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WO2006012800A1 - Appareil de fabrication d’huile à partir de déchets plastiques dans la production industrielle en continu - Google Patents

Appareil de fabrication d’huile à partir de déchets plastiques dans la production industrielle en continu Download PDF

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Publication number
WO2006012800A1
WO2006012800A1 PCT/CN2005/001195 CN2005001195W WO2006012800A1 WO 2006012800 A1 WO2006012800 A1 WO 2006012800A1 CN 2005001195 W CN2005001195 W CN 2005001195W WO 2006012800 A1 WO2006012800 A1 WO 2006012800A1
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WO
WIPO (PCT)
Prior art keywords
oil
disposed
dust removal
outlet
water
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Ceased
Application number
PCT/CN2005/001195
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English (en)
Chinese (zh)
Inventor
Hao Jiang
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Individual
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Individual
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Filing date
Publication date
Application filed by Individual filed Critical Individual
Publication of WO2006012800A1 publication Critical patent/WO2006012800A1/fr
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

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Classifications

    • 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
    • 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
    • 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
    • C10G9/00—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
    • 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
    • C10G9/00—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
    • C10G9/005—Coking (in order to produce liquid products mainly)
    • 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

Definitions

  • Waste plastic oiling device capable of continuous industrial mass production
  • the present invention relates to a waste plastic oiling apparatus which can continuously produce industrially produced gasoline fractions, diesel fractions or high quality fuel oils and civil liquefied gases by catalytic or non-catalytic cracking using waste plastics or waste lubricating oils or heavy oils.
  • the second high-temperature slagging equipment How to design a safe slagging equipment to discharge the suspended silt impurities generated during the melting and the coke generated by the reaction in the cracking reaction process, and also form the continuous production. Necessary conditions.
  • the third reaction heating problem how to design a non-open flame heating reaction heating furnace, which can meet the requirements of improving flame temperature and radiation intensity, provide sufficient reaction heat, and must obey the flammable and explosive pressure vessel to prohibit open flame. Heating design specification requirements.
  • the sixth design has equipment to ensure safe production measures. This mainly refers to how to ensure the high temperature continuous feeding and slagging in the process of flammable and explosive high temperature reaction, such as feeding back gas protection, slagging fire prevention and Extinguish, container overpressure protection, eliminate tempering, etc., hardware equipment and measures.
  • Japan Fuji Recycling Company and POKODA Group Corporation Energy Materials Recycling Department are researching and developing waste plastic oiling technology.
  • the first feature is that waste plastics are subject to careful sorting, washing and drying, extrusion molding, etc., and the processing steps are very complicated. It is huge; another feature is that melting and cracking are carried out separately, but the problem of solidification of molten plastic in the pump body and in the pipeline is not solved.
  • Other companies are also vigorously conducting research and development, but they have not been able to form industrial-scale production facilities.
  • an object of the present invention is to provide a waste plastic oiling apparatus which can be continuously industrially produced.
  • a waste plastic oiling device capable of continuous industrial production comprising: a reaction kettle, a feeding device connected to the reaction vessel, and a heating device for reacting the reaction vessel a defocusing device disposed at the bottom of the reaction vessel, followed by a fractionation-strip-condensation cooling device, an oil-gas separation-gas absorption device, an oil extraction and refining device, and an oil-gas separation-gas after the reactor a liquefied gas recovery device drawn from the absorption device; characterized in that: it further comprises a three-waste treatment device having a flue gas dedusting and dust removal device and an oil-water separation device, wherein the flue gas de-blackening and dust removal device is connected to the flue gas of the reaction vessel heating device An oil-water separation device connected to the oil extraction and refining device; the feeding device includes a two-stage feeding device surrounded by a heating device, and the heating device of the reaction vessel is a non-open flame radiation
  • the high temperature interlocking defocusing device comprises a first stage coke discharge tank and a second stage coke discharge tank connected to a first row of focus slide valves on the bottom defocused tube of the reaction kettle, connected to the first and second stage coke discharges a second sliding valve between the tanks and a third sliding valve connected under the secondary discharging tank, the three sliding valves interlocking the coke, the first-stage coke cans is provided with two rows of focal robots and one Focusing manipulator.
  • the high-temperature interlocking defocusing device comprises three parallel-discharging and co-operating coke-discharging tanks, wherein one front decanting tank is disposed on the same axis as the defocused tube of the reaction kettle, and the other two of the coke-discharging tanks
  • the central axis of the front decanting tank is disposed at an angle on the left and right sides, and the left and right rows of coke tanks are respectively inclined downwardly to the first-degree focal angle, and the three coke-discharging tanks respectively pass through a row of focal-slip valves
  • a discharge tube of the reaction kettle is connected, and the three slide valves interlock with each other, and a discharge robot is disposed on each of the discharge tanks.
  • the high-temperature interlocking defocusing device comprises two ashing reactors respectively connected to the bottom of the reactor and used for conversion, and a vaporization fractionation tower is respectively arranged on the top seal head of the two ashing reactors, and the fractionation
  • the tower is filled with a filler, and the top of the branching tower is provided with a cooling water coil, and the bottoms of the two ashing reactors are respectively connected to a row of slag containers through a row of slag, and the two rows of slag containers are respectively arranged with cooling Water jacket.
  • the two-stage feeding device comprises a hot-pressing and compacting roll device and a high-temperature sealing and feeding device, the hot-pressing and compacting roll device comprising a bucket elevator, and a flue gas jacketed furnace connected to the bucket elevator, a crawler type chain machine and a hot press hardening roll set in a jacketed furnace, a conveyor belt disposed under the hot pressurizing and thickening roll set, a cooling water spray head disposed above the conveyor belt, and a conveyor belt outlet a gantry file, a cooling pool disposed under the trowel and a squeegee chain machine disposed therein for conveying material to the high temperature sealing feeder.
