CN117025248A - Pyrolysis method for waste plastics - Google Patents
Pyrolysis method for waste plastics Download PDFInfo
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- CN117025248A CN117025248A CN202311006209.4A CN202311006209A CN117025248A CN 117025248 A CN117025248 A CN 117025248A CN 202311006209 A CN202311006209 A CN 202311006209A CN 117025248 A CN117025248 A CN 117025248A
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- Prior art keywords
- pyrolysis
- waste plastics
- gas
- liquid
- pyrolysis gas
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- 238000000197 pyrolysis Methods 0.000 title claims abstract description 230
- 239000002699 waste material Substances 0.000 title claims abstract description 68
- 239000004033 plastic Substances 0.000 title claims abstract description 57
- 229920003023 plastic Polymers 0.000 title claims abstract description 57
- 238000000034 method Methods 0.000 title claims abstract description 26
- 239000007788 liquid Substances 0.000 claims abstract description 63
- 238000001816 cooling Methods 0.000 claims abstract description 25
- 239000002893 slag Substances 0.000 claims description 12
- 238000010438 heat treatment Methods 0.000 claims description 10
- 238000001914 filtration Methods 0.000 claims description 9
- 238000007493 shaping process Methods 0.000 claims description 9
- 238000006243 chemical reaction Methods 0.000 claims description 8
- 230000004048 modification Effects 0.000 claims description 8
- 238000012986 modification Methods 0.000 claims description 8
- 239000011949 solid catalyst Substances 0.000 claims description 8
- 238000000746 purification Methods 0.000 claims description 7
- 239000003054 catalyst Substances 0.000 claims description 6
- 238000006555 catalytic reaction Methods 0.000 claims description 6
- 230000000881 depressing effect Effects 0.000 claims description 5
- 238000002156 mixing Methods 0.000 claims description 5
- 238000007599 discharging Methods 0.000 claims description 4
- 238000002309 gasification Methods 0.000 claims description 4
- 239000003623 enhancer Substances 0.000 claims description 2
- 230000007306 turnover Effects 0.000 abstract description 9
- 239000007789 gas Substances 0.000 description 45
- 238000003860 storage Methods 0.000 description 12
- 239000000498 cooling water Substances 0.000 description 7
- 239000012535 impurity Substances 0.000 description 6
- 238000007600 charging Methods 0.000 description 5
- 239000000446 fuel Substances 0.000 description 5
- 239000000463 material Substances 0.000 description 4
- 238000009833 condensation Methods 0.000 description 3
- 230000005494 condensation Effects 0.000 description 3
- 239000003921 oil Substances 0.000 description 3
- 230000008569 process Effects 0.000 description 3
- 239000002994 raw material Substances 0.000 description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 3
- 239000004129 EU approved improving agent Substances 0.000 description 2
- 239000000654 additive Substances 0.000 description 2
- 230000000996 additive effect Effects 0.000 description 2
- 238000005336 cracking Methods 0.000 description 2
- 230000006866 deterioration Effects 0.000 description 2
- 239000000706 filtrate Substances 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 239000002808 molecular sieve Substances 0.000 description 2
- 230000003647 oxidation Effects 0.000 description 2
- 238000007254 oxidation reaction Methods 0.000 description 2
- 230000002035 prolonged effect Effects 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 description 2
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 230000009089 cytolysis Effects 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 239000002283 diesel fuel Substances 0.000 description 1
- 239000003546 flue gas Substances 0.000 description 1
- 239000000295 fuel oil Substances 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 238000010079 rubber tapping Methods 0.000 description 1
Classifications
-
- 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
- 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
- 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
- C10G1/002—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal in combination with oil conversion- or refining 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
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/10—Feedstock materials
- C10G2300/1003—Waste materials
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Organic Chemistry (AREA)
- Life Sciences & Earth Sciences (AREA)
- Wood Science & Technology (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Materials Engineering (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The invention provides a pyrolysis method of waste plastics, which belongs to the field of pyrolysis of waste plastics, and specifically comprises the steps of firstly pyrolyzing waste plastics at the temperature of not lower than 400 ℃ to generate mixed pyrolysis gas, then carrying out secondary pyrolysis treatment on the mixed pyrolysis gas to obtain pyrolysis gas, and cooling the pyrolysis gas to obtain pyrolysis liquid. The pyrolysis temperature can be increased to more than 400 ℃, the pyrolysis temperature is not controlled below 380 ℃, and the generation of pyrolysis liquid with high wax content can be prevented, so that the pyrolysis rate of waste plastics is greatly improved. In addition, the month turnover rate can reach 20-25 cycles through the special designed waste plastic pyrolysis mode of the batch pyrolysis subsystem.
