CN1526793A - Industrial method of reusing waste plastics to produce gasoline and diesel oil - Google Patents
Industrial method of reusing waste plastics to produce gasoline and diesel oil Download PDFInfo
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- CN1526793A CN1526793A CNA031346618A CN03134661A CN1526793A CN 1526793 A CN1526793 A CN 1526793A CN A031346618 A CNA031346618 A CN A031346618A CN 03134661 A CN03134661 A CN 03134661A CN 1526793 A CN1526793 A CN 1526793A
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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
- C10B47/28—Other processes
- C10B47/32—Other processes in ovens with mechanical conveying means
- C10B47/44—Other processes in ovens with mechanical conveying means with conveyor-screws
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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
- 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
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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
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/141—Feedstock
- Y02P20/143—Feedstock the feedstock being recycled material, e.g. plastics
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- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Combustion & Propulsion (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
- Separation, Recovery Or Treatment Of Waste Materials Containing Plastics (AREA)
Abstract
The present invention is industrial method of reusing waste plastics to produce gasoline and diesel oil. Waste plastics including polyethylene, polypropylene and polystyrene in certain proportion are mixed and heated to liquefy and crack inside one reactor with double-screw stirrer inside it and molten salt inside sandwiched layer as heat conducting medium; the produced material is viscosity reducing cracked and the cracked gas is condensated into liquid fed to rectifying tower; molten plastic liquid is pumped from the reactor into one solid-liquid separator with separating molten salt liquid to separate residue and dirt; clean molten plastic is returned to the reactor while the separated residue and dirt is exhausted via screw extruder in the bottom of the separator; and decompression distillation is performed to produce oil. The present invention can produce oil with high quality in low cost and high conversion rate while tackling white pollution.
Description
Affiliated technical field
The present invention relates to the method that industrialization is produced gasoline, diesel oil with plastic waste, belong to petrochemical complex refining field.
Background technology
From the seventies in last century so far, the a lot of scientific research personnel in the whole world have paid great amount of manpower and material resources and have engaged in the research that utilizes plastic waste to produce vapour, diesel oil, especially China, more outstanding, only delivering of patent documentation just has 100 parts more than, and consistent generally acknowledge adopt plastic waste to produce gasoline, the diesel oil technology is a kind of method that reclaims plastics preferably.See with regard to present disclosed patent documentation, existing method of producing gasoline, diesel oil with plastic waste mainly is that plastic waste is adopted complicated catalytic cracking technology, burn with fire is straight then, form the higher liquid of viscosity behind the oiling, obtain gasoline, the diesel oil of finished product by the rectifying tower distillation.There is following deficiency in aforesaid method: the catalyst cracker that (1) needs are complicated; When (2) burning with fire is straight, the plastic waste inequality of in melting process, being heated, temperature or high or low influence the plastic cracking degree of depth and coking phenomenon occurs, makes the processed oil downgrade; (3) the plastics oiling is thermo-negative reaction, and the heat conductivility of its material is relatively poor, and the time that reaches the thermally splitting temperature is longer, and wall green coke phenomenon appears in the heat exchange weak effect; (4) liquid viscosity that forms behind the plastic waste oiling is higher, and is mobile poor, do not have visbreaking unit, and this material can cause the load of rectifying tower as rectifying tower distillatory basic material, produces a large amount of recycle stock, makes the oil refining cost up; (5) plastic waste has a certain amount of earth, sandstone etc. and mixes in collection, letter sorting, fusion process, does not remove the tripping device of this objectionable impurities, causes deslagging not thorough, and can not operate continuously; (6) normal pressure or positive pressure operation reduce the dial-out degree of depth of oil product and oil product transformation efficiency, waste energy.
Summary of the invention
Technology of the present invention is dealt with problems and is: a kind of complicated catalyst cracker that do not need is provided, but continuous production, oil product transformation efficiency height, oil quality is good, cost is low, the method that the industrialization of save energy is produced gasoline, diesel oil with plastic waste, thus the defective that existing plastic waste is produced gasoline, the existence of diesel oil method solved.
