CN1246510A - Process and equipment for producing gasoline and diesel oil with waste plastics and/or heavy oil - Google Patents
Process and equipment for producing gasoline and diesel oil with waste plastics and/or heavy oil Download PDFInfo
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- CN1246510A CN1246510A CN99107968A CN99107968A CN1246510A CN 1246510 A CN1246510 A CN 1246510A CN 99107968 A CN99107968 A CN 99107968A CN 99107968 A CN99107968 A CN 99107968A CN 1246510 A CN1246510 A CN 1246510A
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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
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W30/00—Technologies for solid waste management
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- Y02W30/62—Plastics recycling; Rubber recycling
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Abstract
The present invention relates to a process and equipment for producing gasoline and diesel oil with used plastics and/or heavy oil. Said process includes directly mixing the raw materials with heat carrier to result in heat transfer and cracking reaction, thermal decomposing, catalytic cracking, and fractionation. A catalyst used in said process is disclosed. Said equipment is composed of extruder, screw reactor, combustion chamber, fixed bed, gasifying chamber, separator case, cyclone separator and hydrocarbon oil collector.
Description
The present invention relates to use plastic waste, high boiling hydrocarbon is produced the method and apparatus of lower boiling hydrocarbon ils.From plastic waste and heavy oil, produce the method and apparatus of gasoline, diesel especially by thermo-cracking and catalytic pyrolysis.
About with plastic waste and high boiling hydrocarbon being the existing a lot of reports of method of raw material production low boiling hydrocarbon, open flat 4-50929 (10) the spy, 7-166171 and 3-86790 and clear and 60-58485,63-132995, all adopt still formula [upright or for sleeping in] reactor to carry out heat scission reaction among 63-178195 and USP4851601 and the EP-A-0607862 (the application people is MAZDA MOTOR CORPORATION), the direct heat of still outer wall, still inwall material interruption is heated, still wall temperature difference is big, the still outer wall is subject to high temperature and burns out distortion, and the easy local superheating coking of still inwall influences conversion rate of products and equipment life, heat-transfer effect is poor, deslagging scarfing cinder difficulty.And fixed bed catalyst needs other heat supplied.This is to use tank reactor cracking organic high molecular compound and polyolefinic weakness now.Some extraordinary ranks uses helical reactors, belongs to indirect heat transfer equally, that is, the direct heat of cylinder body outer wall, storeroom is accepted heat in the tube, and heat transfer efficiency is poor.Particularly screw rod is subject to thermal bending deformation, causes the difficult sealing in screw rod two ends, and splitting gas is external in the tube lets out, and screw spiral is assemblied in circular barrel center, and the tube internal upper part does not have gasification space, and the influence reaction is carried out.What have reacts under vacuum and nitrogen protection condition.Traditional decompression delayed coking and the fluidized catalyzing method of the normal employing of black oil oil breaking, the steam consumption quantity height, investment is big, complicated operation.
The object of the invention will overcome above-mentioned shortcoming exactly, and the method and apparatus of producing gasoline, diesel from plastic waste and high boiling hydrocarbon is provided.Specifically, the inorganic particulate thermal barrier is entered in the helical reactors and raw material direct contact heat transfer generation thermally splitting continuously circularly, the gas phase hydrocarbon of generation is gone into fixed bed generation catalyzed reaction, and plastic waste and high boiling hydrocarbon are changed into gasoline, diesel.The present invention has reaction and conducts heat soon, and power consumption is few, equipment noncoking, oil-containing not in the slag, the characteristics of the high and less investment of finished product transformation efficiency.
The present invention be following be to realize.
