CN111621315A - Pyrolysis process system for recycling waste plastics - Google Patents
Pyrolysis process system for recycling waste plastics Download PDFInfo
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- CN111621315A CN111621315A CN202010477366.3A CN202010477366A CN111621315A CN 111621315 A CN111621315 A CN 111621315A CN 202010477366 A CN202010477366 A CN 202010477366A CN 111621315 A CN111621315 A CN 111621315A
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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
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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
- C10B47/00—Destructive distillation of solid carbonaceous materials with indirect heating, e.g. by external combustion
- C10B47/18—Destructive distillation of solid carbonaceous materials with indirect heating, e.g. by external combustion with moving charge
- C10B47/22—Destructive distillation of solid carbonaceous materials with indirect heating, e.g. by external combustion with moving charge in dispersed form
- C10B47/24—Destructive distillation of solid carbonaceous materials with indirect heating, e.g. by external combustion with moving charge in dispersed form according to the "fluidised bed" technique
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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
- C10B57/00—Other carbonising or coking processes; Features of destructive distillation processes in general
- C10B57/18—Modifying the properties of the distillation gases in the oven
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- 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
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- 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
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- 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
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- 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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Abstract
The invention discloses a pyrolysis process system for recycling waste plastics resources, which comprises a feeding unit, a pyrolysis unit, a fuel gas recycling unit and a heat supply unit, wherein the feeding unit is used for pretreating and feeding waste plastics; the pyrolysis unit is used for carrying out pyrolysis treatment on the waste plastics conveyed by the feeding unit; the pyrolysis unit comprises a fluidized bed cracking furnace, a circulating cyclone dust collector, a high-temperature circulating fan, a high-temperature heat exchanger and a catalytic reforming reactor, wherein the fluidized bed cracking furnace comprises an inner-layer pyrolysis part and an outer-layer heating jacket; the fuel gas recycling unit is used for recycling fuel gas generated after the catalytic reforming reactor; the heat supply unit is used for recycling the fuel gas recycled by the fuel gas recycling unit and providing heat required by reaction for the heating jacket and the catalytic reforming reactor. The pyrolysis process system adopts the fluidized bed to indirectly heat the anaerobic pyrolysis process, oxygen does not participate in the pyrolysis process, and pollutants such as dioxin and the like are not generated.
Description
Technical Field
The invention relates to the technical field of plastic treatment, in particular to a pyrolysis process system for recycling waste plastics.
Background
The plastic has the advantages of light weight, low cost, convenient use, corrosion resistance and the like, and is widely applied to the fields of packaging, agriculture, light industry, automobiles and the like. However, the plastic is easy to age and break, the service cycle is short, the natural decomposition cycle is long, and the wide application of the plastic brings convenience to our lives, and simultaneously, a large amount of waste plastics are generated, and serious pollution is caused to the environment and the ecological system. Therefore, the recycling of waste plastics has very important practical significance.
At present, the treatment method of waste plastics mainly comprises landfill, mechanical recycling, incineration and pyrolysis. The waste plastic landfill occupies large land area, the waste plastic is difficult to degrade, and the waste plastic exists for a long time in the landfill process, and causes secondary pollution to soil and water. The mechanical recycling of waste plastics mainly adopts a physical method to recycle the waste plastics so as to reduce the waste plastics into similar plastic products, but the waste plastics have complex components, high mechanical recycling cost and low benefit, and simultaneously, the mechanical recycling easily causes secondary pollution. In the incineration technology of waste plastics, the reduction of the waste plastics through incineration is very obvious, and part of heat energy can be recycled, but the incineration can cause very serious environmental pollution, generate harmful substances such as dioxin, acid gas, fly ash and the like, and simultaneously cause corrosion damage to related equipment. Pyrolysis refers to the thermal decomposition of waste plastics into small molecular compounds including pyrolysis oil, pyrolysis gas and carbon powder under the condition of no oxygen or oxygen deficiency; compared with direct incineration, the pyrolysis technology has the advantages of small environmental pollution, resource utilization of pyrolysis products, and is the most potential waste plastic pyrolysis treatment method in the future.