Technical solution of the present invention is: the method that industrialization is produced gasoline, diesel oil with plastic waste, its feature comprises the following steps:
(1) with plastic waste polyethylene, polypropylene, polystyrene, or polyethylene, polystyrene, or polypropylene, polystyrene fusion in proportion;
(2) plastic waste that above-mentioned fusion is good has two helical ribbon agitators in advancing, and adorns in the reactor of fused salt heat-conducting medium chuck the heating cracking of liquefying outward;
(3) to the plastic waste in the reactor through heating pyrolyze, the material that reaction generates carries out viscosity breaking, cracked gas forms liquid through condensation, send rectifying tower to carry out rectifying;
(4) simultaneously, in constantly being pumped to, plastics fusion liquid in the reactor is equipped with in the solid-liquid separation cylinder of fused salt parting liquid, residue in the reactor, earth are effectively separated, residue, earth are discharged outside the cylinder by the screw extrusion press of solid-liquid separation cylinder bottom, and clean plastics fusion liquid returns in the reactor;
(5) finish in (2), (3), (4) step, implement underpressure distillation.
Mix proportions in the plastic waste in the described step (1) is a polyethylene: polypropylene: polystyrene is 0.8～1.2: 0.8～1.2: 0.7～0.9, or polyethylene: polystyrene is 0.8～1.2: 0.3～0.5, or polypropylene: polystyrene is 0.8～1.2: 0.3～0.5, wherein preferred proportion is a polyethylene: polypropylene: polystyrene is 1: 1: 0.8, or polyethylene: polystyrene is 1: 0.4～0, or polypropylene: polystyrene is 1: 0.4.
Reactor in the described step (2) is flute profile reactor or vertical response still, and temperature of molten salt is 200 ℃～800 ℃, and preferred temperature is 450 ℃～550 ℃.
Plastics heating liquefaction cracking temperature in the described step (2) is 350 ℃～400 ℃.
Two helical ribbon agitators in the described step (2) are that outer ribbon turns clockwise, and interior ribbon is rotated counterclockwise, and outer ribbon and reactor inwall are spaced apart two helical ribbon agitators of 2mm～5mm.
Visbreaking mode in the described step (3) adopts visbreaking still or other demulcent low temperature pyrolyzer modes, wherein the visbreaking kettle is horizontal round shape, and vertically fire tube arrangement is provided with sedimentation tank in the still at the bottom of the still, still center upper portion and distillation tower join, and the visbreaking temperature of plastic liquid is 250 ℃～300 ℃ in the still.
Solids constituent in the described step (4) is a cone-shaped body from cylinder body, the outlet of cylinder upper end is connected with the reactor gaseous phase outlet, the lower end of cylinder is provided with screw extrusion press, cylinder body taper tangent line place establishes a material inlet, the reactor slag-drip opening is connected in series with the solid-liquid separation cylinder material inlet through pump, the loadings of the molten parting liquid of salt is 2/5～3/5 of a solid-liquid separation cylinder cubic capacity, and temperature of molten salt is 350 ℃～400 ℃.
Underpressure distillation in the described step (5) is made up of mechanical type vacuum pump, vacuum reservoir, control valve, vacuum meter, wherein pressure distribution is: reactor operating pressure-0.02 kilogram～-0.08 kilogram, the solid-liquid separation cylinder operating pressure is-0.02 kilogram～-0.08 kilogram, and visbreaking still operating pressure is-0.02 kilogram～0.08 kilogram.
The advantage that the present invention compared with prior art has is as follows:
1. owing to mix a certain proportion of polystyrene, saved complicated catalytic cracking unit, just can produce high-grade gasoline and diesel oil without catalyzer.
As everyone knows, plastic waste is a high molecular polymer, simple polyethylene or acrylic plastering, in thermal cracking process, the oil product that generates is based on straight-chain paraffin and alkene, if as gasoline products, its octane value is on the low side, if suitably mix a certain proportion of polystyrene plastic, will improve aromaticity content in the gasoline products, and then improved the octane value of gasoline, can produce automobile-used high-grade gasoline product, and for diesel product, straight-chain paraffin content height, cetane value is just high, approximate straight-run diesel oil product.Therefore, implement the present invention and can in a cover production equipment technical process, can produce qualified gasoline, two kinds of products of diesel oil fully.
2. do heat-conducting medium in the reactor with fused salt, thoroughly solved the plastic waste inequality of being heated in melting process, temperature or high or low influences the defective that the plastic cracking degree of depth and coking phenomenon are brought.
