis carbon treatment device communicated with the discharge port (III)16 of the third pyrolysis reactor.
In the above preferred embodiment, hot oil gas generated after the reaction raw materials undergo pyrolysis reaction in the three pyrolysis reactors enters the oil gas condensation cooling device through the pyrolysis oil gas outlets on the respective gas-solid two-phase discharging machines to undergo condensation cooling treatment, the coolable part is condensed to obtain condensed oil, and non-condensable gas enters the pyrolysis gas recycling device to provide heat energy for the first pyrolysis reactor, the second pyrolysis reactor and the third pyrolysis reactor.
In addition, substances such as pyrolytic carbon and the like generated after the reaction raw materials complete the third-stage pyrolysis reaction in the third pyrolysis reactor enter a pyrolytic carbon treatment device through a discharge hole (III) of the third pyrolysis reactor, and subsequent grinding, modification and granulation treatment are carried out, so that products such as high-added-value pyrolytic carbon black and the like with few impurities and good quality are finally obtained.
The invention also provides a novel continuous thermal cracking treatment method, which comprises the following steps:
(1) a raw material feeding step of adding reaction raw materials into a feeding device of the thermal cracking reaction system;
(2) a thermal cracking reaction step, namely adding the reaction raw materials into the feeding device, and then feeding the reaction raw materials into a thermal cracking device to perform three-stage continuous cascade thermal cracking reaction to finally obtain a pyrolysis product;
(3) a solid-phase product discharging step, namely cooling the solid-phase product generated in the thermal cracking reaction step of the reaction raw material to obtain pyrolytic carbon for recycling;
(4) a step of condensation and cooling treatment of hot oil gas, in which the hot oil gas generated in the step of thermal cracking reaction of the reaction raw material is cooled, and condensed oil is obtained and then recovered;
(5) a pyrolysis gas recycling step, namely recycling pyrolysis gas generated in the thermal cracking reaction step of the reaction raw materials to provide heat energy for the thermal cracking reaction step;
(6) and a flue gas treatment step, wherein the flue gas generated in the thermal cracking reaction step of the reaction raw material is treated and discharged after reaching the standard.
In the treatment method, three stages of continuous cascade pyrolysis reactions are arranged, the three pyrolysis processes of the waste tire are respectively and independently arranged in the reaction section, and the temperature is respectively and independently controlled, so that the reaction target is clear, the heat energy consumption is lower, the reaction is more sufficient, and the quality of the reaction product is higher.
In addition, the flue gas treatment step arranged in the treatment method enables toxic and harmful gases generated in the pyrolysis reaction to be effectively treated, so that the environmental pollution is prevented; the hot oil gas condensation and cooling treatment step is arranged, so that oil substances generated in the pyrolysis reaction of the waste tires can be efficiently recovered, and the comprehensive utilization rate of the waste tires is improved; the pyrolysis gas recycling step is arranged, so that the noncondensable oil gas generated by the waste tire in the pyrolysis reaction can be further recycled, and heat energy is provided for the pyrolysis device.
In a preferred embodiment, the three-stage continuous step thermal cracking reaction in the thermal cracking reaction step comprises: a first-stage pyrolysis reaction, a second-stage pyrolysis reaction and a third-stage pyrolysis reaction;
wherein the reaction conditions of the first-stage pyrolysis reaction, the second-stage pyrolysis reaction and the third-stage pyrolysis reaction are respectively 220-280 ℃ and-50-5 kPa, 360-420 ℃ and-50-5 kPa, and 450-550 ℃ and-50-5 kPa.
In the preferred embodiment described above, the purpose of the primary pyrolysis reaction is: the preheating of the waste tire colloidal particles and the desorption of the tire filling oil are realized. Wherein, the temperature of the reaction condition can be selected from 220, 230, 240, 250, 260, 270, 280 ℃ or any value in the above limited range and fall into the protection range of the invention, and the pressure can be selected from-50, -45, -40, -35, -30, -25, -20, -15, -10, -5kPa or any value in the above limited range and fall into the protection range of the invention.