At present, the pyrolysis industrial treatment of waste plastics is not fully mature, and the common problems are as follows: the tar content of the pyrolysis product is high, the pipeline of equipment is blocked, the normal operation is influenced, and the subsequent use of the product is influenced; the content of hydrogen chloride in the pyrolysis gas is high, equipment is corroded, and the environment is polluted; pyrolysis oil has complex and unstable components, which makes commercial application difficult; and the method also has the defects of low energy utilization rate, low pyrolysis efficiency, more oil content in pyrolysis wastewater, difficult treatment and the like.
Disclosure of Invention
In order to overcome the defects of the prior art, the invention provides a pyrolysis process system for recycling waste plastics, which solves the traditional problems, adopts an indirect heating anaerobic pyrolysis technology to pyrolyze and gasify the waste plastics into combustible gas, and simultaneously is matched with technologies such as tar high-temperature catalytic reforming, fuel gas deacidification purification, waste water purification and the like to convert the waste plastics into clean combustible gas so as to achieve the purpose of recycling the waste plastics, and simultaneously, the whole process does not generate environmental pollution problems such as dioxin, hydrogen chloride and the like.
The invention is realized by adopting the following technical scheme:
a pyrolysis process system for recycling waste plastics comprises:
the feeding unit is used for pretreating and feeding waste plastics;
the pyrolysis unit is used for carrying out pyrolysis treatment on the waste plastics conveyed by the feeding unit; the pyrolysis unit comprises a fluidized bed cracking furnace, a circulating cyclone dust collector, a high-temperature circulating fan, a high-temperature heat exchanger and a catalytic reforming reactor, the fluidized bed cracking furnace comprises an inner-layer pyrolysis part and an outer-layer heating jacket, and the pyrolysis part, the circulating cyclone dust collector, the high-temperature circulating fan, the high-temperature heat exchanger and the catalytic reforming reactor are sequentially connected to form a circulating fluidized cracking system;
the fuel gas recycling unit is used for recycling the fuel gas generated after the catalytic reforming reactor; and
and the heat supply unit is used for recycling the fuel gas recycled by the fuel gas recycling unit to provide heat required by the reaction for the heating jacket and the catalytic reforming reactor.
Preferably, the cracking temperature of the fluidized bed cracking furnace is 500-700 ℃.
Preferably, the temperature of the catalytic reforming reactor is between 700 ℃ and 1000 ℃.
Preferably, the feeding unit comprises a pretreatment assembly and a feeding assembly, wherein the pretreatment assembly comprises a first belt conveyor, a crusher, a second belt conveyor and a storage bin which are sequentially connected; the feeding assembly comprises a quantitative belt conveyor, a bucket elevator, a primary sealing screw, a secondary sealing screw and a feeding screw which are connected with the storage bin, and the feeding screw is used for being connected with the pyrolysis unit.
Preferably, the fuel gas recycling unit comprises a fuel gas purifying and cooling unit, a fuel gas conveying and storing unit, a fuel gas recycling unit and a wastewater treatment unit, the fuel gas purifying and cooling unit comprises a fuel gas cyclone dust collector, a waste heat boiler, a water-cooling heat exchanger, a primary deacidification tower, a secondary deacidification tower and a steam-water separator which are sequentially connected, the fuel gas cyclone dust collector is used for being connected with a fuel gas outlet of the catalytic reforming reactor, an air outlet pipe of the steam-water separator is connected with the fuel gas conveying and storing unit, and a liquid outlet of the steam-water separator is connected with the wastewater treatment unit; the gas recycling unit is connected with the gas conveying and storing unit.
Preferably, the gas conveying and storing unit comprises a gas induced draft fan, a gas holder and a torch, and the gas holder is respectively connected with the heat supply unit and the gas recycling unit.
Preferably, the gas recycling unit is a gas generator unit or a gas boiler driving a steam turbine generator set.
Preferably, the heat supply unit comprises a hot blast stove, a combustion fan and a gas fan, and the gas fan is used for sequentially conveying flue gas generated by the hot blast stove into the catalytic reforming reactor and the fluidized bed cracking furnace to provide energy for pyrolysis and catalytic reforming.