Method of the present invention comprises: earlier thermal barrier heating flame in the combustion chamber is risen to high temperature, send in the flute profile helical reactors with worm conveyor.Described plastic waste is clamp-oned in the flute profile helical reactors of (or go into the black oil oil pump) sealing, and directly mixed the generation heat cracking reaction, resolve into gas phase hydrocarbon and residue with thermal barrier.The gas phase hydrocarbon enters fixed bed generation catalyzed reaction and generates small molecules gas phase hydrocarbon, collects the gas phase hydrocarbon by traditional method and obtains gasoline, diesel.The mixture that inorganic thermal barrier and cracked residue form is subjected to screw rod to promote to flow into vaporizer, enters separator box through worm conveyor.With gas blower high-temperature flue gas is sent into separator box, ceaselessly mixture is blown in the cyclonic separator, collect solid mixture, isolate gas.With worm conveyor above-mentioned solid mixture being sent into the combustion chamber burns.In the combustion chamber, the organism in the mixture is burned clean, and the inorganic particulate hot body is heated to high temperature again and falls into circularly gives the reactor heat supply in the channel reactor.In the said process, the continuous recurrent state of heating that thermal barrier is in heating all the time---heat release---is to guarantee that enough heats are arranged in the channel reactor.
In the aforesaid method, heat scission reaction and catalytic cracking reaction can be kept normal pressure or be higher than normal pressure, and catalytic cracking reaction is to carry out on the catalytic fixed bed that places vaporizer inside, and catalyzed reaction institute heat requirement is supplied with by high-temperature gasification chamber interior heat.Catalyst system therefor is a DL-1 type catalyzer.
Equipment of the present invention mainly comprises extruding machine, flute profile helical reactors, combustion chamber, vaporizer, separator box, cyclonic separator and hydrocarbon ils collection device.Described channel reactor comprises; The elongated cylindrical housing fixes on the ground motionless.Lower housing portion is semicircle and disposes the screw rod agitator that the intravital screw rod agitator of shell drives with electromagnetic motor.Extruding machine and heat-carrier inlet are configured in flute profile helical reactors top one end, and vaporizer is configured in the other end.Fixed bed, its arranged perpendicular communicates with the gas-phase product outlet of reactor in the vaporizer inner and upper, and the separator box bottom is connected with the bottom of vaporizer through worm conveyor, and the top of separator box is connected with the cyclonic separator middle part by pipeline.The cyclonic separator bottom communicates with the top of combustion chamber through worm conveyor.Described combustion chamber includes oily vapour burner and air nozzle.The bottom, combustion chamber connects the top of material-storage jar, and the bottom of material-storage jar communicates with flute profile helical reactors top through worm conveyor.
Equipment of the present invention further comprises the hydrocarbon ils fractionation plant, all belongs to the conventional gasoline, diesel tripping device that uses in this area, comprising: separation column, condenser, water-and-oil separator and water-sealed tank etc.
Brief description of drawings
Figure one is an equipment flowsheet of the present invention:
The present invention is auspicious to be stated:
One of purpose of the present invention provides a kind of with waste plastics and or heavy oil production gasoline The method and apparatus of diesel oil. Comprise: earlier with inorganic granule heat carrier in the combustion chamber In rise to high temperature with fuel oil (or imflammable gas) combustion heating, use again spiral The conveyer continuous circulation is ceaselessly delivered to high-temperature heat carrier in the flute profile helical reactors. With spiral (or reciprocating type) extruding machine described waste plastics is pushed and (maybe will weigh Dregs of fat oil pump enters) in the flute profile helical reactors of sealing, and directly and heat carrier exist Mixed occurrence conducts heat and carries out heat cracking reaction in the reactor, and material rotates at screw rod With promote lower in the reactor feeding mouth one end shift to the other end, raw material constantly divides Solution becomes gas phase hydrocarbon and residue. It is anti-that the gas phase hydrocarbon enters fixed bed generation catalysis through vaporizer Should generate little molecule gas phase hydrocarbon, little molecule gas phase hydrocarbon is through the fractionating column fractionation, again by passing The collection method of purification of system obtains gasoline, diesel. Inorganic fine granularity heat carrier and splitting The mixture of separating residue formation is subjected to screw rod to promote to flow into vaporizer, through conveying worm Enter separator box. With air blast inspiration high-temperature flue gas and send into separator box, do not stop Ground is blown into mixture in the cyclone separator from separator box, collect solid mixture, Contain inorganic grit in the isolated gas, discharger behind cyclone dust collectors. With conveying worm above-mentioned solid mixture is sent into the combustion chamber. In the combustion chamber, Organic matter in the mixture is burned clean, and inorganic grit is discharged with high-temperature flue gas, does not have Machine graininess heat carrier is heated to again high temperature and falls into material-storage jar, through helical feed The channel reactor of sending into of machine continuous circulation is given the reactor heat supply.