The purpose of the secondary pyrolysis reaction is: the natural rubber and the synthetic rubber in the waste tire are cracked in sequence to generate organic matters and pyrolytic carbon distributed between C1-C16. Wherein, the temperature in the reaction condition can be selected from 360, 370, 380, 390, 400, 410, 420 ℃ or any value in the above limited range, and the pressure can be selected from-50, -45, -40, -35, -30, -25, -20, -15, -10, -5kPa or any value in the above limited range, and all fall into the protection range of the invention.
The purpose of the three pyrolysis reactions is: desorption of small molecular organic matters attached to the pyrolytic carbon is realized, the quality of the pyrolytic carbon is further stabilized, and the pyrolytic reaction is stopped by gradually reducing the temperature. Wherein, the temperature of the reaction condition can be selected from 450, 460, 470, 480, 490, 500, 510, 520, 530, 540, 550 ℃ or any value in the above-defined range, and the pressure can be selected from-50, -45, -40, -35, -30, -25, -20, -15, -10, -5kPa, or any value in the above-defined range.
In a preferred embodiment, the reaction raw material is selected from any one or a combination of a plurality of waste tires, waste rubber products, waste plastic products or sludge waste, but the selected raw material is not limited to the above.
In order to more clearly and specifically describe the novel continuous thermal cracking reaction system and the processing method thereof provided by the embodiments of the present invention, the following description will be made with reference to specific embodiments.
Example 1
The embodiment of the invention provides a use method of a novel continuous thermal cracking reaction system, which comprises the following specific contents:
the waste tire colloidal particles (blocks) to be treated are conveyed to a feeding hole of a reaction raw material feeding device through a colloidal particle (block) conveying belt 1, and then the waste tire colloidal particles enter the reaction raw material feeding device. Above-mentioned useless tire micelle (piece) continues to impel forward in reaction raw materials feed arrangement's spiral feed unit 2 earlier, the micelle reentrant does not have spiral cavity unit 3 (from the oxygen-insulated structure), treats that micelle (piece) gathering certain quality gets into tertiary continuous step pyrolysis device through reaction raw materials feed arrangement discharge gate 4 after, carries out syllogic pyrolytic reaction, and after the pyrolytic reaction ended, solid phase product is again through a series of modification and granulation processing back, finally obtains the pyrolysis carbon black that impurity is few, the quality is good. In addition, flue gas generated by the waste tire to be treated in the pyrolysis reaction enters a flue gas purification device 19 communicated with flue gas outlets 17-1, 17-2 and 17-3 of the three-stage continuous step pyrolysis device for purification treatment, and is discharged after reaching the standard.
Wherein, the three-stage pyrolysis reaction that above-mentioned micelle (piece) was carried out specifically is:
(1) first-stage pyrolysis reaction: the colloidal particles enter a first pyrolysis reactor 6 through a discharge port 4 of a reaction raw material feeding device, and carry out thermal cracking reaction at the temperature of 220-280 ℃ and under the condition of-50 to-5 kPa, wherein the reaction in the step is to realize the preheating of the colloidal particles (blocks) of the waste and old tires and the desorption of the tire additives mainly. The reaction is continuously carried out along with the rotation of the first pyrolysis reactor 6, reaction products are pushed to the end of a discharge hole (I)8 of the first pyrolysis reactor 6, the products obtained by the reaction enter a first gas-solid two-phase discharge machine 7, an oil-gas mixture generated in the pyrolysis reaction enters an oil-gas condensation cooling device 22 communicated with a pyrolysis oil-gas outlet 20-1 for condensation cooling treatment, condensed oil is obtained, and solid-phase materials enter a second pyrolysis reactor from the discharge hole (I)8 of the first pyrolysis reactor 6;