Preferably, the temperature of the burned flue gas in the hot blast stove is controlled to be 700-1000 ℃.
Preferably, the pyrolysis process system still includes gas cleaning unit and lime-ash collection unit, the gas cleaning unit is including quench tower, sack cleaner flue gas, draught fan and the chimney that connects gradually, the quench tower with heating jacket connects, the lime-ash collection unit includes that the pyrolysis furnace arranges sediment water-cooling spiral, cyclone arranges sediment water-cooling spiral, sack cleaner arranges grey spiral and lime-ash collecting box.
Compared with the prior art, the invention has the beneficial effects that:
(1) the pyrolysis process system adopts the fluidized bed to indirectly heat the anaerobic pyrolysis process, oxygen does not participate in the pyrolysis process, and pollutants such as dioxin and the like are not generated.
(2) The invention utilizes the raw material pyrolysis gas as the fluidizing medium for self-circulation fluidization, and heats the circulating pyrolysis gas through the high-temperature heat exchanger, thereby increasing the heat exchange efficiency and improving the pyrolysis efficiency.
(3) The invention integrates the technologies of high-temperature catalytic reforming and cracking tar, wet deacidification for removing hydrogen chloride, efficient air floatation for removing oil from sewage and the like, solves the difficult problem of waste plastic pyrolysis, and makes the whole treatment system more perfect.
(4) The main product of the traditional waste plastic pyrolysis process is an oil product, but the waste plastic pyrolysis oil has complex and unstable properties, does not have related standards, and needs to be disposed according to a dangerous waste mode. The waste plastic is catalytically cracked at high temperature, and the pyrolysis product is mainly clean micromolecular combustible gas, so that the method is more environment-friendly to use.
Drawings
FIG. 1 is a schematic structural view of a pyrolysis process system for resource recycling of waste plastics according to the present invention;
FIG. 2 is a schematic structural diagram of the feeding unit shown in FIG. 1;
FIG. 3 is a schematic diagram of the gas purification and cooling unit shown in FIG. 1;
FIG. 4 is a process flow diagram of example 1 of the present invention.
In the figure: 10. a feeding unit; 11. a pre-processing assembly; 12. a feed assembly; 111. a first belt conveyor; 112. a crusher; 113. a second belt conveyor; 114. a storage bin; 121. a quantitative belt conveyor; 122. a bucket elevator; 123. primary sealing spiral; 124. secondary sealing spiral; 125. a feed screw; 20. a pyrolysis unit; 21. a fluidized bed cracking furnace; 22. a circulating cyclone dust collector; 23. a high temperature circulating fan; 24. a high temperature heat exchanger; 25. a catalytic reforming reactor; 30. a gas recycling unit; 31. a gas purification and cooling unit; 310. a gas cyclone dust collector; 311. a waste heat boiler; 312. a water-cooled heat exchanger; 313. a first-stage deacidification tower; 314. a secondary deacidification tower; 315. a steam-water separator; 32. a gas delivery and storage unit; 33. a gas reuse unit; 34. a wastewater treatment unit; 40. a heat supply unit; 50. a flue gas purification unit; 60. an ash collection unit.
Detailed Description
The invention will be further described with reference to the accompanying drawings and the detailed description below:
referring to fig. 1, a pyrolysis process system for recycling waste plastics resources according to a preferred embodiment of the present invention is used for pyrolyzing waste plastics by using an indirect heating anaerobic pyrolysis technology to pyrolyze and gasify the waste plastics into combustible gas, and the pyrolysis process system includes a feeding unit 10, a pyrolysis unit 20, a gas recycling unit 30, a heat supply unit 40, a flue gas purification unit 50, and an ash collection unit 60.
The invention adopts the indirect heating anaerobic pyrolysis technology to pyrolyze and gasify the waste plastics into combustible gas, and simultaneously combines the technologies of tar high-temperature catalytic reforming, fuel gas deacidification purification, waste water purification and the like to convert the waste plastics into clean combustible gas, thereby achieving the purpose of recycling the waste plastics, and simultaneously avoiding the environmental pollution problems of dioxin, hydrogen chloride and the like in the whole process.