Description
Technical Field
The invention relates to the field of pyrolysis of waste plastics, in particular to a pyrolysis method of waste plastics.
Background
FIG. 1 shows a system (hereinafter referred to as the system) defined in GB/T32662-2016 "complete production equipment for producing pyrolysis oil of waste rubber and waste plastics", wherein the pyrolysis oil device for waste plastics is manufactured and put into practical use according to the standard, and one cycle of the system comprises the processes of charging, heating, pyrolysis, cooling, deslagging and the like.
The system has the following defects in application: (1) The prior art device is a general device for waste rubber and waste plastic, does not distinguish the obvious difference of the process in the pyrolysis process of the waste rubber and the waste plastic, and is completely different in the aspects of raw material shape, component composition, raw material density, stacking weight, water content (waste plastic is higher than waste rubber by more than 5 percent), and the like, so that the charging and heating time period of the waste plastic is prolonged by about 8 hours.
(2) The waste plastic raw materials have complex components, PP, PE, PS, PVC, PET and the like, are mixed together, and have different pyrolysis temperatures, and are obviously different from the waste rubber, after pyrolysis is started, excessive pyrolysis liquid with high wax content is generated for controlling the pyrolysis temperature to be below 380 ℃, and the corresponding pyrolysis time length is prolonged by at least 4 hours compared with the waste rubber.
(3) The existing waste plastic pyrolysis device needs 50 hours for one cycle period, the monthly turnover rate can only be kept between 10 and 12 cycles, and the equipment utilization rate is too low.
In summary, the method for cracking and oiling the waste rubber and the waste plastic is not suitable for general use, and a special method for pyrolysis of the waste plastic should be designed.
In view of this, the present invention has been made.
Disclosure of Invention
The invention provides a pyrolysis method of waste plastics, which aims to solve the problem that the pyrolysis oiling method of waste rubber and waste plastics in the prior art is not suitable for common use.
In order to solve the problems, the invention adopts the following scheme:
a pyrolysis method for waste plastics includes such steps as first pyrolyzing waste plastics at 400 deg.C or higher to generate mixed pyrolysis gas, then performing secondary pyrolysis to obtain pyrolysis gas, and cooling to obtain pyrolysis liquid.
The pyrolysis temperature can be increased to more than 400 ℃, the pyrolysis temperature is not controlled below 380 ℃, and the generation of pyrolysis liquid with high wax content can be prevented, so that the pyrolysis rate of waste plastics is greatly improved. In addition, the month turnover rate can reach 20-25 cycles through the special designed waste plastic pyrolysis mode of the batch pyrolysis subsystem.
In other preferred embodiments, the waste plastic pyrolysis method includes the steps of:
step a, first pyrolysis treatment: first pyrolyzing waste plastics at a temperature of not lower than 400 ℃ and generating mixed pyrolysis gas;
step b, secondary pyrolysis treatment: carrying out secondary pyrolysis treatment on the mixed pyrolysis gas to obtain primary pyrolysis gas;
step c, cooling treatment: cooling the primary pyrolysis gas to obtain primary pyrolysis liquid;
and d, purifying: and heating and gasifying the primary pyrolysis liquid to form secondary pyrolysis gas, carrying out catalytic reaction on the secondary pyrolysis gas, and cooling to obtain the secondary pyrolysis liquid.
In other preferred embodiments, the step a specifically includes:
first pyrolyzing waste plastics in a rotary main pyrolyzer at the temperature of not lower than 450 ℃ to generate mixed pyrolysis gas and hot slag;
and when the temperature in the rotary main pyrolyzer is reduced to 340-360 ℃, discharging the hot slag and cooling.
In other preferred schemes, the step b specifically comprises the steps of introducing the mixed pyrolysis gas into a secondary pyrolysis device for secondary pyrolysis treatment, and then introducing the mixed pyrolysis gas into a dewaxing and pour point depressing device for dewaxing treatment to obtain primary pyrolysis gas.