In the said process, the company of heating that heat carrier is in heating all the time---heat release---Continuous recurrent state, that is, heat carrier is heat temperature raising in the combustion chamber---spiral response Heat release cooling in the device---the process of heat temperature raising in the combustion chamber again. To guarantee groove Enough heats are arranged in the shaped reaction device.
In the said method, heat scission reaction and catalytic cracking reaction can be kept normal pressure or height In normal pressure, heat carrier is discharged from the combustion chamber and the temperature control when entering helical reactors Built in 500-1000 ℃, be preferably in 600-700 ℃. Heat carrier leaves spiral reverse Temperature when answering device is controlled at 400-800 ℃, is preferably in 500-600 ℃, urges Changing cracking reaction is to carry out catalysis in the catalytic fixed bed that places vaporizer inside Reaction institute calorific requirement is supplied with by high-temperature gasification chamber interior heat, and the catalytic reaction temperature is 300-600 ℃, be preferably in 300-450 ℃, catalyst system therefor is the DL-1 type Catalyst, its composition (weight) comprising: (be trade name, China is neat for CHO-1 The Shandong petrochemical plant is produced) 8%, REY24%, modenite (the sial aluminum ratio is 12: 1) Be 25% and ZSM-5 catalyst 43%. Can be used for after each component fully mixed The present invention. Heat carrier can be selected granule sand and particulate Si hydrochlorate and or carbonic acid Salt compound and other hard inorganic salts. Such as alumina silicate, the diameter of particle generally exists 0,1-3 millimeter is preferably in 0,5-2,0 millimeter. It is former that available the present invention processes Material also comprises: crude oil, residual oil, organic house refuse and other organic high sub-chemical combination Thing.
Particularly, method of the present invention comprises step:
1, be 0,1 with diameter earlier---3 millimeters graininess silicic acid aluminium is as heat carrier In the combustion chamber, rise with fuel oil (or reclaiming cracked gas) and air burning heating Temperature falls into conservation tank after 500-1000 ℃, follow continuously with conveying worm again Ring is ceaselessly delivered to heat carrier in the flute profile helical reactors.
2, with spiral (or reciprocating type) extruding machine described plastic waste is pushed in the flute profile helical reactors of (or go into the black oil oil pump) sealing, and directly in reactor, mix the generation heat transfer and carry out heat cracking reaction with thermal barrier, material in screw rod rotation with under promoting material hand-hole one end in the flute profile helical reactors shift to the other end, constantly resolve into gas phase hydrocarbon and residue after raw material is heated.The gas phase hydrocarbon enters catalyzed reaction generation small molecules gas phase hydrocarbon takes place in the interior fixed bed of vaporizer, and small molecules gas phase hydrocarbon obtains gasoline, diesel by traditional collection method of purification again through the separation column fractionation.
3, the mixture that inorganic thermal barrier and thermo-cracking residue are formed is subjected to the screw rod of reactor to promote to flow into the vaporizer bottom, enters separator box through worm conveyor.With gas blower inspiration high-temperature flue gas and send into separator box, ceaselessly said mixture is blown in the cyclonic separator from separator box.Metal, stone etc. fall into separated the removing in separator box bottom, and the solid mixture that cyclonic separator is collected falls into storage tank, and isolated gas contains inorganic grit, discharger after fly-ash separator separates.