Specifically, the feeding unit 10 is used for pretreating and feeding the waste plastics to ensure that the waste plastics are quantitatively and stably fed into the pyrolysis unit 20 after being uniformly crushed; as shown in fig. 2, the feeding unit 10 includes a pretreatment module 11 and a feeding module 12, the pretreatment module 11 includes a first belt conveyor 111, a crusher 112, a second belt conveyor 113 and a storage bin 114 connected in sequence, and waste plastics are crushed and then buffered in the storage bin 114; feeding component 12 is including the quantitative band conveyer 121 of connecting feed bin 114, bucket elevator 122, one-level sealed spiral 123, sealed spiral 124 of second grade and feeding spiral 125, install the belt weigher on the quantitative band conveyer 121, be used for measuring and controlling the plastics of feed bin 114 output, feeding spiral 125 is used for being connected with pyrolysis unit 20, feeding component 12 adopts the sealed spiral of doublestage, extrude the material into blockily, prevent that the air from pressing from both sides in the material, get into pyrolysis unit 20, play better sealed effect, adopt feeding spiral 125 again, break up blocky material, it is more even to make it get into pyrolysis unit 20, be convenient for subsequent pyrolysis.
Referring to fig. 1 again, the pyrolysis unit 20 is used for pyrolyzing the waste plastics conveyed by the feeding unit 10, the pyrolysis unit 20 includes a fluidized bed cracking furnace 21, a circulating cyclone 22, a high-temperature circulating fan 23, a high-temperature heat exchanger 24 and a catalytic reforming reactor 25, the fluidized bed cracking furnace 21 includes an inner pyrolysis part and an outer heating jacket, the pyrolysis part of the fluidized bed cracking furnace 21, the circulating cyclone 22, the high-temperature circulating fan 23, the high-temperature heat exchanger 24 and the catalytic reforming reactor 25 are sequentially connected to form a circulating fluidized cracking system, specifically, a top feeding pipeline, a top pyrolysis gas output pipeline, a bottom fluidized medium input pipeline and a bottom ash collecting pipeline are arranged on the pyrolysis part, the feeding pipeline is connected with the feeding screw 125 of the feeding unit 10, the pyrolysis gas output pipeline is connected with the circulating cyclone 22, the fluidized medium input pipe is connected with the catalytic reforming reactor 25, and the ash collecting pipe is used for being connected with the ash collecting unit 60; the heating jacket is provided with a top flue gas output pipeline and a bottom high-temperature flue gas input pipeline, the flue gas output pipeline is used for being connected with the flue gas purification unit 50, and the high-temperature flue gas input pipeline is used for being connected with the heat supply unit 40.
The fluidized bed cracking furnace 21 adopts a fluidized bed cracking mode, high-temperature flue gas is used for heating the heating jacket, the cracking temperature is 500-. The circulation flow of the pyrolysis fuel gas generated by pyrolysis is as follows: the fuel gas generated by pyrolysis is led out from a pyrolysis gas output pipeline at the top of the fluidized bed cracking furnace 21, passes through a circulating cyclone dust collector 22 and is sent into a high-temperature heat exchanger 24 by a circulating fan, the fuel gas enters a high-temperature catalytic reforming reactor 25 after heat exchange, the temperature of the catalytic reforming reactor 25 is 700-1000 ℃, tar in the fuel gas is removed by high-temperature catalytic cracking, a part of reformed fuel gas enters the fluidized bed cracking furnace 21 and is self-circulated as a fluidizing medium, and the rest of the fuel gas enters a fuel gas recycling unit 30 for recycling.
In one embodiment, the high-temperature heat exchanger 24 includes a heat exchange layer and a heating interlayer, the pyrolysis gas is connected to the heat exchange layer, and the heating interlayer is connected to the heat supply unit, that is, the high-temperature flue gas passes through the high-temperature heat exchanger 24 and then heats the heating jacket of the fluidized bed cracking furnace 21, wherein the high-temperature heat exchanger 24 is one of a fixed tube plate heat exchanger, a U-shaped tube plate heat exchanger, and a plate heat exchanger, and preferably, the high-temperature heat exchanger 24 is a U-shaped tube plate heat exchanger.