  • the hot-pressing and compacting roll device comprising a bucket elevator, and a flue gas jacketed furnace connected to the bucket elevator, a crawler type chain machine and a hot press hardening roll set in a jacketed furnace, a conveyor belt disposed under the hot pressurizing and thickening roll set, a cooling water spray head
  • the high-temperature sealing feeding device comprises a hoist driven by a variable frequency speed regulating motor, a feeding inclined pipe connected between the hoist and a hopper with a mixer, and a sealed plastic melting feeding extrusion connecting the hopper
  • the feeding extruder comprises a pusher screw driven by a variable frequency speed regulating motor and a screw barrel surrounding the pusher screw, and a heating flue gas jacket is arranged at an exit of the feeding extruder
  • a feeding cylinder is vertically connected at the outlet of the feeding extruder, and a topping robot is disposed at the top of the feeding cylinder, and the bottom of the feeding cylinder is connected to the reaction vessel through a thermal expansion joint and a feeding valve.
  • the two-stage feeding device is a two-stage feeding extruder, and the two-stage feeding extruder comprises a screw barrel, and one end of the two barrels is respectively mounted with a speed regulating motor, and the output of the two speed regulating motors a screw is respectively connected to the end, and the two screws are respectively provided with spiral blades, and electric heating devices are respectively arranged around the two screw barrels; a feeding hopper with a stirring and discharging machine is arranged at the inlet of the first feeding extruder.
  • a catalyst hopper is disposed on an upper side of the hopper, an inlet of the secondary feeding extruder is located below the outlet of the primary feeding extruder, and an inlet of the secondary feeding extruder is provided with a double roller A hopper, an outlet of the secondary feeding extruder is connected to a feeding cylinder on a side of the top of the reactor.
  • the non-open flame radiant heating device comprises a ring jacketed furnace disposed around the reaction vessel and a combustion furnace disposed at a lower portion of the reactor, a ring flame guide or six flame tubes communicating with the ring jacket furnace And a burning furnace, a flame-retardant plate is disposed on the burning furnace, and a flame-retardant hole is disposed on the flame-retardant plate, and a burner is disposed on each side of the burning furnace, the burning The fire exit of the device is inclined in the direction of the furnace wall, so that the flame that is ejected forms a swirling flame in the furnace.
  • the flue gas dehumidification and dust removal device is a dust removal tower, a partition is arranged in the middle of the dust removal tower, the dust removal tower is divided into upper and lower sections, the upper part is sprayed with dust, and the lower part is water sealed and dusted, the dust removal tower a circulating water pump is disposed outside, and a recirculating water nozzle connected to the outlet of the circulating water pump is disposed in the dust removing tower, and a liquid flow pipe is disposed at a lowest point of the partition, and the flue gas inlet and outlet are respectively disposed on the dust removing tower In the lower stage, the outlet pipe at the top of the dust removal tower is connected to the water in the lower part of the dust removal tower, and the bottom of the dust removal tower is connected to the circulation water pump inlet through a filter.
  • the oil-water separation device includes a grease trap and a water-oil separator, the grease trap is connected to a bottom outlet of the oil extraction and refining device, and the oil-water separator is connected to a water outlet of the grease trap through a water pump.
  • the water outlet of the oil water separator is connected to the circulating water pump, and the oil drain of the grease trap and the oil water separator is connected Reactor.
  • the utility model also comprises a plastic crusher arranged between the hot press compacting roll device and the high temperature sealing feeding device, before the reaction kettle is arranged, and the hot waste oil and the heavy oil are transported to the reaction kettle. Tubular furnace.
  • the present invention has the following advantages due to the above technical solution: 1.
  • the present invention adopts a two-stage feeding device, and a heating device is arranged around the two-stage feeding device, so that the waste plastic conveyed through the two-stage feeding device is Semi-melting or close to melting state, therefore, it can effectively prevent the unsafe phenomenon that the occasional high-temperature oil and gas in the reactor is backflowed back to the screw barrel and the hopper; at the same time, two sets of stirring blades connected in series are arranged in the reaction kettle.
  • the reaction kettle is set to a negative pressure, which further prevents the back-flushing phenomenon occurring in the reaction kettle, and in particular, various types of interlocking slagging devices are arranged in the system, which effectively ensures the continuous large-scale operation of the present invention.
  • Industrial production. 2 The invention provides a hot press compacting roll device in the two-stage feeding device, and a flue gas jacketed furnace, a chain machine, a roll set, a conveyor belt, a gantry file, and a cooling pool are arranged in the hot press compacting roll device.
  • the chain machine in the pool so that it can be heated in the process of conveying the waste plastic in the chain machine, and is rolled by the hot-pressed and dense-rolled roll group to form a tightly pressed plastic belt, and the plastic belt can be
  • the cooling water nozzle is used to cool down, and is cut into smaller plastic pieces by the gantry boring tool, and then sent to the next process through the chain machine in the cooling pool.
  • the crusher can also cut the plastic into more. The fine particles effectively solve the problem of pre-treatment of waste plastics with a certain proportion of silt dust. 3.
  • the invention provides a high-temperature sealing feeding device in the two-stage feeding device, and a flue gas jacket is arranged at the outlet end of the high-temperature sealing feeding device feeding extruder, and the waste plastic is plasticized or melted into the reaction by the flue gas heating.
  • the kettle is arranged to reduce the blockage formed by the block material;
  • the bucking manipulator is arranged on the upper part of the feeding cylinder, and the feeding block is blocked or not smooth by manual or automatic processing by the robot;
  • an electronic monitor is arranged in the unloading inclined pipe, and is monitored with the regulator of the hoisting machine.
  • the invention provides a two-stage feeding extruder in the two-stage feeding device, and the outlet of the first-stage extruder is arranged above the inlet of the second-stage extruder, so that the structure is simple and the operation and control are convenient. 5.
  • the present invention is provided with a tubular heating furnace for preheating waste oil and heavy oil before the reaction vessel, so that the invention can be used for both waste plastic oiling and waste lubricating oil or heavy oil. It is a high-quality fuel or gasoline-diesel fraction that can be used in both catalytic cracking and non-catalytic cracking processes.
