CN2408118Y - Equipment for producing gasoline and diesel oil by using waste plaste and/or heavy oil - Google Patents
Equipment for producing gasoline and diesel oil by using waste plaste and/or heavy oil Download PDFInfo
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- CN2408118Y CN2408118Y CN99216787U CN99216787U CN2408118Y CN 2408118 Y CN2408118 Y CN 2408118Y CN 99216787 U CN99216787 U CN 99216787U CN 99216787 U CN99216787 U CN 99216787U CN 2408118 Y CN2408118 Y CN 2408118Y
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- oil
- combustion chamber
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- 239000003502 gasoline Substances 0.000 title claims abstract description 19
- 239000000295 fuel oil Substances 0.000 title claims abstract description 8
- 239000002283 diesel fuel Substances 0.000 title abstract description 10
- 239000002699 waste material Substances 0.000 title abstract 2
- 238000002485 combustion reaction Methods 0.000 claims abstract description 29
- 229930195733 hydrocarbon Natural products 0.000 claims abstract description 24
- 150000002430 hydrocarbons Chemical class 0.000 claims abstract description 24
- 239000004215 Carbon black (E152) Substances 0.000 claims abstract description 23
- 239000003921 oil Substances 0.000 claims abstract description 22
- 238000000926 separation method Methods 0.000 claims abstract description 15
- 230000008016 vaporization Effects 0.000 claims abstract description 8
- 230000004888 barrier function Effects 0.000 claims description 24
- 238000003860 storage Methods 0.000 claims description 23
- 239000013502 plastic waste Substances 0.000 claims description 16
- 239000006200 vaporizer Substances 0.000 claims description 15
- 239000000463 material Substances 0.000 claims description 8
- 230000008676 import Effects 0.000 claims description 6
- 239000007921 spray Substances 0.000 claims description 5
- 239000004575 stone Substances 0.000 claims description 5
- 239000000428 dust Substances 0.000 claims description 3
- 230000002093 peripheral effect Effects 0.000 claims description 3
- 239000003923 scrap metal Substances 0.000 claims description 3
- 238000009834 vaporization Methods 0.000 claims description 3
- 238000010304 firing Methods 0.000 claims description 2
- 238000006243 chemical reaction Methods 0.000 abstract description 12
- 238000004939 coking Methods 0.000 abstract description 3
- 239000002893 slag Substances 0.000 abstract description 2
- 239000004033 plastic Substances 0.000 abstract 2
- 229920003023 plastic Polymers 0.000 abstract 2
- 238000005265 energy consumption Methods 0.000 abstract 1
- 239000007789 gas Substances 0.000 description 18
- 238000005336 cracking Methods 0.000 description 8
- 238000009835 boiling Methods 0.000 description 6
- 238000000034 method Methods 0.000 description 6
- 239000000203 mixture Substances 0.000 description 6
- 239000002956 ash Substances 0.000 description 5
- 238000006555 catalytic reaction Methods 0.000 description 5
- 239000008247 solid mixture Substances 0.000 description 5
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 4
- 238000010504 bond cleavage reaction Methods 0.000 description 4
- 239000003546 flue gas Substances 0.000 description 4
- 238000004519 manufacturing process Methods 0.000 description 4
- 239000000047 product Substances 0.000 description 4
- 230000007017 scission Effects 0.000 description 4
- 150000003384 small molecules Chemical class 0.000 description 4
- 239000010881 fly ash Substances 0.000 description 3
- 238000005194 fractionation Methods 0.000 description 3
- 239000002994 raw material Substances 0.000 description 3
- 238000007789 sealing Methods 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- 150000001335 aliphatic alkanes Chemical class 0.000 description 2
- 150000004945 aromatic hydrocarbons Chemical class 0.000 description 2
- 239000000446 fuel Substances 0.000 description 2
- 229910052751 metal Inorganic materials 0.000 description 2
- 239000002184 metal Substances 0.000 description 2
- 238000000746 purification Methods 0.000 description 2
- 239000005995 Aluminium silicate Substances 0.000 description 1
- CIWBSHSKHKDKBQ-JLAZNSOCSA-N Ascorbic acid Chemical compound OC[C@H](O)[C@H]1OC(=O)C(O)=C1O CIWBSHSKHKDKBQ-JLAZNSOCSA-N 0.000 description 1
- 239000004411 aluminium Substances 0.000 description 1
- 229910052782 aluminium Inorganic materials 0.000 description 1
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 description 1
- PZZYQPZGQPZBDN-UHFFFAOYSA-N aluminium silicate Chemical compound O=[Al]O[Si](=O)O[Al]=O PZZYQPZGQPZBDN-UHFFFAOYSA-N 0.000 description 1
- 235000012211 aluminium silicate Nutrition 0.000 description 1
- 229910000323 aluminium silicate Inorganic materials 0.000 description 1
- 238000005452 bending Methods 0.000 description 1
- 239000003054 catalyst Substances 0.000 description 1
- 238000007233 catalytic pyrolysis Methods 0.000 description 1
- 239000007795 chemical reaction product Substances 0.000 description 1
- 239000003818 cinder Substances 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 230000006837 decompression Effects 0.000 description 1
- 230000003111 delayed effect Effects 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000002309 gasification Methods 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 230000001737 promoting effect Effects 0.000 description 1
- 230000000306 recurrent effect Effects 0.000 description 1