(2) and (3) second-stage pyrolysis reaction: solid-phase materials generated in the first-stage pyrolysis reaction enter a second pyrolysis reactor 10 and then enter the second pyrolysis reactor 10 through a second solid-phase feeder 9, and the thermal cracking reaction is carried out under the conditions of 360-420 ℃ and-50-5 kPa, wherein the reaction is to realize the sequential cracking of natural rubber, synthetic rubber and the like as main components in the waste tire to generate organic matters and pyrolytic carbon distributed between C1 and C16. The reaction is continuously carried out along with the rotation of the second pyrolysis reactor 10, reaction products are pushed to the end of a discharge hole (II)12 of the second pyrolysis reactor 10, the products obtained by the reaction enter a second gas-solid two-phase discharge machine 11, gas phases generated in the pyrolysis reaction enter an oil gas condensation cooling device 22 communicated with a pyrolysis oil gas outlet 20-2 for condensation cooling treatment, condensed oil is obtained, and solid-phase materials enter a third pyrolysis reactor from the discharge hole (II)12 of the second pyrolysis reactor 10;
(3) three-stage pyrolysis reaction: the solid phase material generated in the second-stage pyrolysis reaction enters a third pyrolysis reactor 14 through a third solid phase feeder 13, and the thermal cracking reaction is carried out under the conditions of 450-550 ℃ and-50 to-5 kPa, wherein the step of reaction is to realize desorption of small molecular organic matters attached to the pyrolytic carbon, further stabilize the quality of the pyrolytic carbon, and terminate the reaction through subsequent gradual temperature reduction. The reaction is continuously carried out along with the rotation of the third pyrolysis reactor 14, the reaction product is pushed to the end of the discharge hole (III)16 of the third pyrolysis reactor 14, the reaction product is stabilized along with the gradual termination of the thermal cracking reaction and enters the third gas-solid two-phase discharge machine 15, the gas phase generated in the thermal cracking reaction enters the oil-gas condensation cooling device 22 communicated with the pyrolysis oil-gas outlet 20-3 for condensation cooling treatment to obtain condensed oil, the solid phase material enters the pyrolysis carbon spiral feeder 27 from the discharge hole (III)16 of the third pyrolysis reactor 14, and the carbon black with less impurities and good quality is finally prepared through the processes of magnetic separation, grinding, modification, granulation and the like.
(4) In addition, in the process that the waste tires enter the three-stage continuous step pyrolysis device for treatment, after the oil-gas mixture discharged from the reaction processes of the first pyrolysis reactor 6, the second pyrolysis reactor 10 and the third pyrolysis reactor 14 is subjected to condensation treatment, the liquid phase is condensed oil, and non-condensed gas is sent to the heating furnace 26 together to provide heat energy for the first pyrolysis reactor 6, the second pyrolysis reactor 10 and the third pyrolysis reactor 14.
Example 2
The embodiment provides a novel continuous thermal cracking treatment method, which comprises the following specific contents:
(1) raw material feeding step:
conveying waste tire colloidal particles to a reaction raw material feeding device of a thermal cracking reaction system through a colloidal particle conveying belt 1, continuously advancing the waste tire colloidal particles through a spiral feeding unit 2 of the reaction raw material feeding device, feeding the colloidal particles into a spiral cavity-free unit 3 of a self-anaerobic structure, and after the colloidal particles are gathered to a certain mass, feeding the colloidal particles into a three-stage continuous step pyrolysis device through a discharge port 4 of the reaction raw material feeding device to perform three-stage pyrolysis reaction;
(2) thermal cracking reaction:
the colloidal particles enter a three-stage continuous cascade pyrolysis device through a discharge port 4 of a reaction raw material feeding device to carry out three-stage continuous cascade pyrolysis reaction, and then the pyrolysis carbon black with less impurities and good quality is obtained after modification and granulation treatment.