  • the invention adopts a ring-shaped jacketed furnace which is arranged around the reaction vessel and a combustion furnace which is arranged in the lower part of the reaction vessel, and which has a large flow cross section, small resistance, and can ensure the negative pressure of the furnace, or six flame guides.
  • the tube is connected to the annular jacketed furnace and the burning furnace.
  • the invention has various interlocking and decoking devices, so that the flow dynamic operation of the reaction kettle can be effectively ensured, and the opening or closing of each sliding valve or the slag discharging valve is realized during the operation of the reaction kettle. Interlocking and decoking, especially in the coke cans, a twisting manipulator is installed, which can discharge various jams in time to ensure the smooth operation of the coke. 8.
  • the invention also provides an ashing reaction kettle for conversion in the interlocking decoking device, further pulverizing the fluid state slag entering the ashing reaction kettle, making the waste plastic oil more thoroughly, and discharging the ash.
  • the slag is a solid carbon black and can be used as a fuel.
  • the present invention is provided with a flue gas dedusting and dust removing device including a dust removing tower and an oil-water separating device including a grease trap and a water-oil separator, so that the waste flue gas generated by the burning furnace can be sprayed and water-sealed and dust-removed. It is discharged into the environment to reduce environmental pollution. At the same time, the waste oil can be separated.
  • the water After the water is purified, it can be used for the dust removal tower.
  • the oil is returned to the reactor for further cracking, thus effectively solving the "three wastes" faced by the oilification equipment. solving issues.
  • the present invention when the present invention is provided with an exhaust gas coke boiler, it is also possible to use the coke produced by the apparatus of the present invention and excess gas as fuel to produce steam or the like.
  • Figure 1 is a schematic view of the system apparatus of the present invention
  • FIG. 2 is a schematic view showing the structure of a waste plastic hot press compacting roll device of the present invention
  • FIG. 3 is a schematic view showing the structure of the high temperature sealing feeding device of the present invention
  • Figure 4 is a schematic view showing the structure of the flow dynamic reaction kettle and the non-open flame radiation heating furnace of the present invention.
  • Figure 5 is a schematic view showing another structure of the flow dynamic reaction kettle and the non-open flame radiation heating furnace of the present invention.
  • Figure 6 is a schematic view showing the structure of the high temperature interlocking defocusing device of the present invention.
  • FIG 7 is another schematic structural view of the high temperature interlocking defocusing device of the present invention.
  • Figure 8 is a schematic view showing the structure of the branching-striping-condensing cooling device of the present invention
  • Figure 9 is a schematic view showing the structure of the oil-gas separation-gas absorption device of the present invention.
  • Figure 10 is a schematic view showing the structure of the liquefied gas recovery device of the present invention.
  • Figure 11 is a schematic view showing the structure of the oil extracting and refining device of the present invention
  • Figure 12 is a schematic view showing the structure of the "three wastes" processing apparatus of the present invention.
  • Figure 13 is another embodiment of the high temperature defocused device of the present invention.
  • the waste plastics cracking device capable of continuously large-scale industrial production of the present invention comprises: a hot press compacting roll device 1, a high temperature sealed charging device 2, a flow dynamic reaction kettle device 3, and a non-open flame radiation heating device 4
  • the high-temperature interlocking defocusing device 5 the fractionation-striping-condensation cooling device 6, the oil-gas separation-gas absorption device 7, the liquefied gas recovery device 8, the oil extraction and refining device 9, and the "three wastes" treatment device 10, and the like. The details are described separately below.
  • the newly added hot-pressed compacting roll device 1 of the present invention includes a front set
  • the bucket elevator 101 is connected to the bucket elevator 101 as a flue gas jacketed furnace 102.
  • the jacketed furnace 102 is a sandwich oven composed of an inner and outer two-layer structure that provides heat from flue gas waste heat.
  • the inner layer of the jacketed furnace 102 is provided with a motor-driven crawler type chain machine 103.
  • the crawler belt on the chain machine 103 feeds the waste plastic fed from the bucket elevator 101 back into the hot press compacting roll set 104, and the jacketed furnace.
  • the outer layer of the outer layer is provided with a flue gas jacketed furnace, and the waste plastic from the hot chain machine 103 is heated by the hot flue gas introduced from the flue gas inlet 105 to a softening temperature.
  • the control thermocouple 106 disposed on the upper portion of the roll set 104 and the regulating valve 107 on the flue gas inlet 105 automatically control the plastic softening rolling temperature.
  • the conveyor belt 108 disposed under the roll set 104 feeds the softened plastic strip rolled by the roll set 104 into a gantry cutter 109 mounted at the rear thereof, and is cut into small pieces, and a cooling water spray head is disposed above the conveyor belt 108.
  • the softened plastic strip rolled out by the roll set 104 is cooled and hardened to facilitate cutting and preventing adhesion.
  • the small piece of plastic cut from the file 109 falls into the cooling pool 111 at the lower part of the file 109.
  • the cutting frequency of the file 109 can be adjusted according to the required size of the cutting block.
  • the scraping type chain machine 112 disposed in the pool 111 can be cooled.
  • the rear plastic piece is sent to the subsequent equipment on the shore of the pool 111, and the rotational speed of the chain machine 103 and the gap of the roll set 104 can be set to be adjustable and controllable.
  • the high-temperature sealing and feeding device 2 of the present invention comprises a hoist 201 disposed at the front portion, which is driven by the variable frequency speed regulating motor 202, and can be controlled by the speed regulating motor 202 and the regulator 203.
  • the blanking pipe 204 is connected to the hoist 201 and the hopper 205 with the mixer.
  • the electronic monitor 206 is disposed in the middle of the blanking pipe 204 to monitor the smoothness of the blanking, and continuously feeds the monitored information into the regulator 203. Thereby, the feed amount of the hoisting machine 201 and the pushing speed of the unloading inclined pipe 204 are adjusted.