- RMAQACBXLXPBSY-UHFFFAOYSA-N silicic acid Chemical compound O[Si](O)(O)O RMAQACBXLXPBSY-UHFFFAOYSA-N 0.000 description 1
- 235000012239 silicon dioxide Nutrition 0.000 description 1
- 239000007858 starting material Substances 0.000 description 1
- 230000000153 supplemental effect Effects 0.000 description 1
- 230000009466 transformation Effects 0.000 description 1
- 238000013022 venting Methods 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G11/00—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
- C10G11/02—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils characterised by the catalyst used
-
- 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
- C10G1/08—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal with moving catalysts
-
- 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
Landscapes
- Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Life Sciences & Earth Sciences (AREA)
- Wood Science & Technology (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
- Separation, Recovery Or Treatment Of Waste Materials Containing Plastics (AREA)
- Catalysts (AREA)
- Liquid Carbonaceous Fuels (AREA)
Abstract
The utility model relates to equipment for producing gasoline and diesel oil by using waste plastics and/or heavy oil, which is mainly composed of a plastic extruder, a groove-shaped spiral reactor, a combustion chamber, a vaporizing chamber, a separation box, a spiral stirrer, a cyclone separator, a hydrocarbon oil separation device, etc. The utility model has the characteristics of fast reaction and heat transfer, low energy consumption, no equipment coking, no oil containing in slag, high finished product conversion rate and less investment.
Description
The utility model relates to uses plastic waste, the equipment of high-boiling hydrocarbons material production lower boiling hydrocarbon ils, be a kind of by thermo-cracking and catalytic pyrolysis from plastic waste and or heavy oil produce the equipment of gasoline, diesel.
About plastic waste and high boiling hydrocarbon is the existing a lot of reports of equipment of raw material production low boiling hydrocarbon, open flat 4-50929 and clear and 60-58485 the spy, 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 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, the easy local superheating coking of still inwall, influence 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 that splitting gas is external in difficult sealing in screw rod two ends and the tube lets out, and screw spiral is assemblied in circular barrel center, and a tube internal upper part does not have gasification space, and the influence reaction is carried out.What have reacts under the vacuum of harshness 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 purpose of this utility model will overcome above-mentioned shortcoming exactly, provide from plastic waste and or high boiling hydrocarbon such as heavy oil produce the equipment of gasoline, diesel.Specifically, the inorganic particulate thermal barrier is dropped in the helical reactors and raw material direct contact heat transfer generation thermally splitting continuously circularly, the gas phase hydrocarbon of generation enters fixed bed generation catalyzed reaction, and plastic waste and high boiling hydrocarbon are changed into gasoline, diesel.The utlity model has reaction and conduct heat soon, 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 purpose of this utility model realizes with following mode.
A kind of with plastic waste and or heavy oil produce the equipment of gasoline, diesel, mainly comprise extruding machine (2), flute profile helical reactors (21), combustion chamber (9), vaporizer (22), separator box (25), cyclonic separator (11,13,37) and hydrocarbon ils collection device.Described flute profile helical reactors (21) comprises; Elongated cylindrical housing (40) fixes on the ground motionless.Housing (40) bottom is semicircle and disposes screw rod agitator (3) that accept peripheral magnetic electromotor (1,19) between the screw rod agitator (3) in the housing (40) and drive, the material in the housing (40) does not have any leakage.Extruding machine (2) and thermal barrier (4) inlet are configured in channel reactor (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 channel reactor (21), and its outlet connects separation column (28).Vaporizer (22) bottom is connected by spiral conveyer (3) with separator box (25) middle part.The bottom of separator box (25) is basin (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 (12) connects tornado dust collector (13), and cyclonic separator (11) bottom connects the outlet on the material-storage jar (5), and material-storage jar (5) bottom communicates through worm conveyor (3) and with the top (10) of combustion chamber (9).Described combustion chamber (9) includes oil, vapour burner (8,6) and air nozzle (7).Bottom, combustion chamber (9) connects the top of material-storage jar (5), and material-storage jar (5) bottom communicates with flute profile helical reactors (21) top through worm conveyor (3).The utility model further comprises the hydrocarbon ils fractionation plant, all belongs to the conventional gasoline, diesel tripping device that uses in this area, comprising: separation column (28), condenser (29,33), water-and-oil separator (30 and 38) and water-sealed tank (31) etc.