In other preferred embodiments, the step c specifically includes introducing the primary pyrolysis gas into a cooling tank with a condensation pipeline, and condensing the primary pyrolysis gas in the condensation pipeline to obtain a primary pyrolysis liquid.
In other preferred schemes, the step d is specifically that the primary pyrolysis liquid is introduced into a rotary purification reaction device, secondary pyrolysis gas is obtained after heating and gasification, then the secondary pyrolysis gas is introduced into a modification and molecular shaping device for catalytic reaction, and then the secondary pyrolysis gas after catalytic reaction is cooled to obtain the secondary pyrolysis liquid.
In other preferred embodiments, the step d further includes: and introducing the secondary pyrolysis liquid into a pyrolysis liquid filtering device, filtering, and mixing with at least three pyrolysis liquid enhancers to obtain mixed pyrolysis liquid.
In other preferred embodiments, the secondary pyrolysis device is filled with at least one catalyst.
In other preferred embodiments, the modification and molecular shaping device is filled with at least two catalysts.
In other preferred embodiments, the catalyst is a solid catalyst.
Compared with the prior art, the invention has the following beneficial effects:
first, the pyrolysis temperature in this scheme can be improved to more than 400 ℃, need not control below 380 ℃, can prevent that the pyrolysis liquid that wax content is high from producing to greatly improve waste plastic pyrolysis rate.
Secondly, the month turnover rate can reach 20-25 cycles through the special designed waste plastic pyrolysis mode of the batch pyrolysis subsystem.
Thirdly, the scheme can upgrade, remove condensation, remove impurities, decolor and the like, and the color, smell and purity of the primary pyrolysis liquid with more black, smell and impurities are greatly improved after the primary pyrolysis liquid is treated by the subsystem.
Drawings
In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings that are needed in the description of the embodiments or the prior art will be briefly described, and it is obvious that the drawings in the description below are some embodiments of the present invention, and other drawings can be obtained according to the drawings without inventive effort for a person skilled in the art.
FIG. 1 is a flow chart of a system method defined in GB/T32662-2016 complete production equipment for cracking and oiling waste rubber and waste plastics, which is described in the background art of the invention;
fig. 2 is a flow chart of the pyrolysis method of waste plastics according to the present invention.
Description of the reference numerals
01. A feed system; 02. a lysis system; 03. an oil gas cooling system; 04. a non-condensable combustible gas purification system; 05. a discharging system; 06. a flue gas purification system; 07. a circulating water cooling system; 08. an electrical control system;
1. a charging machine; 2. a rotary main pyrolyzer; 3. a secondary pyrolysis device; 4. dewaxing and pour point depressing device; 5. a cooling water tank; 6. a condensing duct; 7. a primary pyrolysis liquid storage tank; 8. a delivery conduit; 9. a rotary purifying reaction kettle; 10. a modifying and molecular shaping device; 11. a modified pyrolysis liquid storage tank; 12. a non-condensable gas delivery conduit; 13. a pyrolysis liquid filtering device; 14. a liquid collecting tank; 15. pyrolysis liquid blending device; 16. a pyrolysis liquid storage tank; 17. a non-condensable gas recycling pipeline; 18. a high-temperature slag discharging device; 19. a high-temperature slag collecting and cooling device; 20. a water cooling tower; 21. a heater group;
A. auxiliary fuel.
Detailed Description
To further clarify the above and other features and advantages of the present invention, a further description of the invention will be rendered by reference to the appended drawings. It should be understood that the specific embodiments presented herein are for purposes of explanation to those skilled in the art and are intended to be illustrative only and not limiting.
In the description of the present specification, a description referring to terms "one embodiment," "some embodiments," "examples," "specific examples," or "some examples," etc., means that a particular feature, structure, material, or characteristic described in connection with the embodiment or example is included in at least one embodiment or example of the present invention. In this specification, schematic representations of the above terms are not necessarily directed to the same embodiment or example. Furthermore, the particular features, structures, materials, or characteristics described may be combined in any suitable manner in any one or more embodiments or examples. Furthermore, the different embodiments or examples described in this specification and the features of the different embodiments or examples may be combined and combined by those skilled in the art without contradiction.
In the following description, numerous specific details are set forth in order to provide a thorough understanding of the present invention. It will be apparent, however, to one skilled in the art that the specific details need not be employed to practice the present invention. In other instances, well-known steps or operations have not been described in detail in order to avoid obscuring the invention.