To utilize plastic waste to produce gasoline, diesel oil be the thermo-negative reaction plastics fully can oiling by heat absorption, and this process is an item change process.But the heat conductivility of plastics is relatively poor, given temperature or high or low, and the heating surface inequality all will be brought influence to plastics oiling or cracking severity.For solving this defective, the heat-conducting medium of the present invention in reacting kettle jacketing is fused salt.Fused salt is optimal heat-conducting medium, and has obtained widespread use at oil, chemical field, and it can the furnishing proportioning, and the heat conduction temperature is adjusted in 200 ℃～800 ℃, and turndown ratio is very big.Implement the present invention and do the heat-conducting medium scheme with fused salt, thoroughly solved with the straight heating surface inequality of being brought of burning of fire, temperature or high or low influences the defective that the plastic cracking degree of depth and coking phenomenon are brought.
3. be provided with inside and outside two helical ribbon agitator in the reactor of the present invention, the heat conductivility that has solved its material in the thermo-negative reaction of plastics oiling up hill and dale is relatively poor, and it is inhomogeneous easily to cause reaction mass to be heated, and cracking level is inconsistent, and with this defective of local coking.
The plastics oiling is thermo-negative reaction, but the heat conductivility of its material is relatively poor, and the time that reaches the thermally splitting temperature is longer, and it is inhomogeneous to cause reaction mass to be heated easily, and cracking level is inconsistent, and with local coking phenomenon.In order to solve this defective, the present invention is provided with inside and outside two helical ribbon agitator in reactor, outer ribbon turns clockwise, interior ribbon is rotated counterclockwise, it is when work, because inside and outside ribbon reverse direction rotation, formation laminar flow bump, turbulization, make plastics oil obtain abundant heat exchange, accelerated heating rate, outer ribbon and flute profile reactor inwall maintain 2mm～5mm at interval, outer ribbon can scrape off the coke that generates because of wall reaction when rotated at any time, has guaranteed fused salt heat-transfer effect in still thus.
4. adopt the visbreaking measure, reduced the viscosity of oil product, improved the yield of light oil of refinery, reduced the recycle stock ratio of rectifying tower.
The liquid viscosity that forms behind the plastic waste oiling is higher, and mobile poor, this kind material can cause the load of rectifying tower as rectifying tower distillatory basic material, produces a large amount of recycle stock, makes the oil refining cost up.In order to solve this defective, adopt other demulcent low temperature pyrolyzer modes such as visbreaking still, reduce the viscosity of oil product, improve the yield of light oil of refinery, reduce the recycle stock of rectifying tower.
5. plastics as not cleaning, have a certain amount of earth, sandstone etc. and mix in collection, letter sorting, fusion process, and this objectionable impurities can influence the operational cycle of reactor as not removing, and making it can not continuous production.For solving this difficult problem, the present invention adopts solid-liquid separation cylinder to play the effect of body refuses such as discharging earth, sandstone.
The present invention is according to organic and inorganic immiscible principle, and the different characteristic of various different substances proportions produces, high-temperature pump is the slag-drip opening by reactor continuously through pipeline, material in the reactor is driven in the solid-liquid separation cylinder, because oil and fused salt are immiscible, and oily proportion is lighter than the proportion of fused salt, thus oil just buoyance lift go out the fused salt liquid level, enter the reactor gaseous phase outlet by the outlet on the solid-liquid separation cylinder, enter in the reactor.Enter the residues such as earth, sandstone of solid-liquid separation cylinder, sink to the solid-liquid separation cylinder bottom because of proportion overweights fused salt, wait to deposit to when a certain amount of, screw extrusion press is just with its discharge.Begin it again, and earth, sandstone in the reactor just cement out, and have prolonged the operational cycle of reactor, make it continuous production.
6. the present invention is according to the boiling point of cut, and the principle that descends with the reduction of external pressure realizes, has implemented underpressure distillation in each link, has improved the dial-out rate of oil product, and then has improved the transformation efficiency of oil product, has saved the energy.
In a word, the present invention does not need complicated catalyst cracker, but continuous production, oil product transformation efficiency height, oil quality is good, and cost is low, save energy, thereby solved existing plastic waste and produced the defective that gasoline, diesel oil technology and equipment exist, the improvement of effectively controlling white pollution, be the method that a kind of reclamation of solid wastes is handled.
Description of drawings
Fig. 1 is for producing the structural representation of gasoline, diesel equipment among the present invention.