4, with worm conveyor the solid mixture in the storage tank is pushed the combustion chamber.In the combustion chamber, organism in the mixture is burned clean, inorganic grit is discharged with high-temperature flue gas, and the inorganic particulate thermal barrier is heated to high temperature again and falls into material-storage jar, sends into the flute profile helical reactors through the continuous round-robin of worm conveyor and puies forward arch heat for the scission reaction in the reactor.
In the said process, thermal barrier is in all the time and is heated---heat release---heated continuous circulation shape.To guarantee that enough heats are arranged in the channel reactor.
Another object of the present invention provides the equipment of realizing aforesaid method, and equipment of the present invention mainly comprises extruding machine, the flute profile helical reactors, and the combustion chamber, vaporizer,
Separator box, cyclonic separator and hydrocarbon ils collection device.Described flute profile helical reactors comprises; The elongated cylindrical housing fixes on the ground motionless.Lower housing portion is semicircle and disposes the screw rod agitator, accepts peripheral magnetic electromotor between the intravital screw rod agitator of shell and drives, and the intravital material of shell does not have any leakage.Extruding machine and heat-carrier inlet are configured in channel reactor top one end respectively.Vaporizer is configured in the channel reactor the other end.Fixed bed, its arranged perpendicular are in the vaporizer inner and upper, and its import communicates with the gas-phase product outlet of channel reactor, and its outlet connects separation column.The bottom of vaporizer is connected by spiral conveyer with the separator box middle part.The bottom of separator box is a storage tank, collects scrap metal and stone etc.The top of separator box is connected with the cyclonic separator middle part by pipeline.Cyclonic separator top connects tornado dust collector, and the cyclonic separator bottom connects storage tank top, and the storage tank bottom communicates through worm conveyor and with the top of combustion chamber.Described combustion chamber includes oily vapour burner and air nozzle.The bottom, combustion chamber connects the top of material-storage jar, and the bottom of material-storage jar communicates with flute profile helical reactors top through worm conveyor.
Equipment of the present invention further comprises the hydrocarbon ils fractionation plant, all belongs to the conventional gasoline, diesel tripping device that uses in this area, comprising: separation column, condenser, water-and-oil separator and water-sealed tank etc.
Below in conjunction with accompanying drawing equipment of the present invention is further described.
Referring to figure one, equipment of the present invention mainly comprises extruding machine (3), flute profile spiral shell
Revolve reactor (21), combustion chamber (5), vaporizer (22), separator box (25), cyclonic separator (11), separation column (28), condenser (29,33), water-and-oil separator (30,38) and water-sealed tank (31) etc.Described flute profile helical reactors (21) comprises; Elongated cylindrical housing (21) fixes on the ground motionless.Housing (21) bottom is semicircle and disposes screw rod agitator (3) that channel reactor (21) top is vaporization space.Accepting peripheral magnetic electromotor (1,19) between the screw rod agitator (3) in the housing (21) drives.Screw rod agitator (3) one ends support with circular baffle plate (20) and separate with magnetic electromotor (19), and the other end is had the cross steelframe support fixation of circular hole (36) by the center.Housing (21) internal screw agitator (3) has any to external leakage because of the indirect driving that is subjected to extraneous magnetic force can not cause the material in the housing (21) because of the rotation of screw rod.Between extruding machine (2) and the flute profile helical reactors (21) valve (17) is housed.Extruding machine (2) and thermal barrier (4) inlet are configured in flute profile helical reactors (21) top one end respectively.Vaporizer (22) is configured in channel reactor (21) the other end.Fixed bed (23), its arranged perpendicular are in vaporizer (22) inner and upper, and its import communicates with the gas-phase product outlet of flute profile helical reactors (21), and its