Fig. 1 is an equipment drawing of the present utility model
Among the figure, 1-motor, 2-extruding machine, 3-screw rod agitator, the 4-thermal barrier, 5-material-storage jar, 6-vapour nozzle, 7-air nozzle, the spray of 8-oil, 9-combustion chamber, 10-exhaust outlet of combustion chamber, 11-cyclonic separator, 12-cyclonic separator venting port, the 13-fly-ash separator, 14-stores ash bin, 15-ash discharging hole, the 16-solid mixture, 17-valve, 18-liquid starting material inlet, 19-magnetic electromotor, the 20-circular baffle plate, 21-flute profile helical reactors, 22-vaporizing chamber, the 23-fixed bed, 24-manhole, 25-separator box, the 26-basin, 27-gas blower, 28-separation column, the 29-gasoline condenser, 30-gasoline water-and-oil separator, 31-water-sealed tank, 32-stripping jar, 33-diesel oil condenser, 34-diesel storing, 35-gasoline basin, the cross steelframe that the 36-center is with holes, 37-thermal barrier separator, 38-diesel oil water-and-oil separator, 39-hot-blast spray nozzle, 40-elongated cylindrical housing.
Equipment of the present utility model mainly comprises extruding machine (2), flute profile helical reactors (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 (40) fixes on the ground motionless.Housing (40) 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 (40) 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 (40) 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 (40) 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 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 a storage ash can (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 material-storage jar (5) top, and material-storage jar (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.Diesel oil 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 the utility model is further detailed.
Is 0 with diameter earlier, the hard particles shape pure aluminium silicate of 1-3 millimeter is packed into (5) in the material-storage jar as thermal barrier (4), with pushing in the combustion chamber (9) of spiral conveyer (3) constant speed.With oil fuel (or reclaim splitting 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 flute profile helical reactors (21) to promote to flow into vaporizer (22) bottom, enters separator box (25) through worm conveyor (3).Send into separator box (25) with the high-temperature flue gas that gas blower (27) inspiration was handled through thermal barrier separator (37) 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 material-storage jar (5).Isolated gas contains the inorganic grit that initial feed is brought into, through fly-ash separator (13) separate the back from store ash bin (14) through the hole (15) discharger.With worm conveyor (3) solid mixture (16) in the material-storage jar (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.Inorganic carrier (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 heat scission reaction heat supply in the reactor (21).In the said process, inorganic particulate thermal barrier (4) is in all the time and is heated---heat release---heated continuous recurrent state.Its objective is that the scission reaction of guaranteeing in the flute profile helical reactors (21) has enough heats.
Below illustrate in greater detail the utility model by specific embodiment, but the utility model 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 material-storage jar 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) and burn, thermal barrier (4) is heated in combustion chamber (9) and is warmed up to 600-700 ℃, ceaselessly fall into and stock jar (5), use worm conveyor (3) to circulate continuously again and ceaselessly thermal barrier (4) is delivered in the flute profile helical reactors (21).(PP is 25% with the plastic waste in 1400 kilograms of Beijing winters with spiral (or reciprocating type) extruding machine (2), PP is 25%, PE is 50%) push in the flute profile helical reactors (21) of sealing, and direct and thermal barrier (4) directly living heat transfer of 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 (22) from material inlet one end of reactor (21) under screw rod (3) promotes.Material inlet temperature in the reactor (21) is controlled at 600-700 ℃, and the residue temperature out after the cracking is controlled at 500 to 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 DX-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) in the reactor (21) to promote to flow into vaporizer (22) bottom, goes into 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).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 material-storage jar (5).Isolated gas contains the inorganic grit that plastic waste is brought into, through fly-ash separator (13) separate the back from store ash bin (14) through the hole (15) discharger.With worm conveyor (3) solid mixture (16) in the material-storage jar (5) is pushed combustion chamber (9).(9) lining in the combustion chamber contains oil residue by burning out in the mixture (16).Wherein, the inorganic grit that proportion is little is taken away with high-temperature flue gas.Heavy particulate state thermal barrier (4) is burned again to be heated to 600-700 ℃, and falls into material-storage jar (5), sends into the plastic waste heat supply of giving in the flute profile helical reactors (21) in the reactor through the continuous round-robin of worm conveyor (3).In the said process, 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%), and PS is
350KG (25%), PE are 700KG (50%).