The invention provides a pyrolysis method of waste plastics, which comprises the steps of firstly pyrolyzing the waste plastics at the temperature of not lower than 400 ℃ to generate mixed pyrolysis gas, then carrying out secondary pyrolysis treatment on the mixed pyrolysis gas to obtain pyrolysis gas, and cooling the pyrolysis gas to obtain pyrolysis liquid.
The pyrolysis temperature can be increased to more than 400 ℃, the pyrolysis temperature is not controlled below 380 ℃, and the generation of pyrolysis liquid with high wax content can be prevented, so that the pyrolysis rate of waste plastics is greatly improved. In addition, the month turnover rate can reach 20-25 cycles through the special designed waste plastic pyrolysis mode of the batch pyrolysis subsystem.
The following describes the embodiments of the present invention in connection with specific examples.
In example 1, as shown in fig. 2, firstly, waste plastics are charged into the charging machine 1 and then pyrolyzed by the rotary main pyrolyzer 2, the pyrolysis temperature can be increased to 400 ℃ (in other examples, the pyrolysis temperature can be increased to 400 ℃ or higher, such as 410 ℃, 430 ℃, 450 ℃, 470 ℃ or the like), and the pyrolysis liquid with high wax content does not need to be controlled below 380 ℃ to prevent generation of the pyrolysis liquid, thereby greatly improving the pyrolysis rate of the waste plastics. The waste rubber pyrolysis intermittent device in the prior art needs about 35 hours for one cycle period, and the waste plastic pyrolysis device in the prior art needs 50 hours for one cycle period, and obviously, the equipment utilization rate of the prior art scheme is too low, and the monthly turnover rate can only be kept between 10 and 12 cycles. The month turnover rate can reach 20-25 cycles through the pyrolysis mode of the specially designed waste plastics of the batch pyrolysis separation system.
The mixed pyrolysis gas enters the secondary pyrolysis device 3, the pyrolysis component with high wax content is pyrolyzed again into a component with very low wax content (the secondary pyrolysis device 3 is filled with a solid catalyst, such as Raschig ring or pall ring), and then enters the dewaxing and pour point depressing device 4, and the residual high wax component is removed. The primary pyrolysis gas treated by the secondary pyrolysis device 3 passes through a cooling water tank 5, a condensing pipeline 6 is arranged in the cooling water tank 5, the primary pyrolysis gas enters the condensing pipeline 6, the primary pyrolysis gas is condensed into primary pyrolysis liquid in the condensing pipeline 6, and then the primary pyrolysis liquid enters a primary pyrolysis liquid storage tank 7.
Secondly, the primary pyrolysis liquid in the primary pyrolysis liquid storage tank 7 continuously enters the rotary purification reaction kettle 9 through the conveying pipeline 8, secondary pyrolysis gas is formed by heating and gasification and then enters the modification and molecular shaping device 10, and two solid catalysts are filled in the device, so that the pyrolysis gas can be modified, coagulated, decontaminated, decolored and the like. The primary pyrolysite with more black, odor and impurity is greatly improved in color, odor and purity after being treated by the subsystem. The pyrolysis gas treated by the modification and molecular shaping device 10 enters the cooling water tank 5 again for cooling, secondary pyrolysis liquid is obtained after cooling, and the secondary pyrolysis liquid enters the modified pyrolysis liquid storage tank 11.
Meanwhile, the non-condensable gas in the primary pyrolysis liquid storage tank 7 is conveyed through a non-condensable gas conveying pipeline 12, one part of the non-condensable gas is heated and reacted by adding auxiliary fuel A to form pyrolysis liquid, the pyrolysis liquid enters the rotary purification reaction kettle, and the other part of the non-condensable gas is heated and reacted by adding auxiliary fuel A to form pyrolysis liquid, and the pyrolysis liquid is circulated into the rotary main pyrolyzer 2.
After pyrolysis is finished, when the temperature in the rotary main pyrolyzer 2 is 340 ℃, the increased high Wen Chuzha device 18 can enable the machinery to slag out quickly, and slag enters the high-temperature slag collecting and cooling device 19.