Alternatively, the catalyst employed in the catalytic reforming reactor 25 is, but is not limited to, a platinum-rhenium bimetallic catalyst, a metal oxide catalyst, an iridium-platinum bimetallic catalyst, or a platinum-tin bimetallic catalyst.
The fuel gas recycling unit 30 is used for recycling the fuel gas generated after the catalytic reforming reactor 25, and the fuel gas recycling unit 30 includes a fuel gas purifying and cooling unit 31, a fuel gas transportation and storage unit 32, a fuel gas recycling unit 33, and a wastewater treatment unit 34.
As shown in fig. 3, the gas purifying and cooling unit 31 includes a gas cyclone 310, a waste heat boiler 311, a water-cooled heat exchanger 312, a first-stage deacidification tower 313, a second-stage deacidification tower 314, and a steam-water separator 315, which are connected in sequence. The gas cyclone 310 is used for being connected with a gas outlet of the catalytic reforming reactor 25 of the pyrolysis unit 20, a liquid outlet of the steam-water separator 315 is connected with the wastewater treatment unit 34, and a gas outlet pipe of the steam-water separator 315 is connected with the gas conveying and storing unit 32. In one embodiment, the steam-water separator 315 is, but not limited to, a vertical cylindrical steam-water separator 315 or a spherical steam-water separator 315, and the dryness of the gas obtained by the two separators can reach more than 90%. The working principle is as follows: the temperature of the fuel gas from the pyrolysis unit 20 is 700-.
The gas delivery and storage unit 32 is used for storing clean and dry combustible gas obtained by the gas purification and cooling unit 31 and delivering the gas to the heat supply unit and the gas recycling unit 33, the gas delivery and storage unit 32 comprises a gas induced draft fan, a gas holder and a torch, the gas induced draft fan is used for being connected with a gas outlet of a steam-water separator 315 of the gas purification and cooling unit 31 and sucking the gas from the steam-water separator 315 into the gas holder for storage, the gas holder is respectively connected with the heat supply unit and the gas recycling unit 33 and delivers and buffers the gas, and the torch is used under emergency evacuation to prevent environmental pollution.
The gas recycling unit 33 supplies the gas to the heat supply unit for utilization, and then the remaining gas is recycled, in this embodiment, the gas recycling unit 33 is but not limited to a gas generator unit or a gas boiler to drive a steam turbine generator set, a part of the gas generated by plastic pyrolysis is used for self-pyrolysis reaction heat supply, and the surplus gas is used for power generation of the gas generator, so that value is generated, and resource recycling of waste plastics is realized.
The wastewater treatment unit 34 comprises a wastewater buffer tank, an oil-water separator and a wastewater treatment air floatation device, wastewater generated by fuel gas in the fuel gas purification cooling unit 31 mainly comes from condensed wastewater of the water-cooling heat exchanger 312, wastewater generated by the primary deacidification tower 313 and the secondary deacidification tower 314 and wastewater separated by the steam-water separator 315, and the wastewater is treated by the wastewater treatment unit 34, so that the treated wastewater can reach the wastewater discharge standard and is discharged outside.
The heat supply unit 40 is used for supplying heat required by the reaction to the fluidized bed cracking furnace 21 and the catalytic reforming reactor 25 of the pyrolysis unit 20 by using the fuel gas recovered by the fuel gas recycling unit 30, the heat supply unit 40 comprises a hot blast stove, a combustion-supporting fan and a fuel gas fan, the fuel used by the combustion of the hot blast stove is the fuel gas purified by the fuel gas recycling unit 30, the fuel gas generated by the self pyrolysis of the waste plastics is used for providing energy for the pyrolysis of the waste plastics, and the energy is saved and the emission is reduced. The gas fan is used for conveying the flue gas generated by the hot blast stove to the catalytic reforming reactor 25 and the fluidized bed cracking furnace 21 in sequence, and providing energy for the pyrolysis and catalytic reforming of the units. In one embodiment, the temperature of the burned flue gas in the hot blast stove is controlled to be 700-1000 ℃.