  • a high temperature sealed plastic melt extruder 207 is disposed below the hopper 205.
  • the feed extruder 207 includes a pusher screw 209 that is driven by the variable speed motor 208 and a barrel 210 that surrounds the pusher screw 209.
  • the use of the variable frequency speed regulating motor 208 makes the pushing speed of the pushing material easier to control, and makes the feeding extruder 207 operate safely and reliably, which provides a guarantee for the automation of the feeding, and can prevent the occurrence of an accident or terminate the accident in time.
  • the feeding extruder 207 is also characterized in that a flue gas jacket 211 is provided at the outlet thereof, and the waste plastic is plasticized or melted into the reaction vessel 301 by the flue gas heating.
  • the charging cylinder 212 is vertically installed on the top sealing head of the reaction vessel 301, and is connected with a feeding extruder 207 and a reaction kettle 301.
  • a charging robot 213 is disposed at the top of the charging cylinder 212, and a cutter 214 is disposed at the end of the robot 213 to prevent In case of plastic congestion at the bottom of the feeding cylinder, the dredging process is used.
  • the thermal expansion joint 218 is disposed at a lower portion of the charging cylinder 212 to absorb the stress generated by the thermal expansion and contraction. This stress is due to the high temperature of the reaction vessel 301 during operation, and the reactor 301 is thermally expanded to extend upward by 10 to 30 mm, and the feeding extruder is fed.
  • a monitoring alarm thermal element 215 is disposed in the middle of the feeding extruder 207.
  • the alarm thermal element 215 immediately sends a signal to the regulator 216, the regulator 216 is adjusted and sent to the frequency converter motor 208 of the feeding extruder 207, automatically adjusting the pushing speed of the variable frequency motor 208, accelerating the pushing material to block the return air; Then, the feed valve 217 will be quickly closed, and the feed extruder 207 and the lifter 201 will be stopped by the signal.
  • the monitoring the thermal element 215 sends a signal to the variable frequency motor 208, starts the feeding extruder 207 and the elevator 201, and then opens the feeding valve 217 to resume normal operation.
  • the flow dynamic reactor device 3 of the present invention comprises a flow dynamic reaction vessel 301.
  • the reactor 301 is provided with upper and lower two-stage stirring blades 302 and 303, a rectangular stirring blade 302 and a curved shape.
  • the agitating paddles 303 are arranged in a crossover arrangement (the two are schematically drawn in one plane), and the vertical bearings between the upper and lower agitating paddles 302 and 303 are provided with vertical bearings, which are adjustable in centrality. Tie rod support. All the blades of the paddles 302, 303 are provided with a knife edge on both sides to break the coke block or the sintered plastic block in the liquid.
  • An electric heating jacket furnace 404 is disposed around the reaction vessel 301 to provide heat required for the reaction; a vaporization-fractionator 306 is disposed on the top of the reactor head, and a cooling water coil 307 is disposed at the top of the reactor to provide internal reflux to generate the entire tower. Rectification.
  • the tower is filled with a high efficiency Pall ring.
  • the light component gasoline split or naphtha fraction
  • the diesel portion is extracted from the side line of the middle of the tower, and the heavy heavy oil and heavy wax are fractionated and returned to the reaction vessel 301.
  • the removal of light components ensures that the flash point of diesel or high quality fuel is acceptable, and the removal of heavy components and heavy wax ensures that the carbon residue and freezing point are acceptable.
  • a defocused tube 304 with an anti-coking jacket is arranged, which can prevent the high temperature flue gas from burning the defocused tube, avoiding the coking of the heavy oil in the tube wall, and ensuring the smooth discharge path.
  • the catalyst slurry feeding device 305 is disposed on the top of the reaction kettle 301.
  • the lower isolation tank is equipped with a high temperature resistant glass plate level gauge to control the catalyst paddle addition speed.
  • a foaming section 306 is arranged on the top of the reactor 301, and a grid support plate and a Pall ring are arranged in the foaming gasification section 306.
  • the top of the vaporization section 306 is provided with a cooling water coil 307 for generating internal reflux and a light oil return pipe 308 for providing external reflux.
  • the charging cylinder 212 disposed at the top of the reaction vessel 301 is installed at a 90° angle to the feed feeding extruder 207.
  • the non-open flame radiation type heating device 4 of the present invention is disposed under the reaction vessel 301 and integrated with the reaction vessel 301.
  • the utility model comprises a furnace skirt 401.
  • a circular flame guiding sleeve 402 (as shown in FIG. 4) or six to eight flame guiding tubes 403 (shown in FIG. 5) are arranged around the skirt 401, and a ring around the reaction kettle 301 is arranged.
  • the jacket furnace 404 and the combustion furnace 405 at the lower portion of the reactor 301 are in communication via a ring flame guide 402 or a flame tube 403.
  • the heating device of the present invention is different from the conventional reaction combustion furnaces in that the flow section of the flame trap 402 or the flame guiding tube 403 is larger than twice the cross section of the jacketed furnace 404 around the reaction vessel 301. This reduces the flow resistance of the flue gas from the wide flow volume of the furnace and shortens the section, ensures the vacuum of the furnace and good combustion state, and prevents the furnace from generating positive pressure, which provides a guarantee for improving the furnace temperature.
  • This design solves the problem that the flow path of the flame tube is small in the previous design, causing large resistance, low vacuum of the furnace, and even positive pressure combustion often occurs, the flame exits the furnace door, is unsafe, and limits the temperature increase of the furnace, so that the reaction is provided. Insufficient heat and other issues.
  • a waveform thermal expansion joint 406 is disposed at the upper and lower ends of the flame shield 402 or the flame tube 403 (as shown in FIG. 4 and FIG. 5). Show), to absorb the thermal expansion stress, to ensure the normal operation of the furnace.