outlet connects separation column (28).The bottom of vaporizer (22) is connected by spiral conveyer (3) with separator box (25) middle part.The bottom of separator box (25) is storage tank (26), collects scrap metal and stone etc.The top of separator box (25) is connected with cyclonic separator (11) middle part by pipeline.Cyclonic separator (11) top connects tornado dust collector (13), and cyclonic separator (11) bottom connects storage tank (5) top, and storage tank (5) bottom communicates through worm conveyor (3) and with the top of combustion chamber (9).Described combustion chamber (9) includes oil firing mouth (8), vapour burner (6) and air nozzle (7).Bottom, combustion chamber (9) connects the top of material-storage jar (5), and the bottom of material-storage jar (5) communicates with flute profile helical reactors (21) top through worm conveyor (3).Separation column (28) top connects gasoline condenser (29) import, condenser (29) outlet connects gasoline water-and-oil separator (30) top, water-and-oil separator (30) top communicates with water-sealed tank (31), and water-sealed tank (31) top is connected with the combustion vapour nozzle (6) of combustion chamber (9).Water-and-oil separator (30) bottom connects gasoline tank (35).Stripping jar (32) is equipped with at separation column (28) middle part.Stripping jar (32) connects diesel oil condenser (33) import.Condenser (33) outlet connects diesel oil water-and-oil separator (38) top, and oily water separation separator (38) bottom connects diesel oil tank (34).
Below in conjunction with accompanying drawing method of the present invention is further detailed.
Is 0 with diameter earlier, the particulate state silicic acid aluminium of 1-3 millimeter is packed into (5) in the storage tank as thermal barrier (4), with pushing in the combustion chamber (9) of spiral conveyer (3) constant speed.With oil fuel (or reclaim cracking tail gas) and air through separately nozzle (6,7,8,) spray into simultaneously in the combustion chamber (9), thermal barrier (4) is heated in combustion chamber (9) and rises to 500-1000 ℃ and fall into conservation tank (5), use again worm conveyor (3) continuously circulation ceaselessly thermal barrier (4) is delivered in the flute profile helical reactors (21).Described plastic waste is pushed or heavy oil is pumped in the flute profile helical reactors (21) of sealing through hand-hole (18) with spiral (or reciprocating type) extruding machine (2), and direct and living heat transfer of thermal barrier (4) hybrid concurrency in flute profile helical reactors (21), carry out heat cracking reaction.Material in screw rod (3) rotation with under promoting in the reactor (21) end shift to the other end.After being heated, raw material constantly resolves into gas phase hydrocarbon and residue.In the fixed bed (23) of gas phase hydrocarbon in vaporizing zone enters vaporizer (22), and generate small molecules gas phase hydrocarbon with DL-1 type catalyzer generation catalyzed reaction, small molecules gas phase hydrocarbon obtains gasoline, diesel by traditional collection method of purification again through separation column (28) fractionation.The mixture (16) that thermal barrier (4) and thermo-cracking residue are formed is subjected to the screw rod (3) of reactor (21) to promote to flow into vaporizer (22) bottom, enters separator box (25) through worm conveyor (3).Send into separator box (25) with gas blower (27) inspiration high-temperature flue gas through hand-hole (39), ceaselessly said mixture (16) is blown in the cyclonic separator (11) from separator box (25).Metal, stone etc. fall into separator box (25) bottom (26) are separated through the hole to be removed, and the solid mixture (16) that cyclonic separator (11) is collected falls into storage tank (5).Isolated gas contains the inorganic grit that raw material is brought into, after fly-ash separator (13) separates from ash storage box (14) through the hole (15) discharger.With worm conveyor (3) solid mixture (16) in the storage tank (5) is pushed combustion chamber (9).(9) lining in the combustion chamber, the organism in the mixture (16) is by burning out, and inorganic grit is taken away with high-temperature flue gas.Thermal barrier (4) is heated to 500-1000 ℃ and fall into material-storage jar (5) again, through worm conveyor (3) continuously round-robin send into flute profile helical reactors (21) and give reaction heat supply in the reactor.