The flue gas purification unit 50 is used for treating flue gas in the heating jacket of the fluidized bed cracking furnace 21, and the flue gas purification unit 50 comprises a quench tower, a bag-type dust remover, a flue gas induced draft fan and a chimney which are connected in sequence, wherein the flue gas induced draft fan is connected with the heating jacket, the working principle of the flue gas induced draft fan is that the flue gas is cooled by the quench tower and then is dedusted by the bag-type dust remover, and after the environmental protection reaches the standard, the flue gas induced draft fan is finally conveyed.
The ash collecting unit 60 is used for collecting powder slag in the fluidized bed cracking furnace 21, the cyclone dust collector, the bag-type dust collector and other equipment in a centralized manner to avoid dust raising, the ash collecting unit 60 comprises a cracking furnace slag discharging water-cooling spiral, a cyclone dust collector slag discharging water-cooling spiral, a bag-type dust collector ash discharging spiral and an ash collecting box, the cracking furnace slag discharging water-cooling spiral is connected with the pyrolysis part of the fluidized bed cracking furnace 21, the cyclone dust collector slag discharging water-cooling spiral is connected with the circulating cyclone dust collector 22, and the ash collecting box is respectively connected with the cracking furnace slag discharging water-cooling spiral, the cyclone dust collector slag discharging water-cooling spiral, the bag-type dust collector ash discharging spiral and.
Description of connection relationship of each unit: the feeding unit 10 is connected with a cracking furnace material inlet of a fluidized bed cracking furnace 21 and provides raw materials for the pyrolysis unit 20; the heat supply unit 40 is connected with the flue gas inlet of the high-temperature heat exchanger 24, and the high-temperature heat exchanger 24 is connected with the fluidized bed cracking furnace 21 to provide reaction energy for the pyrolysis unit 20; the ash residue collecting unit 60 is connected with the flue gas outlet of the fluidized bed cracking furnace 21, and the treated flue gas reaches the discharge standard; the ash collecting system is connected with an ash outlet of the fluidized bed cracking furnace 21, comprises a slag outlet of the fluidized bed cracking furnace 21 and a slag outlet of the circulating cyclone dust collector 22, and collects a solid product generated after the waste plastic is pyrolyzed, mainly pyrolytic carbon powder; the gas purification and cooling unit 31 is connected with the outlet of the catalytic reforming reactor 25, and is used for cooling, purifying and pyrolyzing the generated combustible gas, and removing harmful gas substances such as hydrogen chloride and the like in the combustible gas; the waste water treatment unit 34 is connected with a waste water outlet of the gas purification cooling unit 31, and the treated waste water reaches the discharge standard; the gas purifying and cooling unit 31 is connected with the gas conveying and storing unit 32; and finally, the fuel gas enters a fuel gas recycling unit 33, so that waste plastic pyrolysis resource utilization is realized.
Example 1
The waste plastics are waste plastics produced by paper mills.
As shown in fig. 4, waste plastics are conveyed to a crusher 112 by a first belt conveyor 111, and are conveyed to a bin 114 for buffering by a second belt conveyor 113 after being crushed, and materials in the bin 114 are conveyed to a bucket elevator 122 by a quantitative belt conveyor 121, are lifted to enter a first-stage sealing screw 123, then enter a second-stage sealing screw 124, are conveyed to a feeding screw 125, and finally are conveyed to a pyrolysis part of a fluidized bed cracking furnace 21 by the feeding screw 125.
The material enters the pyrolysis part, and simultaneously the high-temperature flue gas enters a heating jacket of the fluidized bed cracking furnace 21 to indirectly heat the material, the gas product fuel gas generated after the material pyrolysis is led out from the top of the pyrolysis part (the fuel gas temperature is 550-. A part of the fuel gas after catalytic reforming enters the fluidized bed cracking furnace 21 for self-circulation as a fluidizing medium, and the rest of the fuel gas enters the fuel gas purifying and cooling unit 31, namely the finally generated fuel gas. The high-temperature flue gas comes from the hot blast stove of the heat supply unit 40, the fuel of the hot blast stove is clean fuel gas in the gas holder, the fuel gas is combusted to generate flue gas, the temperature is 700-.