Wherein, the three-stage continuous cascade thermal cracking reaction specifically comprises the following steps:
one-stage pyrolysis reaction: the colloidal particles enter a first pyrolysis reactor 6 through a discharge port 4 of a reaction raw material feeding device, and carry out thermal cracking reaction at the temperature of 220-280 ℃ and under the condition of-50 kPa to-5 kPa. With the rotation of the first pyrolysis reactor 6, the reaction is continuously carried out, the reaction product is pushed to the end of a discharge port (I)8 of the first pyrolysis reactor 6, the product obtained by the reaction enters a first gas-solid two-phase discharging machine 7, and the solid-phase material enters a second pyrolysis reactor 10 from the discharge port (I)8 of the first pyrolysis reactor 6;
two-stage pyrolysis reaction: after the solid phase material generated in the first-stage pyrolysis reaction enters the second pyrolysis reactor 10 through the first solid phase feeder 9, the thermal cracking reaction is carried out under the conditions of 360-420 ℃ and-50 to-5 kPa. The reaction is continuously carried out along with the rotation of the second pyrolysis reactor 10, the reaction product is pushed to the discharge port (II)12 end of the second pyrolysis reactor 10, the product obtained by the reaction enters the second gas-solid two-phase discharging machine 11, and the solid-phase material enters the third pyrolysis reactor from the discharge port (II)12 of the second pyrolysis reactor 10;
three-stage pyrolysis reaction: after entering a third pyrolysis reactor 14 through a second solid phase feeder 13, the solid phase material generated in the second-stage pyrolysis reaction is subjected to a thermal cracking reaction at the temperature of 450-550 ℃ and under the pressure of-50 to-5 kPa. The reaction is continuously carried out along with the rotation of the third pyrolysis reactor 14, and the reaction product is pushed towards the discharge port (III)16 of the third pyrolysis reactor 14, and is stabilized along with the gradual termination of the thermal cracking reaction, and enters the third gas-solid two-phase discharge machine 15.
(3) Solid-phase product discharging step:
the stabilized solid phase material enters a pyrolytic carbon spiral feeder 27 from a discharge port (III)16 of a third pyrolytic reactor 14, is further treated by dividing wall type cooling (a refrigerant is provided by a cooling water pipeline 31-1) and then enters a magnetic separator 28, the separated pyrolytic steel wire is recycled to a temporary storage device 29, the separated crude carbon black is conveyed to a crude bin through a conveying pipeline 30 under negative pressure, and the pyrolytic carbon black with less impurities and good quality is finally prepared through the working procedures of grinding, modification, granulation and the like.
(4) A hot oil gas condensation and cooling treatment step:
products obtained by reactions generated in the first-stage pyrolysis reaction, the second-stage pyrolysis reaction and the third-stage pyrolysis reaction respectively enter a first gas-solid two-phase discharging machine 7, a second gas-solid two-phase discharging machine 11 and a third gas-solid two-phase discharging machine 15, and oil-gas mixtures generated in the pyrolysis reactions enter an oil-gas condensation cooling device 22 communicated with pyrolysis oil-gas outlets 20-1, 20-2 and 20-3 for condensation cooling treatment to obtain condensed oil;
(5) and (3) recycling pyrolysis gas:
in the process that the waste tires enter the three-stage continuous stepped pyrolysis device for treatment, after the oil-gas mixture discharged in the reaction process of the first pyrolysis reactor is condensed, the liquid phase is condensed oil, and the non-condensed gas and the gas discharged by the first gas-solid two-phase discharging machine 7 are sent to the heating furnace 26 together to provide heat energy for the first pyrolysis reactor heating jacket 6-1, the second pyrolysis reactor heating jacket 10-1 and the third pyrolysis reactor heating jacket 14-1.
(6) Flue gas treatment:
flue gas generated in the pyrolysis reaction of the waste tires to be treated enters a flue gas purification device 19 through flue gas outlets 17-1, 17-2 and 17-3 and flue gas pipelines 18-1, 18-2 and 18-3 to be subjected to flue gas purification treatment, and is discharged after reaching the standard;
example 3
The following achievements are obtained in actual production practice by utilizing the using method of the novel continuous thermal cracking reaction system and the novel continuous thermal cracking treatment method provided by the embodiment 1-2 of the invention:
(1) in the aspect of energy consumption: when the system and the treatment method are utilized, the comprehensive energy consumption is 156kWh when 1t of waste tires are treated, and the energy is saved by more than 20 percent compared with other cracking technologies in the industry;
(2) product distribution and quality: when the system and the processing method are utilized, 0.4t of pyrolysis oil, 0.35t of pyrolysis carbon, 0.15t of steel wire and 0.1t of gas can be produced when 1t of waste tires are processed.