Embodiment
Embodiment 1
The first step, with plastic waste polyethylene, polypropylene, polystyrene in ratio fusion in 1: 1: 0.8, as 100 kilograms of polyethylene, 100 kilograms of polypropylene, 80 kilograms of polystyrene;
Second step, the plastic waste that fusion according to the above ratio is good has two helical ribbon agitators in advancing with hydraulic pusher, fused salt is housed as heating liquefaction cracking in the flute profile of heat-conducting medium chuck or the vertical response still outward, temperature of molten salt is 450 ℃, and heating liquefaction cracking temperature is 350 ℃ in the reactor;
The 3rd step, plastic waste in the reactor is through heating pyrolyze, and the material that reaction generates enters and carries out the viscosity breaking distillation in visbreaking still or other demulcent low temperature pyrolyzer devices, and the visbreaking temperature is 250 ℃, cracked gas forms liquid through condenser condenses, send rectifying tower to carry out rectifying;
The 4th step, simultaneously, plastics fusion liquid in the reactor is equipped with the solid-liquid separation cylinder of fused salt parting liquid in pump pumps into continuously, residue in the reactor, earth are effectively separated, residue, earth are discharged outside the cylinder by the screw extrusion press of solid-liquid separation cylinder bottom, and clean plastics fusion liquid returns in the reactor;
In finishing above steps, implement underpressure distillation, wherein the reactor operating pressure is about-0.04 kilogram～-0.06 kilogram, and the solid-liquid separation cylinder operating pressure is about-0.04 kilogram～-0.06 kilogram, and visbreaking still operating pressure is-0.04 kilogram～0.06 kilogram.
The first step, with plastic waste polyethylene, polystyrene in ratio fusion in 1: 0.4, as 100 kilograms of polyethylene, 40 kilograms of polystyrene;
Second step, the plastic waste that fusion according to the above ratio is good has two helical ribbon agitators in advancing with hydraulic pusher, and heating liquefaction cracking in reactor is housed outward in the flute profile or vertical response still of fused salt as the heat-conducting medium chuck, temperature of molten salt is 550 ℃, and the heating liquefaction temperature is 450 ℃ in the reactor;
The 3rd step, plastic waste in the reactor is through heating pyrolyze, and the material that reaction generates enters and carries out the viscosity breaking distillation in visbreaking still or other demulcent low temperature pyrolyzer devices, and the visbreaking temperature is 300 ℃, cracked gas forms liquid through condenser condenses, send rectifying tower to carry out rectifying;
The 4th step, simultaneously, plastics fusion liquid in the reactor is equipped with the solid-liquid separation cylinder of fused salt parting liquid in pump pumps into continuously, residue in the reactor, earth are effectively separated, residue, earth are discharged outside the cylinder by the screw extrusion press of cylinder bottom, and clean plastics fusion liquid returns in the reactor;
In finishing (2), (3), (4) step, implement underpressure distillation, wherein the reactor operating pressure is-0.04～-0.08 kilogram, and the solid-liquid separation cylinder operating pressure is-0.04～-0.08 kilogram, and visbreaking still operating pressure is-0.04～0.08 kilogram.
The first step, with thermoplastics type's plastic waste such as polypropylene, polystyrene in the fusion of 1: 0.4 ratio mix proportions, as 100 kilograms of polypropylene, 40 kilograms of polystyrene;
In second step, the plastic waste that fusion according to the above ratio is good has two helical ribbon agitators in advancing with hydraulic pusher, fused salt is housed as heating liquefaction in the reactor of heat-conducting medium chuck outward, and temperature of molten salt is 500 ℃, and the heating liquefaction temperature is 380 ℃ in the reactor,
In the 3rd step, the plastic waste in the reactor is through heating pyrolyze, and the material that reaction generates enters and carries out the viscosity breaking distillation in the visbreaking still, and the visbreaking temperature is 280 ℃, and cracked gas forms liquid through condenser condenses, send rectifying tower to carry out rectifying;
The 4th step, simultaneously, plastics fusion liquid in the reactor is equipped with the solid-liquid separation cylinder of fused salt parting liquid in pump pumps into continuously, residue in the reactor, earth are effectively separated, residue, earth are discharged outside the cylinder by the screw extrusion press of cylinder bottom, and clean plastics fusion liquid returns in the reactor;
In finishing (2), (3), (4) step, implement underpressure distillation, wherein the reactor operating pressure is-0.04～-0.08 kilogram, and the solid-liquid separation cylinder operating pressure is-0.04～-0.08 kilogram, and visbreaking still operating pressure is-0.04～0.08 kilogram.