The finally generated fuel gas after catalytic reforming enters the fuel gas cyclone dust collector 310 of the fuel gas purification and cooling unit 31 for dust removal, and then enters the waste heat boiler 311 for temperature reduction, wherein the temperature of the fuel gas is reduced from 750-plus-800 ℃ to 150-plus-250 ℃, and steam is generated for heat recovery. The cooled fuel gas enters a water-cooled heat exchanger 312 to be further cooled to 50-60 ℃, a large amount of condensed water is generated, the condensed water enters a sewage buffer tank, the fuel gas enters a primary deacidification tower 313 to remove a large amount of residual tar and carbon powder of acidic gas hydrogen chloride, the primary deacidification tower enters a secondary deacidification tower 314 to ensure that impurities such as acidic harmful gas in the fuel gas are completely removed, then the fuel gas enters a steam-water separator 315 to remove moisture, and the clean and dry fuel gas is sent to a gas cabinet by a fuel gas induced draft fan of a fuel gas conveying and storing unit 32.
The gas in the gas holder is conveyed to the hot blast stove of the heat supply unit 40 for combustion all the way to provide energy for the pyrolysis reaction, and the gas is conveyed to the gas generator unit of the gas recycling unit 33 all the way for power generation to generate electric energy, thereby realizing resource recycling. Meanwhile, the gas burner is provided with a torch, so that when the gas needs to be discharged emergently, the gas can be discharged through the torch in a burning way, and the environment pollution caused by the gas is prevented.
The wastewater condensed by the water-cooled heat exchanger 312, the wastewater generated by the deacidification tower and the wastewater separated by the steam-water separator 315 are collected to a wastewater buffer tank of the wastewater treatment unit 34, and then are conveyed to an oil-water separator, and after oil stains in the water are separated, the water enters a wastewater air floatation treatment device, and the wastewater is discharged after reaching the standard after being treated.
The above embodiments are only preferred embodiments of the present invention, and the protection scope of the present invention is not limited thereby, and any insubstantial changes and substitutions made by those skilled in the art based on the present invention are within the protection scope of the present invention.
Various other modifications and changes may be made by those skilled in the art based on the above-described technical solutions and concepts, and all such modifications and changes should fall within the scope of the claims of the present invention.
Claims (10)
1. A pyrolysis process system for recycling waste plastics resources is characterized by comprising:
the feeding unit is used for pretreating and feeding waste plastics;
the pyrolysis unit is used for carrying out pyrolysis treatment on the waste plastics conveyed by the feeding unit; the pyrolysis unit comprises a fluidized bed cracking furnace, a circulating cyclone dust collector, a high-temperature circulating fan, a high-temperature heat exchanger and a catalytic reforming reactor, the fluidized bed cracking furnace comprises an inner-layer pyrolysis part and an outer-layer heating jacket, and the pyrolysis part, the circulating cyclone dust collector, the high-temperature circulating fan, the high-temperature heat exchanger and the catalytic reforming reactor are sequentially connected to form a circulating fluidized cracking system;
the fuel gas recycling unit is used for recycling the fuel gas generated after the catalytic reforming reactor; and
and the heat supply unit is used for recycling the fuel gas recycled by the fuel gas recycling unit to provide heat required by the reaction for the heating jacket and the catalytic reforming reactor.
2. A pyrolysis process system for recycling waste plastics as resources according to claim 1, wherein the cracking temperature of the fluidized bed cracking furnace is 500 ℃ to 700 ℃.
3. A pyrolysis process system for resource recycling of waste plastics according to claim 1, wherein the temperature of the catalytic reforming reactor is 700 ℃ to 1000 ℃.
4. The waste plastic resource recycling pyrolysis process system as claimed in claim 1, wherein the feeding unit comprises a pretreatment assembly and a feeding assembly, the pretreatment assembly comprises a first belt conveyor, a crusher, a second belt conveyor and a bin which are connected in sequence; the feeding assembly comprises a quantitative belt conveyor, a bucket elevator, a primary sealing screw, a secondary sealing screw and a feeding screw which are connected with the storage bin, and the feeding screw is used for being connected with the pyrolysis unit.