  • This structure solves the problem that the expansion ring is seriously leaked in the previous design, the furnace vacuum is lowered, and the combustion is poor, which not only solves the problem of absorbing thermal expansion stress but also ensures the furnace sealing problem.
  • a radiation obstruction plate 407 made of a high-radiation-resistant high-temperature (1000 ⁇ or higher) material is disposed on the combustion furnace 405, and a flame-retardant hole is disposed on the flame-retardant plate 407, and a flame-retardant hole is distributed on the flame-retardant plate 407.
  • the plate 407 prevents the flame from directly contacting the reaction vessel 301, forming a non-open flame radiant heating mode.
  • the design of the present invention is combined with the aforementioned large flame-conducting cross-section channel structure, which can not only allow a high furnace temperature, fully ensure the heat supply of the reactor, but also ensure the safe operation of the production, and fundamentally solve the flammability.
  • the burner 408 used in the combustion furnace 405 is a mixed oil and gas type, and has the functions of automatic ignition, flame monitoring, flameout protection, etc., which are disposed on the lower part of the furnace and above the ash, and two burners are respectively disposed in the combustion furnace 405.
  • the fire inlet is inclined in the direction of the furnace wall, so that the flame that is ejected forms a flame in the furnace, so that the heat of the flame trap 407 is more uniform.
  • a flue gas outlet 409 is disposed at an upper portion of the reactor annular jacket furnace 404, and the derived flue gas can be removed from the jacketed furnace 102 of the hot press densification roll device 1 and the flue gas jacket 211 of the high temperature seal feeding device 2, and the like.
  • the flue gas is finally sent to the "three wastes" treatment unit 10 for flue gas de-blackening treatment, and finally the water vapor, nitrogen and carbon dioxide are discharged from the chimney.
  • the high temperature interlocking defocusing device 5 of the present invention is disposed on one side of the reaction vessel 301, and is composed of a primary coke discharge tank 501 and a secondary coke discharge tank 502.
  • the first stage coke canister 501 and the reaction kettle 301 are connected by a jacketed discharge tube 304.
  • a first discharge spool valve 503 is disposed on the exhaust pipe 304.
  • a second spool valve 504 is disposed between the secondary coke cans 501, 502, and a third spool valve 505 is disposed below the secondary coke canister 502.
  • the three valves 503, 504, and 505 operate in an interlocked state, that is, in the normal state, the spool valve 503 is normally open, and the spool valves 504 and 505 are normally closed.
  • the interlocking coke removal procedure is as follows: In the first step, when a certain amount of coke paddle is deposited in the first-stage coke oven 501, the slide valve 503 is closed, and the connection with the reaction kettle 301 is cut off to ensure the safety of slag discharge.
  • the valve is in the closed state; the second step, the slide valve 504 is opened, the coke residue in 501 is discharged into the secondary coke discharge tank 502, and in the third step, the slide valve 504 is closed, and the slide valve 505 is opened, the opening degree is 10 ⁇ 30 %, let it gradually drain the slag, fall into the slant bottom defocusing pool 506, and carry the condensed and cooled coke block in the water to the ground by a chain scraper (not shown).
  • the above three steps of slagging are continuously repeated, and the coke generated in the reaction is continuously discharged to ensure continuous operation of the device.
  • Three robots 507, 508, 509 are respectively disposed at the top and the side of the first-stage coke can 501, and the top ends of the robots 507, 509 are respectively provided with a sparse drill pipe having a trigeminal drill bit, and the robot 509 is directly connected to the exhaust pipe 304 and At the bottom of the reaction vessel 301, the robot 507 passes straight through the valve front of the spool 505. The bottom of the robot 508 is a disk to monitor the accumulation of the bottom of the primary coke 501.
  • the robots 507, 508, and 509 can be controlled automatically or manually.
  • the high-temperature interlocking defocusing device 5 of the present invention can also adopt a multi-head structure, which is different from the above-mentioned single-head interlocking defocusing device in that three sets of parallel decanting tanks 510 are provided. , 511, 512, available Run in conversion, flexible operation, increase the flow of defocused.
  • the front decanting tank 510 is disposed on the same center line as the reaction vessel 301, and is connected to the defocused tube 305 through the defocused sliding 513.
  • the horizontal dipstick 514 is disposed on the same axis of the decanter 510 and the defocused tube 305.
  • the left and right side decanting tanks 511, 512 are disposed at a position horizontally at an angle of about 30° to the left and right of the central axis of the coke-discharging tank 510, and have the same structure as the coke-discharging tank 510, but the left and right sides of the coke-discharging tanks 511 and 512 are designed.
  • the flow axis has a certain degree of flow coke, that is, the central axis of the defocusing tubes 514, 515 of the coke drums 511, 512 is inclined at an angle of 5 to 15 ° with the horizontal angle, which is favorable for the downward flow of the coke pad and prevents the coke from being discharged.
  • the bottoms of the tubes 514, 515 are deposited.
  • the fractionation-strip-condensation cooling device 6 of the present invention comprises a fractionation tower 601 with a flue gas jacket 602 as a heat source in the lower portion, and a grid support plate 603 is arranged in the lower portion of the fractionation tower 601, and supports A high efficiency Pall ring packing 604 is placed in the tower.
  • the bottom of the tower is provided with a heavy diesel fuel collecting tank 605 and its extraction line side line 606, a light diesel oil collecting tank 607 and its extraction line side line 608, a kerosene fuel collecting tank 609 and its extraction side line 610.
  • a gasoline return port 611 From the top of the tower to the bottom of the tower, there are a gasoline return port 611, a kerosene return port 612, a light diesel oil return port 613, a heavy diesel oil return port 614 and a heavy oil return port 615.
  • the kerosene stripper 616, the light diesel stripper 617, and the heavy diesel stripper 618 are mounted on the same axis from top to bottom, and they are disposed on the side of the fractionation column 601.
  • the condensing cooling water tank 619 is disposed on the lower side of the stripping towers 616, 617, and 618 so that each oil flow can automatically flow through the respective condensing cooling coils 620 to the next process by means of the difference.