Industrialization is produced gasoline with plastic waste in the various embodiments described above of the present invention, diesel equipment, comprise hydraulic feed machine 1, in two helical ribbon agitators 3 are arranged, the reactor 2 of fused salt heat-conducting medium chuck 4 is housed outward, visbreaking still 5, distillation tower 6, solid-liquid separation cylinder 7, screw extrusion press 8, high temperature slush pump 9, mixing oil condenser 10, mixing oil receives cylinder 11, vacuum reservoir 12, vacuum pump 13, rectifying tower 14, reboiler 15, gasoline condenser 16, gasoline receives cylinder 17, diesel oil condenser 18, diesel oil receives cylinder 19, volume pump 20 major equipments such as grade are formed, plastic waste need not clean after collecting, the simple earth of removing, sandstone, behind the bulk impurity such as metal, with polyethylene, polypropylene, polystyrene, or polyethylene, polystyrene, or polypropylene, polystyrene, in the ratio fusion of introducing in the inventive method, advance in flute profile or the vertical response still 2 by hydraulic feed machine 1, fusion under the temperature of negative pressure-0.02～0.08 kilogram pressure and 200 ℃～800 ℃, two helical ribbon agitators 3 rotate in the reactor 2 simultaneously, make material in reactor 2, accelerate the heat exchange cracking, cracked gas enters visbreaking still 5 by reactor 2 gaseous phase outlets, the kettle of visbreaking still 5 is horizontal round shape, vertically fire tube arrangement in the still, be provided with sedimentation tank at the bottom of the still, still center upper portion and distillation tower join, 250 ℃～300 ℃ of the temperature of visbreaking still 2,0.02～0.08 kilogram of pressure of negative pressure, the splitting gas that comes out from reactor 2 can produce polyreaction at circulation duct, form liquid state greater than the macromole hydrocarbon of 250 ℃～300 ℃ of boiling points and fall into visbreaking still 5, hydrocarbon gas less than 250 ℃～300 ℃ of boiling points enters mixing oil condenser 10 by distillation tower, condensation forms liquid and flows into mixing oil reception cylinder 11, mixed solution is squeezed into rectifying tower 14 through volume pump 20, rectifying tower 14 is under the effect of reboiler, cat head goes out gasoline, the gasoline hydrocarbon gas forms liquid by gasoline condenser 16 condensations and enters gasoline reception cylinder 17, the diesel oil hydrocarbon gas forms liquid through 18 condensations of diesel oil condenser and enters diesel oil reception cylinder 19 in the tower, heavy oil enters into solid-liquid separation cylinder 7 and gets back to reactor 2 cracking again at the bottom of the tower, solids constituent is a cone-shaped body from cylinder body 7, the outlet of cylinder upper end is connected with reactor 2 gaseous phase outlets, the lower end of cylinder is provided with screw extrusion press, cylinder body taper tangent line place establishes a material inlet, reactor 2 slag-drip openings are connected in series with solid-liquid separation cylinder 7 material inlets through pump, the loadings of the molten parting liquid of salt is 2/5～3/5 of a solid-liquid separation cylinder cubic capacity, and temperature of molten salt is 350 ℃～400 ℃.The plastics liquid that will have earth, sandstone that two helical ribbon agitators 3 in the reactor 2 do not stop in rotation is pushed slag-drip opening to, high temperature slush pump 9 is squeezed into plastics liquid in the solid-liquid separation cylinder, after the solid-liquid separation, clean plastics liquid returns in the reactor 2 by reactor 5 gaseous phase outlets, earth, sandstone through deposit a certain amount of after, discharge outside the cylinder by screw extrusion press.
Claims (10)
1, the industrialization method of producing gasoline, diesel oil with plastic waste, its feature comprises the following steps:
(1) with plastic waste polyethylene, polypropylene, polystyrene, or polyethylene, polystyrene, or polypropylene, polystyrene fusion in proportion;
(2) plastic waste that above-mentioned fusion is good has two helical ribbon agitators in advancing, and adorns in the reactor of fused salt heat-conducting medium chuck the heating cracking of liquefying outward;
(3) to the plastic waste in the reactor through heating pyrolyze, the material that reaction generates carries out viscosity breaking, cracked gas forms liquid through condensation, send rectifying tower to carry out rectifying;
(4) simultaneously, in constantly being pumped into, plastics fusion liquid in the reactor is equipped with in the solid-liquid separation cylinder of fused salt parting liquid, residue in the reactor, earth are effectively separated, residue, earth are discharged outside the cylinder by the screw extrusion press of solid-liquid separation cylinder bottom, and clean plastics fusion liquid returns in the reactor;
(5) in finishing (2), (3), (4) step, implement underpressure distillation.