5. The waste plastic resource recycling pyrolysis process system as claimed in claim 1, wherein the gas recycling unit comprises a gas purification cooling unit, a gas transportation storage unit, a gas recycling unit and a wastewater treatment unit, the gas purification cooling unit comprises a gas cyclone, a waste heat boiler, a water-cooled heat exchanger, a primary deacidification tower, a secondary deacidification tower and a steam-water separator which are connected in sequence, the gas cyclone is used for being connected with a gas outlet of the catalytic reforming reactor, an air outlet pipe of the steam-water separator is connected with the gas transportation storage unit, and a liquid outlet of the steam-water separator is connected with the wastewater treatment unit; the gas recycling unit is connected with the gas conveying and storing unit.
6. A pyrolysis process system for recycling waste plastic resources according to claim 5, wherein the gas conveying and storing unit comprises a gas induced draft fan, a gas holder and a torch, and the gas holder is respectively connected with the heat supply unit and the gas recycling unit.
7. A pyrolysis process system for recycling waste plastics as resources according to claim 5, wherein the gas recycling unit is a gas generator unit or a gas boiler driven steam turbine generator set.
8. A pyrolysis process system for recycling waste plastics as resources according to claim 1, wherein the heat supply unit comprises a hot-blast stove, a combustion fan and a gas fan, and the gas fan is used for sequentially conveying flue gas generated by the hot-blast stove into the catalytic reforming reactor and the fluidized bed cracking furnace to provide energy for pyrolysis and catalytic reforming.
9. A pyrolysis process system for recycling waste plastics as resources according to claim 8, wherein the burned flue gas temperature in the hot blast stove is controlled to 700-1000 ℃.
10. The waste plastic resource recycling pyrolysis process system as claimed in claim 1, further comprising a flue gas purification unit and an ash collection unit, wherein the flue gas purification unit comprises a quench tower, a bag-type dust remover flue gas, an induced draft fan and a chimney which are connected in sequence, the quench tower is connected with the heating jacket, and the ash collection unit comprises a cracking furnace slag-discharging water-cooling spiral, a cyclone dust remover slag-discharging water-cooling spiral, a bag-type dust remover ash-discharging spiral and an ash collection box.
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| CN112246832A (en) * | 2020-09-28 | 2021-01-22 | 威尔能环保科技(苏州)有限公司 | Battery material processing system |
| CN113122300A (en) * | 2021-04-23 | 2021-07-16 | 渭沣洁净技术(上海)有限公司 | Process method and device for preparing oil by pyrolyzing high-molecular polymerization waste |
| CN114131786A (en) * | 2021-10-29 | 2022-03-04 | 深圳万宏业科技有限公司 | Recovery and extraction system for waste composite material |
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| CN115108546A (en) * | 2022-04-27 | 2022-09-27 | 东南大学 | System and method for continuously preparing carbon material co-hydrogen from organic solid waste high polymer |
| CN115926848A (en) * | 2021-11-29 | 2023-04-07 | 北京工商大学 | Resource treatment device and treatment method for waste wind power blades |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN112246832A (en) * | 2020-09-28 | 2021-01-22 | 威尔能环保科技(苏州)有限公司 | Battery material processing system |
| CN114811591A (en) * | 2021-01-29 | 2022-07-29 | 上海市机电设计研究院有限公司 | Hazardous waste salt pyrolysis system and pyrolysis process thereof |
| CN113122300A (en) * | 2021-04-23 | 2021-07-16 | 渭沣洁净技术(上海)有限公司 | Process method and device for preparing oil by pyrolyzing high-molecular polymerization waste |
| CN114131786A (en) * | 2021-10-29 | 2022-03-04 | 深圳万宏业科技有限公司 | Recovery and extraction system for waste composite material |
| CN115926848A (en) * | 2021-11-29 | 2023-04-07 | 北京工商大学 | Resource treatment device and treatment method for waste wind power blades |
| CN115926848B (en) * | 2021-11-29 | 2024-02-13 | 北京工商大学 | Recycling treatment device and treatment method for waste wind power blades |
| CN115108546A (en) * | 2022-04-27 | 2022-09-27 | 东南大学 | System and method for continuously preparing carbon material co-hydrogen from organic solid waste high polymer |
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