In the said process, thermal barrier (4) is in all the time and is heated---heat release---heated continuous circulation shape.Purpose is the scission reaction institute heat requirement of guaranteeing in the flute profile helical reactors (21).
Below illustrate in greater detail the present invention by specific embodiment, but the present invention is not limited.
Embodiment
The particulate state silicic acid aluminium that earlier with the 2000KG diameter is 0,9 millimeter is packed into (5) in the storage tank as thermal barrier (4), with pushing in the combustion chamber (9) of spiral conveyer (3) constant speed.With No. 0 diesel oil (or reclaiming cracking tail gas) and air through separately nozzle (6,7,8,) spray into simultaneously in the combustion chamber (9) and burn, thermal barrier (4) is heated in combustion chamber (9) and is warmed up to 600-700 ℃, and fall into conservation tank (5), use worm conveyor (3) to circulate continuously again and ceaselessly thermal barrier (4) is delivered in the flute profile helical reactors (21).With spiral (or reciprocating type) extruding machine (2) with 1400KG Beijing plastic waste (PP25% in winter, PS25%, PE50%) push in the flute profile helical reactors (21) of sealing, and direct and living heat transfer of thermal barrier (4) hybrid concurrency in flute profile helical reactors (21), carry out heat cracking reaction.Plastic waste is shifted to the other end that connects vaporizing chamber from material inlet one end of reactor (21) under screw rod (3) promotes.The material inlet temperature of reactor is controlled at 600-700 ℃, and the residue temperature out of reactor is controlled at 500-600 ℃.After being heated, plastic waste constantly resolves into gas phase hydrocarbon and residue.In the fixed bed (23) of gas phase hydrocarbon in vaporizing zone enters vaporizer (22), and with fixed bed (23) in DL-1 type catalyzer generation catalyzed reaction.The catalyzed reaction temperature is controlled at 300-400 ℃.Generate small molecules gas phase hydrocarbon, small molecules gas phase hydrocarbon obtains gasoline, diesel by traditional collection method of purification more at last through separation column (28) fractionation.The mixture (16) that thermal barrier (4) and thermo-cracking residue are formed is subjected to the screw rod (3) of reactor (21) to promote to flow into vaporizer (22) bottom, enters separator box (25) through worm conveyor (3).All gas blower (27) inspiration high-temperature flue gas are sent into separator box (25) through hand-hole (39), ceaselessly said mixture (16) are blown in the cyclonic separator (11) from separator box (25).The metal that contains in the plastic waste, stone etc. fall into separator box (25) bottom (26) are separated through the hole to be removed, and the solid mixture (16) that cyclonic separator (11) is collected falls into storage tank (5).Isolated gas contains the inorganic grit that plastic waste is brought into, after fly-ash separator (13) separates from ash storage box (14) through the hole (15) discharger.With worm conveyor (3) solid mixture (16) in the storage tank (5) is pushed combustion chamber (9).(9) lining in the combustion chamber contains oil residue by burning out in the mixture (16), and inorganic grit is taken away with high-temperature flue gas.Burned again the 600-700 of being heated to ℃ and fall into material-storage jar (5) of thermal barrier (4), through worm conveyor (3) continuously round-robin send into flute profile helical reactors (21) in to the plastic waste heat supply in the reactor.
In the aforesaid method, thermal barrier (4) is in all the time and is heated in---heat release---heated continuous cycle operation process.To guarantee the required enough heats of scission reaction in the flute profile helical reactors (21).In the production, must the supplemental heat carrier in the equipment, unless need be replenished by normal wear.Above-mentioned processing parameter and production result are as follows: plastic waste (W%): 1400KG.Wherein, PP is 350KG (25%),
PS is 350KG (25%), and PE is 700KG (50%).Reaction pressure: 0,05--0, the 1MPA thermal barrier advances temperature of reactor: 600-700 ℃ of thermal barrier goes out temperature of reactor: 500-600 ℃.Catalyzed reaction temperature: 300-350 ℃ catalyzer: DL-1 type catalyzer.Reaction product: gasoline, 630KG (40%) RON is 93,5.