2, the method for gasoline, diesel oil is produced in industrialization according to claim 1 with plastic waste, it is characterized in that: the mix proportions in the plastic waste in the described step (1) is a polyethylene: polypropylene: polystyrene is 0.8～1.2: 0.8～1.2: 0.7～0.9, or polyethylene: polystyrene is 0.8～1.2: 0.3～0.5, or polypropylene: polystyrene is 0.8～1.2: 0.3～0.5.
3, the method for gasoline, diesel oil is produced in industrialization according to claim 1 with plastic waste, it is characterized in that: the fusion preferred proportion in the plastic waste in the described step (1) is a polyethylene: polypropylene: polystyrene is 1: 1: 0.8, or polyethylene: polystyrene is 1: 0.4～0, or polypropylene: polystyrene is 1: 0.4.
4, the industrialization according to claim 1 method of producing gasoline, diesel oil with plastic waste, it is characterized in that: in the described step (2) two helical ribbon agitators are arranged, the reactor of adorning fused salt heat-conducting medium chuck outward is flute profile reactor or vertical response still.
5, the industrialization according to claim 1 method of producing gasoline, diesel oil with plastic waste, it is characterized in that: described temperature of molten salt is 200 ℃～800 ℃, preferred temperature is 450 ℃～550 ℃.
6, the industrialization according to claim 1 method of producing gasoline, diesel oil with plastic waste is characterized in that: the plastics heating liquefaction cracking temperature in the described step (2) is 350 ℃～400 ℃.
7, the method for gasoline, diesel oil is produced in industrialization according to claim 1 with plastic waste, it is characterized in that: the two helical ribbon agitators in the described step (2) are that outer ribbon turns clockwise, interior ribbon is rotated counterclockwise, and outer ribbon and reactor inwall are spaced apart two helical ribbon agitators of 2mm～5mm.
8, the method for gasoline, diesel oil is produced in industrialization according to claim 1 with plastic waste, it is characterized in that: the visbreaking mode in the described step (3) adopts visbreaking still or other demulcent low temperature pyrolyzer modes, wherein the visbreaking kettle is horizontal round shape, vertically fire tube arrangement in the still, be provided with sedimentation tank at the bottom of the still, still center upper portion and distillation tower join, and the visbreaking temperature of plastic liquid is 250 ℃～300 ℃ in the still.
9, the method for gasoline, diesel oil is produced in industrialization according to claim 1 with plastic waste, it is characterized in that: the solids constituent in the described step (4) is a cone-shaped body from cylinder body, the outlet of cylinder upper end is connected with the reactor gaseous phase outlet, the lower end of cylinder is provided with screw extrusion press, cylinder body taper tangent line place establishes a material inlet, the reactor slag-drip opening is connected in series with the solid-liquid separation cylinder material inlet through pump, and the loadings of the molten parting liquid of salt is 2/5～3/5 of a solid-liquid separation cylinder cubic capacity, and temperature of molten salt is 350 ℃～400 ℃.
10, the method for gasoline, diesel oil is produced in industrialization according to claim 1 with plastic waste, it is characterized in that: the pressure distribution of the underpressure distillation in the described step (5) is: reactor operating pressure-0.02 kilogram～-0.08 kilogram, the solid-liquid separation cylinder operating pressure is-0.02 kilogram～-0.08 kilogram, and visbreaking still operating pressure is-0.02 kilogram～0.08 kilogram.