  • the cooling tower 621 is installed at the top of the water tank 619, and the circulating water pump 622 is installed on the bottom side of the water tank 619, and the hot water is pumped into the cooling tower 621, which is sprayed and cooled, and recycled.
  • the oil-gas separation-gas absorption device 7 of the present invention comprises an oil-gas separation column 701, a primary gas absorption tower 702, a secondary gas absorption tower 703, and a water-sealing tank 704, etc., a secondary absorption tower.
  • the 703 is filled with high efficiency Pall ring packing 705. 1.
  • the secondary absorption tower removes the harmful components mixed in the reaction cracking gas, such as hydrogen chloride, hydrogen sulfide, etc., and sends it to the liquefied gas recovery unit 8.
  • the liquefied gas (LPG) recovery unit 8 of the present invention includes a low pressure gas stabilizing tank 801, and a clean cracking gas introduction tank 801 sent from the unit 7 is sent to the primary compressor 802 after the pressure is stabilized. , compressed to 0.3 ⁇ 0.4Mpa, sent to the first-stage compression condensate tank 803, which is equipped with a condensing cooling coil 804, which condenses part of the heavier liquefied gas component into light gasoline recovery, and after de-heavy components
  • the cracked gas is sent to the secondary compressor 805 to be compressed to 0.5 to 0.8 MPa, and then sent to the condensing cooler 806.
  • the liquefied gas component is condensed into a liquid, that is, LPG, and then sent to the high pressure liquid gas separation tank 807, where In the 807 tank, LPG is separated from the dry gas (methyl hydrazine, ethane, ethylene component) which cannot be compressed and liquefied.
  • LPG flows from the bottom of the tank into the high-pressure liquefied gas storage tank 808, and then through the bottled pump 809, and several bottled packing lines 810 The bottle is for sale for civilian use.
  • Dry gas is sent from the top of the 807 tank to the high-pressure dry gas stabilization tank 811, and the water seal flame arrester 812 is sent to the furnace as a fuel for own use. If there is excess flare, it can be sent to the boiler 12 (if set) for fuel.
  • a self-operated pressure self-control valve 813 is mounted on the torch vent line of the flame arrester 812, which controls the full system pressure.
  • the oil extracting and refining device 9 of the present invention comprises a gasoline-light diesel oil extraction system. They are composed of A-extraction tanks 901, 902, B-extraction tanks 903, 904, and additive blending tanks 905, 906, and the like.
  • the gas oil and crude gasoline produced from the cracking reactor and the branching tower cannot fully meet the quality requirements of the national standard and need to be refined.
  • the gas oil is first sent to the A-extraction tank 801, the A agent is added, and the A-extraction purification process is carried out, the non-ideal components are removed, and then sent to the B-extraction tank 803, and the B-extractant is added to further remove the non-ideal components and then fed.
  • the mixing tank 805 is added to the qualified product delivery device for sale according to the performance requirement and the necessary additives; the crude gasoline extraction and refining process is also the same.
  • the "three wastes" processing device 10 of the present invention includes a flue gas de-blackening and dust removing device and a water-oil separating device.
  • the flue gas de-blacking and dust removing device includes a dust removing tower 1001, and a circulating water pump 1004 is disposed outside the dust removing tower 1001.
  • a set of recirculating water nozzles 1005 connected to the outlet of the circulating water pump 1004 is disposed in the dust removing tower 1001.
  • a separator 1006 is arranged in the middle of the dust removal tower 1001, and the dust removal tower 1001 is divided into upper and lower sections, the upper section is sprayed with dust, and the lower section is water sealed and dusted.
  • a liquid flow tube 1007 is disposed at the lowest point of the partition 1006, and the dust removal tower is disposed.
  • the bottom of the 1001 is connected to a filter, and the outlet of the filter is connected to the inlet of the circulating water pump 1004.
  • the flue gas inlet of the dust removing tower 1001 is connected to the flue gas outlet 409 of the non-open flame radiant heating device 4 through a pipeline, and the flue pipe at the top of the dust removing tower 1001 is connected to the stagnant water in the lower section of the dust removing tower 1001, so that the flue gas is in the stagnant water. After the water seal is further removed from the water, it is discharged from the flue gas outlet disposed in the lower stage of the dust removal tower 1001.
  • the oil-water separation device includes a grease trap 1009 and a water separator.
  • the grease trap 1009 is connected to the bottom of the oil extraction and refining device.
  • the oil-water separator 1008 is disposed behind the grease trap 1009, and a pump 1010 is disposed therebetween.
  • the water pump 1010 pumps the water separated from the grease trap 1009 to the oil-water separator 1008.
  • the purified water treated by the oil-water separator 1008 is returned to the dust-removing tower 1001 by the circulating water pump 1004 for use in the dust-removing tower 1001, the grease trap 1009 and the oil-water tank.
  • the oil separated by the separator 1008 is returned to the reaction vessel 301 to continue cracking.
  • the hot press compacting roller device 1 and the high temperature sealing feeding device 2 may be changed, for example, the hot press compacting roll device 1 and the high temperature sealing and feeding device 2 are set to two stages.
  • Feed extruders 220, 230, primary feed extruder 220 are located in front of secondary feed extruder 230.
  • the two-stage feeding extruders 220 and 230 respectively include a screw barrel 221 and 231, and a speed regulating motor 222 and 232 are respectively installed at the ends of the two screw barrels 221 and 231, and the output ends of the two speed regulating motors 222 and 232 are respectively connected with a screw. 223, 233, the two screws 223, 233 are respectively provided with spiral blades (not shown).
  • the screw 223 of the primary feeding extruder 220 may be a single screw or a relatively rotating twin screw.
  • the two barrels 221 and 231 are respectively provided with self-controlled electric heating metal bath blocks or other electric heating devices for heating the barrels 221 and 231, and the lower parts of the two barrels 221 and 231 are provided with a firm bracket.