The product distribution is about the same as other pyrolysis technologies, but the distribution is more stable. Tests and practices prove that the pyrolytic carbon produced by the method can be reused in tire manufacturing, commercial carbon black with specifications of N660 and the like can be replaced in a large proportion or completely, the pyrolytic carbon produced by other cracking technologies can only be used in industries with low requirements on carbon black, such as rubber tubes, adhesive tapes, printing ink and the like, and the market value is only one third of that of products produced by the technology at most.
Comparative example 1
The comparative example provides a single-stage continuous thermal cracking treatment system and a single-stage continuous thermal cracking treatment method for waste tires, and the specific contents are as follows:
a single-stage continuous thermal cracking treatment system for waste tires, which mainly comprises the following devices:
a spiral feeding device, a single-section rotary lining-free horizontal reactor and a discharging device.
The processing method:
(1) waste tire colloidal particles enter a single-section rotary type lining-free horizontal reactor through a spiral feeding system with an oxygen-insulating self-sealing structure, the reactor is provided with a heating jacket, materials are pushed to a discharging end along with the rotation of the reactor in the reactor, the desorption of tire additives and the thermal cracking of components such as synthetic rubber and natural rubber are completed, and the materials are sent to a discharging system after all chemical reaction processes are completed;
(2) hot oil gas generated by cracking enters a condensation cooling treatment unit, non-condensable gas is used as fuel for heating a reactor, and a condensed oil phase is used as a product;
(3) the solid carbon enters a subsequent deep processing unit, and the reaction is stopped by dividing wall type cooling in the conveying process.
Comparative example 2
The comparative example provides an intermittent thermal cracking treatment system and a treatment method thereof, and the specific contents are as follows:
a batch thermal cracking system, mainly comprising the following devices:
the main equipment of the intermittent thermal cracking treatment device is an intermittent horizontal reactor with a lining.
The processing method:
(1) adding the whole waste tire into a reactor, wherein the reactor is provided with a heating jacket, and heating is carried out through external fuel or combustible gas generated by thermal cracking so as to carry out thermal cracking reaction;
(2) hot oil gas generated by cracking enters a condensation cooling unit, non-condensable gas is used as fuel for heating a reactor, and a condensed oil phase is used as a product;
(3) and after the reaction is ended, stopping heating, opening the reactor after the reactor is naturally cooled, and discharging the reacted solid carbon and steel wires to serve as a reaction unit. After the reactor was cleaned, the above process was repeated as a second reaction unit.
Comparative example 3
The comparative example provides a thermal cracking device and a thermal cracking method of a multi-section fixed bed, and the specific contents are as follows:
a thermal cracking device and method of a multi-stage fixed bed mainly comprises the following devices:
the main equipment is a thermal cracking device with a multi-section fixed bed;
the processing method:
the thermal cracking device and the method of the multi-section fixed bed are basically consistent with the treatment process provided in the embodiment of the invention. The main difference lies in the different types of the three-stage reactor. The shell of the three-section reactor selected by the thermal cracking device of the multi-section fixed bed is fixed on the mounting base, the inside of the shell is provided with a multi-bed layer transverse conveying device or a built-in spiral conveying device, and the reaction is continuously carried out by the movement of the bed layers or the rotation of the spiral.
Compared with the novel continuous thermal cracking reaction system and the treatment method thereof provided by the invention, the technical scheme disclosed in the comparative examples 1-3 has various defects, and specifically comprises the following steps:
the single-stage continuous waste tire thermal cracking treatment system has the defects that:
(1) the single heating jacket is adopted, the temperature condition is single, the grading control cannot be realized, and the energy consumption is more than 120 percent of that of the invention;
(2) the processes of desorption, thermal cracking, product desorption and the like of raw materials and additives are mixed in the same reactor, and hot oil gas carries a large amount of particles to enter a condenser, so that the condenser is easily blocked, the maintenance is frequent, and the long-period continuous operation of the device is influenced;
(3) the reaction termination process is only dependent on a cold water jacket in the subsequent solid phase conveying process, so that the desorption effect of volatile components in the product is poor, the subsequent grinding, modification and granulation of the pyrolytic carbon are not facilitated, and the application of the pyrolytic carbon in tire manufacturing is influenced.