Finally, the modified pyrolysis liquor is fed into the pyrolysis liquor filtering device 13 from the modified pyrolysis liquor storage tank 11, impurities are further removed from the purified pyrolysis liquor by the molecular sieve filter material in the pyrolysis liquor filtering device 13, the oxidation resistance and deterioration characteristics are improved, filtered pyrolysis liquor filtrate enters the liquid collecting tank 14 and then flows into the pyrolysis liquor blending device 15, and finally three pyrolysis liquor improving agents are added into the pyrolysis liquor, so that the pyrolysis liquor reaches the quality index of the national standard 5 diesel additive.
In example 2
As shown in fig. 2, firstly, waste plastics are charged into the charging machine 1 and then pyrolyzed by the rotary main pyrolyzer 2, the pyrolysis temperature can be increased to 400 ℃ (in other embodiments, the pyrolysis temperature can be increased to 400 ℃ or higher, such as 410 ℃, 430 ℃, 450 ℃, 470 ℃ or the like), and the pyrolysis temperature does not need to be controlled below 380 ℃ to prevent the generation of pyrolysis liquid with high wax content, thereby greatly improving the pyrolysis rate of waste plastics. The waste rubber pyrolysis intermittent device in the prior art needs about 35 hours for one cycle period, and the waste plastic pyrolysis device in the prior art needs 50 hours for one cycle period, and obviously, the equipment utilization rate of the prior art scheme is too low, and the monthly turnover rate can only be kept between 10 and 12 cycles. The month turnover rate can reach 20-25 cycles through the pyrolysis mode of the specially designed waste plastics of the batch pyrolysis separation system.
After pyrolysis is completed, the increased height Wen Chuzha means 18 enables mechanically rapid tapping when the temperature in the rotary main pyrolyzer 2 is 360 ℃ (in other embodiments, the temperature in the rotary main pyrolyzer 2 may be anywhere between 340 ℃ and 360 ℃, such as 350 ℃). The mixed pyrolysis gas enters the secondary pyrolysis device 3, and the pyrolysis component with high wax content is pyrolyzed again into a component with very low wax content (the secondary pyrolysis device 3 is filled with one solid catalyst, in other embodiments, more than one solid catalyst can be used), and then enters the dewaxing and pour point depressing device 4, so that the residual high wax component is removed. The primary pyrolysis gas treated by the secondary pyrolysis device 3 passes through a cooling water tank 5, a condensing pipeline 6 is arranged in the cooling water tank 5, the primary pyrolysis gas enters the condensing pipeline 6, the primary pyrolysis gas is condensed into primary pyrolysis liquid in the condensing pipeline 6, and then the primary pyrolysis liquid enters a primary pyrolysis liquid storage tank 7.
Secondly, the primary pyrolysis liquid in the primary pyrolysis liquid storage tank 7 continuously enters the rotary purification reaction kettle 9 through the conveying pipeline 8, secondary pyrolysis gas is formed by heating and gasification and then enters the modification and molecular shaping device 10, two solid catalysts (in other embodiments, the types of the solid catalysts can be more than two) are filled in the device, and the pyrolysis gas can be modified, dephlegmated, decontaminated, decolored and the like. The primary pyrolysite with more black, odor and impurity is greatly improved in color, odor and purity after being treated by the subsystem. The pyrolysis gas treated by the modification and molecular shaping device 10 enters the cooling water tank 5 again for cooling, secondary pyrolysis liquid is obtained after cooling, and the secondary pyrolysis liquid enters the modified pyrolysis liquid storage tank 11.
The auxiliary fuel a is used for initial heating of the reaction kettle, and is usually fuel oil or diesel oil, and the reaction kettle is heated under the action of the heater group 21. It should be noted that, in this embodiment, the heater group 21 is a group of gas combustion devices, typically 3-4 in each group, for combusting non-condensable gas, instead of initially heating fuel.
After pyrolysis is finished, when the temperature in the rotary main pyrolyzer 2 is 340 ℃, the increased high Wen Chuzha device 18 can enable the machinery to slag out quickly, and slag enters the high-temperature slag collecting and cooling device 19.