  • the inlet of the first-stage feeding extruder 220 is provided with a hopper 224 with a stirring and discharging machine.
  • the upper side of the charging hopper 224 is provided with a quantitatively-addable catalyst hopper 225, and the inlet of the secondary feeding extruder 230 is located at the first-stage feeding and extruding.
  • the inlet of the secondary feeding extruder 230 is provided with a hopper 235 with a double roller 234, and the outlet of the secondary feeding extruder 230 is connected to the charging cylinder 212 on the top side of the reaction vessel 301.
  • the waste plastic After being pulverized, the waste plastic is lifted into the hopper 224 of the primary feeding extruder 220, and proportionally The catalyst in the catalyst hopper 225 is fed into the hopper 224, mixed with the waste plastic into the primary feeding extruder 220, pushed vigorously forward by the screw 223, and heated by the electric heating device outside the screw 221 to the softening temperature.
  • the outlet of the barrel 221 causes the waste plastic in a semi-molten state to fall into the hopper 235 through the double rollers 234 of the secondary feeding extruder 230, and is then extruded into the secondary feeding extruder 230, which is a waste plastic in a visco state.
  • the outlet of the secondary feeding extruder 230 is extruded, and is introduced into the reaction vessel 301 through the charging cylinder 212 to carry out a cracking reaction.
  • the electric heating device outside the two-stage feeding extruder 220, 230 barrels 221, 231 only heats up at the initial stage of startup, and after normal operation, the strong pushing force of the screws 223, 233 causes the extruded plastic to be extruded. It generates enough heat to soften automatically. At this time, the electric heating stops heating under the control of the control system.
  • the waste plastic extruded from the secondary feeding extruder 230 is in a semi-melting or near-melting state, and can effectively prevent the unsafe phenomenon that the occasional temperature and oil in the reactor 301 is countercurrently returned to the screw barrel 231 and the hopper 235. .
  • the reaction kettle 301 is operated by micro-negative pressure, which can effectively avoid the occurrence of high-temperature oil and gas back-flux.
  • the structure of the high temperature interlocking defocusing device 5 can be various.
  • the slag discharging pipes 304 disposed at the bottom of the reaction kettle 301 are two, and the outlets of the two oil discharging slag pipes 304 are respectively connected to one.
  • the ashing reactors 521 and 522 are provided with heating means around the ashing reactors 521 and 522.
  • the pyrolysis oil and coke discharged from the bottom of the reactor 301 into the two ashing reactors 521 and 522 are further cracked to form oil vapor and Ash residue.
  • the oil vapor generated in the two ashing reactors 521, 522 rises to the vaporization fractionation columns 523, 524 disposed on one side of the top seal head, the tower is filled with a high efficiency Pall ring packing, and the top of the tower is provided with a cooling water coil 525. 526, used to generate internal reflux.
  • the light sputum oil gasoline fraction
  • the middle part of the oil is extracted from the middle (diesel part)
  • the heavy oil and heavy wax are returned to the reactor for cracking.
  • the final residue formed by secondary cracking in the two ashing reactors 521, 522 is ash, discharged into the slag discharge containers 529, 530 through the bottom slag discharge valves 527, 528, and cooled by the surrounding cooling water jackets 531, 532. Thereafter, the system is discharged from the ash discharge valves 533, 534 and carried away by the trolley.
  • the two ashing reactors 521, 522 are used in turn, one operation, and the other can discharge coke.
  • the number of each of the decanting tanks (or ashing reactors) and the defocusing valves of the high-temperature interlocking defocusing device 5 can be changed, for example, the number of the coke-removing tanks is 2 to 4, The number of focal lengths is 2 to 8.
  • the "three wastes" treatment device 10 can also adopt various flue gas and oil-water separation devices in the prior art, even if the de-blackening and dust removal device and the oil-water separation device of the present invention are used, the dust removal tower 1001, the grease trap 1009 and the oil-water separator In addition to 1008, it is also possible to add a replacement to other structures and devices.
  • the waste plastic is removed from mud sand, masonry, cotton cloth, wood, iron filings, etc., as shown in FIG. 1 and FIG. 2, it is firstly crushed and sent to the bucket elevator 101 installed at the foremost part, and then The crawler type chain machine 103 and the roll set 104 surrounded by the flue gas waste jacketed furnace 102 are hot-rolled into plastic strips, and the waste plastics are densified by a packing density of less than 0.1 t/m 3 through the cooling head 110 and the boring tool 109. Become a small piece of plastic of 0.5 ⁇ 1.2t/m 3 . It is also possible to feed the crusher 11 (shown in Fig.
  • the apparatus of the present invention simultaneously processes waste oil or heavy oil, the tubular heating furnace 12 for preheating the waste oil and the heavy oil is placed before the reaction vessel 301, so that the waste plastic and the waste oil can be separately entered separately.
  • the reaction vessel 301 can also be mixed into the reaction vessel 301 while being mixed in any ratio, and cracked into various light fuel oils or gasoline diesel oil.
  • the oil and gas mixture generated by the reaction kettle 301 is introduced into the fractionation column 601 (shown in Figs. 1, 8) from the top, and the gasoline and gas are discharged from the top of the column 601, and the kerosene is extracted from the side line of the tower, light and heavy.
  • Diesel, light and heavy diesel oil is liquid phase inflow into kerosene, light and heavy diesel stripper 616, 617, 618 stripping, kerosene and light diesel oil combined and heavy diesel oil flow through condensing cooling water tank 619 to cool.
  • the gasoline vapor and gas at the top of the fractionation column 601 are cooled by the condensing cooling water tank 619, and then flowed into the oil-gas separation column 701 (as shown in Figs. 1 and 9), and the gasoline is refluxed into the fractionation column 601 to control the temperature at the top of the column to control the quality of the gasoline.
  • the separated crude gasoline is fed into the extraction refining device 9; the gas is introduced into the liquefied gas recovery device 8 (shown in Figs.