The main drawbacks of the batch thermal cracking process and apparatus are:
(1) the single heating jacket is adopted, the temperature condition is single, the grading control cannot be realized, the homogenization degree of materials is poor, the uniformity of the pyrolytic carbon black is poor, the high-value application cannot be realized, and the application to the tire manufacturing cannot be realized;
(2) the reactor is frequently opened, the temperature of the cavity of the reactor is frequently heated and cooled, energy loss is caused, and the energy consumption is more than 150 percent of that of the reactor;
(3) the reactor is frequently opened, the service life of the equipment is influenced, and meanwhile, the residual flammable and combustible gaseous products leak out, so that the environment is polluted and potential safety hazards exist.
The main defects of the multi-stage fixed bed thermal cracking device and method are as follows:
(1) the reaction bed layer is thick, so that the temperature distribution is uneven, the reaction efficiency is further influenced, and the reaction degree is greatly influenced by space due to the uneven temperature field, and the product is unstable and is not beneficial to the generation of high-performance products;
(2) the reactants in the reactor are pushed by the conveying device, a gap is reserved between the conveying device and the inner cavity of the reactor, and the reaction solid products are easy to deposit on the lower part of the reactor to form dead corners and form coking after being heated for a long time.
Compared with the comparative example, the system selected by the invention is characterized in that three stages of continuous cascade pyrolysis reactions are arranged, the three pyrolysis processes of the waste tires or other reaction raw materials are respectively and independently arranged in the reaction section, and the temperature is respectively and independently controlled, so that the reaction target is clear, the heat energy consumption is lower, the reaction is more sufficient, and the reaction efficiency and the product quality are higher. In addition, by selecting the liner-free rotary reactor, compared with other fixed bed reactors, the reaction temperature field distribution is more uniform, the reaction efficiency is higher, the phenomena of coking caused by single temperature of other reactors and influence on the product quality caused by secondary reaction can be avoided, and the problems in the existing thermal cracking technology can be well solved.
Claims (10)
1. The novel continuous thermal cracking reaction system is characterized by comprising a reaction raw material feeding device, a three-stage continuous step pyrolysis device and a flue gas purification device (19), wherein the three-stage continuous step pyrolysis device is communicated with a discharge hole (4) of the reaction raw material feeding device, and the flue gas purification device is communicated with flue gas outlets (17-1, 17-2 and 17-3) of the three-stage continuous step pyrolysis device;
the three-stage continuous cascade pyrolysis device comprises a first pyrolysis reaction unit, a second pyrolysis reaction unit communicated with discharge ports (I) (8) of first pyrolysis reactors of the first pyrolysis reaction unit, and a third pyrolysis reaction unit communicated with discharge ports (II) (12) of second pyrolysis reactors of the second pyrolysis reaction unit.
2. The novel continuous thermal cracking reaction system of claim 1, wherein the reaction raw material feeding device comprises a spiral feeding unit (2), a spiral cavity-free unit (3) and a reaction raw material feeding device discharge port (4) which are arranged in sequence from front to back;
a raw material feeding hole is formed in the top of the spiral feeding unit (2); the spiral feeding unit (2) is internally provided with a spiral shaft and a spiral blade and used for pushing the reaction raw materials to one side of a discharge hole (4) of the reaction raw material feeding device.
3. The novel continuous thermal cracking reaction system according to claim 1, wherein the first pyrolysis reaction unit comprises a first pyrolysis reactor (6), a first pyrolysis reactor heating jacket (6-1) and a first gas-solid two-phase discharging machine (7) which are arranged in sequence from front to back;
the second pyrolysis reaction unit comprises a second solid-phase feeder (9), a second pyrolysis reactor (10), a second pyrolysis reactor heating jacket (10-1) and a second gas-solid two-phase discharging machine (11) which are sequentially arranged from front to back;
the third pyrolysis reaction unit comprises a third solid-phase feeder (13), a third pyrolysis reactor (14), a third pyrolysis reactor heating jacket (14-1) and a third gas-solid two-phase discharging machine (15), which are sequentially arranged from front to back, and the third pyrolysis reactor is also provided with a third pyrolysis reactor discharging hole (III) (16).