Finally, the modified pyrolysis liquor is fed into the pyrolysis liquor filtering device 13 from the modified pyrolysis liquor storage tank 11, impurities are further removed from the purified pyrolysis liquor by the molecular sieve filter material in the pyrolysis liquor filtering device 13, the oxidation resistance and deterioration characteristics are improved, filtered pyrolysis liquor filtrate enters the liquid collecting tank 14 and then flows into the pyrolysis liquor blending device 15, and finally three pyrolysis liquor improving agents are added into the pyrolysis liquor, so that the pyrolysis liquor reaches the quality index of the national standard 5 diesel additive.
While embodiments of the present invention have been shown and described above, it will be understood that the above embodiments are illustrative and not to be construed as limiting the invention, and that variations, modifications, alternatives and variations may be made to the above embodiments by one of ordinary skill in the art within the scope of the invention.
Claims (10)
1. A pyrolysis method for waste plastics is characterized in that waste plastics are first pyrolyzed at the temperature of not lower than 400 ℃ to generate mixed pyrolysis gas, then the mixed pyrolysis gas is subjected to secondary pyrolysis treatment to obtain pyrolysis gas, and pyrolysis liquid is obtained after cooling treatment of the pyrolysis gas.
2. The method for pyrolysis of waste plastics according to claim 1, comprising the steps of:
step a, first pyrolysis treatment: first pyrolyzing waste plastics at a temperature of not lower than 400 ℃ and generating mixed pyrolysis gas;
step b, secondary pyrolysis treatment: carrying out secondary pyrolysis treatment on the mixed pyrolysis gas to obtain primary pyrolysis gas;
step c, cooling treatment: cooling the primary pyrolysis gas to obtain primary pyrolysis liquid;
and d, purifying: and heating and gasifying the primary pyrolysis liquid to form secondary pyrolysis gas, carrying out catalytic reaction on the secondary pyrolysis gas, and cooling to obtain the secondary pyrolysis liquid.
3. The method for pyrolysis of waste plastics according to claim 2, wherein the step a is specifically:
first pyrolyzing waste plastics in a rotary main pyrolyzer at the temperature of not lower than 450 ℃ to generate mixed pyrolysis gas and hot slag;
and when the temperature in the rotary main pyrolyzer is reduced to 340-360 ℃, discharging the hot slag and cooling.
4. The method for pyrolyzing waste plastics according to claim 3, wherein in the step b, the mixed pyrolysis gas is introduced into a secondary pyrolysis device for secondary pyrolysis treatment, and then introduced into a dewaxing and pour point depressing device for dewaxing treatment, so as to obtain the primary pyrolysis gas.
5. The method for pyrolysis of waste plastics according to claim 4 wherein step c is characterized in that the primary pyrolysis gas is introduced into a cooling tank with a condensing pipe, and the primary pyrolysis gas is condensed in the condensing pipe to obtain a primary pyrolysis liquid.
6. The method of pyrolysis of waste plastics according to claim 5, wherein step d is specifically that the primary pyrolysis liquid is introduced into a rotary purification reaction device, secondary pyrolysis gas is obtained after heating and gasification, the secondary pyrolysis gas is introduced into a modification and molecular shaping device for catalytic reaction, and the secondary pyrolysis gas after catalytic reaction is cooled to obtain secondary pyrolysis liquid.
7. The method of pyrolysis of waste plastics according to claim 5, wherein step d further comprises: and introducing the secondary pyrolysis liquid into a pyrolysis liquid filtering device, filtering, and mixing with at least three pyrolysis liquid enhancers to obtain mixed pyrolysis liquid.
8. The method of pyrolysis of waste plastics according to claim 4 wherein the secondary pyrolysis unit is filled with at least one catalyst.
9. The method of pyrolysis of waste plastics according to claim 6 wherein the modifying and molecular shaping means is filled with at least two catalysts.
10. The method for pyrolysis of waste plastics according to claim 8 or 9, characterized in that the catalyst is a solid catalyst.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202311006209.4A CN117025248A (en) | 2023-08-10 | 2023-08-10 | Pyrolysis method for waste plastics |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202311006209.4A CN117025248A (en) | 2023-08-10 | 2023-08-10 | Pyrolysis method for waste plastics |
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| Publication Number | Publication Date |
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| CN117025248A true CN117025248A (en) | 2023-11-10 |
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|---|---|---|---|
| CN202311006209.4A Pending CN117025248A (en) | 2023-08-10 | 2023-08-10 | Pyrolysis method for waste plastics |
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- 2023-08-10 CN CN202311006209.4A patent/CN117025248A/en active Pending
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