  • the accumulated water at the bottom of the dust removal tower 1001 is filtered and sent to the circulating water pump 1004 for further use, and the carbon black in the filter can be used as a fuel.
  • the water After the oil and water separation from the bottom outlet of the oil extraction and refining device 9 into the grease trap 1009, the water enters the oil water separator 1008, and the water from the oil water separator 1008 is sent to the circulating water pump 1004 for further use, and is separated from the grease trap 1009 and the oil water.
  • the oil separated by the vessel 1008 is returned to the reactor 301 to continue cracking.
  • the present invention may select all or part of the apparatus of the system of the present invention as needed, and may add some means to the system of the present invention, such as providing an exhaust gas coke breeze 13 with coke and excess gas produced by the apparatus of the present invention. Fuel, steam production, etc.
  • the invention utilizes waste plastic or waste lubricating oil or heavy oil, etc., and can continuously industrialize large-scale production of gasoline fraction, diesel oil or high quality fuel oil and civil liquefied gas.
  • the "three wastes" treatment device is arranged in the equipment, so that the exhaust gas, the waste oil and the waste water of the invention are treated, the exhaust gas discharged to the environment is minimized, the waste water is recycled, and the separated oil is returned to the reactor for cracking. .

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  • Chemical & Material Sciences (AREA)
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  • Engineering & Computer Science (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Wood Science & Technology (AREA)
  • Materials Engineering (AREA)
  • Combustion & Propulsion (AREA)
  • Processing Of Solid Wastes (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
  • Separation, Recovery Or Treatment Of Waste Materials Containing Plastics (AREA)

Abstract

La présente invention porte sur un appareil de fabrication d’huile à partir de déchets plastiques dans la production industrielle en continu. Elle comporte un réacteur, un magasin d’alimentation connecté au réacteur, un radiateur pour le réacteur, un suppresseur de coke situé au fond du réacteur, un jeu de colonnes de fractionnement, dépouille, refroidissement et condensation, des récipients de séparation de gaz combustible et des réservoirs d’absorption de gaz, une tour de raffinage d’extraction d’huiles, et des récipients de récupération de GPL successivement après le réacteur. Les caractéristiques de l’appareil sont les suivantes : dispositif à triple traitement de déchets comprenant un dispositif de dénoircissage et de dépoussiérage de gaz combustible et un séparateur d’huile et d’eau. Le dispositif de dénoircissage et de dépoussiérage de gaz combustible se fixe à une sortie de gaz combustible du radiateur du réacteur. Le séparateur d’huile et d’eau se combine avec la tour de raffinage d’extraction d’huile. Le magasin d’alimentation comporte des dispositifs d’alimentation à deux niveaux et il est entouré d’un appareil de chauffage. Le radiateur de réacteur est un radiateur rayonnant fermé à l’air libre. Le suppresseur de coke se compose de 2 à 4 réservoirs d’enlèvement de coke et de 2 à 8 valves d’enlèvement de coke solidaires. La présente invention peut s’utiliser non seulement pour le craquage permettant de récupérer de l’huile des déchets plastiques, mais également pour le craquage permettant de fabriquer un combustible entier ou un combustible fractionné haute qualité à partir d’huile de lubrification usagée ou d’huile lourde, et pour récupérer du GPL et ainsi de suite.
PCT/CN2005/001195 2004-08-06 2005-08-04 Appareil de fabrication d’huile à partir de déchets plastiques dans la production industrielle en continu Ceased WO2006012800A1 (fr)

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CNB2004100580183A CN1250677C (zh) 2004-08-06 2004-08-06 可连续工业化大规模生产的废塑料油化装置
CN200410058018.3 2004-08-06

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CN108913165A (zh) * 2018-09-20 2018-11-30 陕西冶金设计研究院有限公司 一种油页岩干馏半焦干法出焦装置
CN110180307A (zh) * 2019-06-24 2019-08-30 中国船舶重工集团公司第七0三研究所 一种应用于燃气轮机的静态油气分离器
CN111377589A (zh) * 2018-12-31 2020-07-07 潍坊奥华环保新材料科技有限公司 一种用于生产岩棉电熔炉的自动气体喷吹加料的工艺
CN111500305A (zh) * 2020-04-28 2020-08-07 徐宗胜 废塑料处理设备
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CN111205884B (zh) * 2020-03-11 2022-02-15 张忠余 一种废塑料炼油设备
CN114164022B (zh) * 2021-11-24 2023-06-09 成都前成科技有限公司 一种塑料再生油的醚化和溶剂精制工艺
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WO2008022790A3 (fr) * 2006-08-25 2008-07-17 Granit Systems S A Procédé et dispositif pour le traitement de déchets à teneur en matière plastique
CN108217777A (zh) * 2018-02-12 2018-06-29 四川旭航新材料有限公司 一种油水分离模块、油水分离系统及方法
CN108217777B (zh) * 2018-02-12 2024-04-26 四川旭航新材料有限公司 一种油水分离模块、油水分离系统及方法
CN108913165A (zh) * 2018-09-20 2018-11-30 陕西冶金设计研究院有限公司 一种油页岩干馏半焦干法出焦装置
CN111377589B (zh) * 2018-12-31 2022-05-06 潍坊奥华环保新材料科技有限公司 一种用于生产岩棉电熔炉的自动气体喷吹加料的工艺
CN111377589A (zh) * 2018-12-31 2020-07-07 潍坊奥华环保新材料科技有限公司 一种用于生产岩棉电熔炉的自动气体喷吹加料的工艺
CN110180307A (zh) * 2019-06-24 2019-08-30 中国船舶重工集团公司第七0三研究所 一种应用于燃气轮机的静态油气分离器
CN110180307B (zh) * 2019-06-24 2024-05-28 中国船舶重工集团公司第七0三研究所 一种应用于燃气轮机的静态油气分离器
CN111500305B (zh) * 2020-04-28 2024-02-20 徐宗胜 废塑料处理设备
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