Priority Applications (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB031346618A CN1223650C (en) | 2003-09-25 | 2003-09-25 | Industrial method of reusing waste plastics to produce gasoline and diesel oil |
| PCT/CN2004/001090 WO2005028593A1 (en) | 2003-09-25 | 2004-09-24 | A inductrialized process and a device for production of gasoline, diesel oil from waste plastics |
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| Application Number | Priority Date | Filing Date | Title |
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| CNB031346618A CN1223650C (en) | 2003-09-25 | 2003-09-25 | Industrial method of reusing waste plastics to produce gasoline and diesel oil |
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| CN1526793A true CN1526793A (en) | 2004-09-08 |
| CN1223650C CN1223650C (en) | 2005-10-19 |
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| WO2009023557A2 (en) * | 2007-08-10 | 2009-02-19 | Warren Vanderpool | Waste processing process |
| US9624439B2 (en) * | 2014-08-10 | 2017-04-18 | PK Clean Technologies | Conversion of polymer containing materials to petroleum products |
| PL3247775T3 (en) * | 2015-01-19 | 2020-12-14 | Bluealp Innovations B.V. | Method and system for transferring plastic waste into a fuel having properties of diesel/heating oil |
| IT201800009798A1 (en) | 2018-10-25 | 2020-04-25 | Proil Srl | PROCESS AND RELATIVE PLANT FOR THE DEPOLYMERIZATION OF PLASTIC MATERIALS FOR THE PRODUCTION OF HYDROCARBONS |
| CN115820281A (en) * | 2022-11-27 | 2023-03-21 | 吉林省秸源新能源科技有限公司 | A pre-reaction cauldron for production of living beings liquid fuel |
Family Cites Families (6)
| Publication number | Priority date | Publication date | Assignee | Title |
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| JPS5187584A (en) * | 1975-01-31 | 1976-07-31 | Japan Gasoline | Haipurasuchitsukuno netsubunkaisochi |
| JPS51126274A (en) * | 1975-04-26 | 1976-11-04 | Chisso Corp | Process for liquidizing plastic waste by making it melt |
| DE4329435C1 (en) * | 1993-09-01 | 1994-12-22 | Leuna Werke Gmbh | Process for the feedstock recycling of used plastics or used plastic mixtures |
| DE4400327A1 (en) * | 1994-01-07 | 1995-07-13 | Basf Ag | Method and device for producing liquid hydrocarbons from plastic waste of different compositions |
| CN2223297Y (en) * | 1995-08-18 | 1996-03-27 | 周鼎力 | Apparatus for producing gasoline diesel oil and carbon black from waste rubber |
| JP2002020763A (en) * | 2000-07-10 | 2002-01-23 | Yukawa Sangyo Kk | Waste plastic liquefaction apparatus and method of liquefying waste plastic using the same |
-
2003
- 2003-09-25 CN CNB031346618A patent/CN1223650C/en not_active Expired - Fee Related
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2004
- 2004-09-24 WO PCT/CN2004/001090 patent/WO2005028593A1/en active Application Filing
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| CN102746883A (en) * | 2011-04-22 | 2012-10-24 | 中国石油天然气股份有限公司 | Petroleum atmospheric and vacuum distillation process |
| CN102746896A (en) * | 2011-04-22 | 2012-10-24 | 中国石油天然气股份有限公司 | Heating method and device for hydrogenation feeding |
| CN102746883B (en) * | 2011-04-22 | 2014-10-15 | 中国石油天然气股份有限公司 | Petroleum atmospheric and vacuum distillation process |
| CN102746896B (en) * | 2011-04-22 | 2014-10-15 | 中国石油天然气股份有限公司 | Heating method and device for hydrogenation feeding |
| CN103627420A (en) * | 2013-12-05 | 2014-03-12 | 六盘水师范学院 | Method for improving coal and waste plastic co-liquefaction oil yield through two-stage treatment process |
| AU2017240574B2 (en) * | 2016-03-30 | 2020-03-05 | Brightmark Plastics Renewal Technologies Llc | Process, apparatus, controller and system for producing petroleum products |
| CN114540066A (en) * | 2020-11-25 | 2022-05-27 | 蓝星(北京)化工机械有限公司 | Waste plastic fast pyrolysis reactor |
| CN115106365A (en) * | 2022-06-28 | 2022-09-27 | 四川国纳科技有限公司 | Method and device for recycling degradable medical supplies |
| CN115106365B (en) * | 2022-06-28 | 2024-01-12 | 四川国纳科技有限公司 | Recovery method and recovery device for degradable medical supplies |
| WO2024037592A1 (en) * | 2022-08-17 | 2024-02-22 | 中国石油化工股份有限公司 | Plastic processing method and system |
Also Published As
| Publication number | Publication date |
|---|---|
| WO2005028593A1 (en) | 2005-03-31 |
| CN1223650C (en) | 2005-10-19 |
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