Gasoline component (weight %): alkane is 19,9%, and naphthenic hydrocarbon is 12%,
Rare hydrocarbon is 48%, and aromatic hydrocarbons is 9,9%,
Other is 10,2%.
Diesel oil: 420KG (35%), cetane value is 52.
Diesel oil component (weight %): alkane is 15%, and naphthenic hydrocarbon is 8%,
Rare hydrocarbon is 55%, aromatic hydrocarbons 10%, and other is 12%
Inorganic residues: 140KG (10%).
Inflammable gas: 210KG (15%) turns back in the combustion chamber and burns.
Claims (12)
1, a kind of with plastic waste and or the heavy oil method of producing gasoline, diesel.Comprise: first inorganic thermal barrier is heated in the combustion chamber rises to high temperature, sends in the flute profile helical reactors with worm conveyor again.Described plastic waste clamp-oned and or the black oil oil pump is gone in the flute profile helical reactors of sealing, allow raw material and thermal barrier directly mix and take place to conduct heat and cracking reaction, decompose generation gas phase hydrocarbon and residue.The gas phase hydrocarbon generates small molecules gas phase hydrocarbon through fixed bed generation catalyzed reaction, and enters the separation column fractionation.The mixture that inorganic thermal barrier and cracked residue form is subjected to screw rod to promote to flow into vaporizer, enters separator box through worm conveyor.With gas blower high-temperature flue gas is sent into separator box, ceaselessly mixture is blown in the cyclonic separator, collect solid mixture, isolate gas.With worm conveyor above-mentioned solid mixture being sent into the combustion chamber burns.In the combustion chamber, the organism in the mixture is burned clean, and inorganic thermal barrier is heated to high temperature again, and falls in the channel reactor to the scission reaction heat supply.It is characterized in that raw material and thermal barrier directly mix generation and conduct heat and cracking reaction the continuous recurrent state of heating that thermal barrier is in heating all the time---heat release---.
2, according to the method for claim 1, it is characterized in that taking place in the described fixed bed catalyzed reaction institute heat requirement and supply with by vaporizing chamber and flute profile helical reactors internal heat.
3, according to the method for claim 1, it is characterized in that described catalyzer is a DL-1 type catalyzer.
4, according to the method for claim 3, it is characterized in that described its composition of DL-1 type catalyzer (weight) comprising: CHO-1 (for trade(brand)name, Chinese Qilu Petrochemical factory produces) 8%, REY24%, mordenite (silica alumina ratio is 12: 1) are 25% and ZSM-5 catalyzer 43%.Each component carried out behind the thorough mixing.
5, according to the method for claim 1, it is characterized in that described heat scission reaction and catalytic cracking reaction can keep normal pressure or be higher than normal pressure.
6, according to the method for claim 1, it is characterized in that accepting between the spiral stirrer in the described flute profile helical reactors driving of extraneous magnetic electromotor.
7, according to the method for claim 1, it is characterized in that described thermal barrier belongs to oxygen silicon, as sand and silicate, the mineral compound that carbonate is formed is as pure aluminium silicate etc.Its particle diameter is 0, the 1-5 millimeter.
8, according to the method for claim 1, it is characterized in that described thermal barrier is 500-1000 ℃ in combustor exit to flute profile helical reactors inlet temperature.Temperature when thermal barrier leaves the spiral channel reactor is 400-800 ℃.
9, according to the method for claim 1, further comprise the step of collecting the hydrocarbon ils behind the separation column.