4. The novel continuous thermal cracking reaction system of claim 3, wherein the first pyrolysis reactor discharge port (I) (8), the second pyrolysis reactor discharge port (II) (12) and the third pyrolysis reactor discharge port (III) (16) are respectively arranged at the bottom of the first gas-solid two-phase discharging machine (7), the bottom of the second gas-solid two-phase discharging machine (11) and the bottom of the third gas-solid two-phase discharging machine (15).
5. The novel continuous thermal cracking reaction system of claim 4, wherein the first pyrolysis reactor outlet (I) (8) is in communication with a first solid phase feeder (9), and the second pyrolysis reactor outlet (II) (12) is in communication with a second solid phase feeder (13).
6. The novel continuous thermal cracking reaction system according to claim 3 or 4, wherein pyrolysis oil gas outlets (20-1, 20-2, 20-3) are formed in the first gas-solid two-phase discharging machine (7), the second gas-solid two-phase discharging machine (11) and the third gas-solid two-phase discharging machine (15);
a spiral shaft and spiral blades are further arranged inside the first gas-solid two-phase discharging machine (7), the second gas-solid two-phase discharging machine (11) and the third gas-solid two-phase discharging machine (15) and are used for respectively pushing the reaction raw materials to one side of the first pyrolysis reactor (6), one side of the second pyrolysis reactor (10) and one side of the third pyrolysis reactor (14);
wherein, the screw shafts of the second gas-solid two-phase discharging machine (11) and the third gas-solid two-phase discharging machine (15) which respectively correspond to the second solid-phase feeding machine (9) and the third solid-phase feeding machine (13) are sequentially provided with forward helical blades, are not provided with reverse helical blades and are provided with reverse helical blades.
7. The novel continuous thermal cracking reaction system according to claim 6, further comprising an oil gas condensation cooling device (22) communicated with the pyrolysis oil gas outlets (20-1, 20-2, 20-3), a pyrolysis gas recycling device for providing thermal energy for the first and second pyrolysis reaction units, and a pyrolysis carbon treatment device communicated with the discharge port (III) (16) of the third pyrolysis reactor.
8. A novel continuous thermal cracking treatment method is characterized by comprising the following steps:
a raw material feeding step of adding reaction raw materials into a feeding device of the thermal cracking reaction system;
a thermal cracking reaction step, namely adding the reaction raw materials into the feeding device, and then feeding the reaction raw materials into a thermal cracking device to perform three-stage continuous cascade thermal cracking reaction to finally obtain a pyrolysis product;
a solid-phase product discharging step, namely cooling the solid-phase product generated in the thermal cracking reaction step of the reaction raw material to obtain pyrolytic carbon for recycling;
a step of condensation and cooling treatment of hot oil gas, in which the hot oil gas generated in the step of thermal cracking reaction of the reaction raw material is cooled, and condensed oil is obtained and then recovered;
a pyrolysis gas recycling step, namely recycling pyrolysis gas generated in the thermal cracking reaction step of the reaction raw materials to provide heat energy for the thermal cracking reaction step;
and a flue gas treatment step, wherein the flue gas generated in the thermal cracking reaction step of the reaction raw material is treated and discharged after reaching the standard.
9. The novel continuous thermal cracking process of claim 8, wherein the three-stage continuous stepwise thermal cracking reaction in the thermal cracking reaction step comprises: a first-stage pyrolysis reaction, a second-stage pyrolysis reaction and a third-stage pyrolysis reaction;
wherein the reaction conditions of the first-stage pyrolysis reaction, the second-stage pyrolysis reaction and the third-stage pyrolysis reaction are respectively 220-280 ℃ and-50-5 kPa, 360-420 ℃ and-50-5 kPa, and 450-550 ℃ and-50-5 kPa.
10. The novel continuous thermal cracking process according to claim 8 or 9, wherein the reaction raw material is selected from any one or a combination of a plurality of waste tires, waste rubber products, waste plastic products, and waste oil sludge.
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