10, a kind of with plastic waste and or heavy oil produce the equipment of gasoline, diesel.Mainly comprise extruding machine, flute profile helical reactors, combustion chamber, fixed bed, vaporizer, separator box, cyclonic separator and hydrocarbon ils collection device.Described flute profile helical reactors comprises; The elongated cylindrical housing fixes on the ground motionless.Lower housing portion is semicircle interior configuration screw rod agitator, accepts extraneous magnetic electromotor between the screw rod agitator and drives.Extruding machine and heat-carrier inlet are configured in feed(raw material)inlet one end on flute profile helical reactors top, and vaporizer is configured in the other end.Fixed bed, its arranged perpendicular communicates with the gas-phase product outlet of flute profile helical reactors in the vaporizer inner and upper.The fixed bed outlet connects the hydrocarbon ils collection device.The bottom of vaporizer is connected with the separator box middle part through worm conveyor.The top of separator box is connected with the cyclonic separator middle part by the outlet conduit of gas blower.The cyclonic separator bottom communicates with the top of combustion chamber through worm conveyor.The top tail gas outlet of combustion chamber connects blower inlet.Described combustion chamber includes oily vapour burner and air nozzle.The bottom, combustion chamber connects the top of material-storage jar, and the material-storage jar bottom communicates with heat-carrier inlet on the flute profile helical reactors through worm conveyor.
11, according to claim 10 described equipment, it is characterized in that the hydrocarbon ils collection device all belongs to the conventional gasoline, diesel tripping device that uses in this area, comprising: separation column, condenser, water-and-oil separator and water-sealed tank etc.
12, according to claim 10 described equipment, it is characterized in that accepting between the screw rod agitator in the described flute profile helical reactors extraneous magnetic electromotor and drive.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN99107968A CN1074447C (en) | 1999-06-08 | 1999-06-08 | Process and equipment for producing gasoline and diesel oil with waste plastics and/or heavy oil |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN99107968A CN1074447C (en) | 1999-06-08 | 1999-06-08 | Process and equipment for producing gasoline and diesel oil with waste plastics and/or heavy oil |
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| Publication Number | Publication Date |
|---|---|
| CN1246510A true CN1246510A (en) | 2000-03-08 |
| CN1074447C CN1074447C (en) | 2001-11-07 |
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| Application Number | Title | Priority Date | Filing Date |
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| CN99107968A Expired - Fee Related CN1074447C (en) | 1999-06-08 | 1999-06-08 | Process and equipment for producing gasoline and diesel oil with waste plastics and/or heavy oil |
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| WO2003010258A1 (en) * | 2001-07-23 | 2003-02-06 | Yuanmo Zhang | A process and an apparatus for producing gasoline and diesel oil from plastic waste and/or heavy oil |
| WO2008131600A1 (en) * | 2007-04-28 | 2008-11-06 | Bin Niu | A process and a device for continuous cracking waste plastics |
| CN101074385B (en) * | 2007-04-28 | 2010-09-15 | 牛斌 | Waste-plastic continuous cracking process and cracker |
| CN101864086B (en) * | 2010-02-12 | 2012-01-04 | 泰兴汤臣压克力有限公司 | Waste organic glass continuous cracking device |
| CN102382668A (en) * | 2010-09-01 | 2012-03-21 | 中国石油化工股份有限公司 | Coal cracking and heavy oil cracking joint production method |
| CN102382669A (en) * | 2010-09-01 | 2012-03-21 | 中国石油化工股份有限公司 | Coal cracking and heavy oil cracking joint production method |
| CN102618323A (en) * | 2011-01-27 | 2012-08-01 | 中国石油化工股份有限公司 | Heavy oil raw material processing method for improving liquid product yield |
| CN102949957A (en) * | 2011-08-26 | 2013-03-06 | 北京低碳清洁能源研究所 | Catalytic heat carrier for pyrolysis of carbonaceous material and preparation method thereof |
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| CN1075328A (en) * | 1992-02-12 | 1993-08-18 | 赵太平 | The method and apparatus of plastic waste continuous production petroleum products |
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| CN1068032C (en) * | 1998-08-27 | 2001-07-04 | 邢力 | Hydrocarbon preparing method and equipment using household refuse and/or organic waste |
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