Reaction pressure: 0,05-0,1MPA
Thermal barrier advances temperature of reactor: 600-700 ℃
Thermal barrier goes out temperature of reactor: 500-600 ℃.
Catalyzed reaction temperature: 300-350 ℃
Catalyzer: DX-1 type catalyzer.
Reaction product: gasoline, 630KG (40%) RON is 93,5.
Gasoline (w%): alkane is 19,9%, and naphthenic hydrocarbon is 12%, and is rare
Hydrocarbon is 48%, and aromatic hydrocarbons is 9,9%, and other is
10，2％。
Diesel oil, 420KG (35%), cetane value is 52.
Diesel oil component (W%) alkane is 15%, and naphthenic hydrocarbon is 8%,
Rare hydrocarbon is 55%, aromatic hydrocarbons 10%, and other is 12% years old
Inorganic residues: 140KG 10%.
Inflammable gas: 210KG 15% turns back in the combustion chamber and burns
Claims (4)
1, a kind of with plastic waste and or heavy oil produce the equipment of gasoline, diesel, mainly comprise: extruding machine (2), flute profile helical reactors (21), screw rod agitator (3), combustion chamber (5), vaporizing chamber (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) comprising: elongated cylindrical housing (40) fixes on the ground motionless; Housing (40) bottom is semicircle and disposes screw rod agitator (3) that housing (40) top is Long Circle or semicircle, is the vaporization space of gas-phase product; Accepting peripheral magnetic electromotor (1,19) between the screw rod agitator (3) in the housing (40) drives; Spiral screw rod agitator (3) one ends support with the round-meshed circular baffle plate in center (20) and separate with magnetic electromotor (19), and the other end is by the round-meshed cross steelframe in center (36) support fixation; Housing (40) 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 (40) 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 particulate state thermal barrier (4) inlet are configured in flute profile helical reactors (21) top one end respectively; Vaporizer (22) is configured in 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) or hydrocarbon ils collection device; The bottom of vaporizer (22) is connected by spiral conveyer (3) with separator box (25) middle part; The bottom of separator box (25) is a storage ash can (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 material-storage jar (5) top, and material-storage jar (5) bottom communicates through worm conveyor (3) and with the top of combustion chamber (9); The top exit of combustion chamber (9) and thermal barrier separator (37) middle part link, and the import of the top of thermal barrier separator (37) and gas blower (27) links, and the hot-blast spray nozzle (39) of the outlet of gas blower (27) and separator box (25) links; Described combustion chamber (9) includes oil firing nozzle (8), vapour burner noz(zle) (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) links through worm conveyor (3) and flute profile helical reactors (21) top one end.
2, according to the equipment of claim 1, wherein said hydrocarbon ils collection device comprises: separation column, condenser, water-and-oil separator, stripping jar and water-sealed tank etc.
3, according to the equipment of claim 1, the first half in the housing (40) of wherein said flute profile helical reactors (21) leaves enough vaporization spaces, and drive shell (40) bottom spiral stirrer (3) motor rotating can be electromagnetic machine or common electric machine.
4, according to the equipment of claim 1, wherein said motor (1) belongs to speed change or constant-seed motor.
Priority Applications (8)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN99216787U CN2408118Y (en) | 1999-07-16 | 1999-07-16 | Equipment for producing gasoline and diesel oil by using waste plaste and/or heavy oil |
| AU58015/00A AU5801500A (en) | 1999-07-16 | 2000-07-13 | A process for producing gasoline and diesel from waste plastics and/or heavy oil |
| JP2001511126A JP2003528937A (en) | 1999-07-16 | 2000-07-13 | Process for producing gasoline and diesel from plastic waste and / or heavy oil |
| EP00943524A EP1228165A4 (en) | 1999-07-16 | 2000-07-13 | A process for producing gasoline and diesel from waste plastics and/or heavy oil |
| PCT/CN2000/000196 WO2001005908A1 (en) | 1999-07-16 | 2000-07-13 | A process for producing gasoline and diesel from waste plastics and/or heavy oil |
| CA002379529A CA2379529A1 (en) | 1999-07-16 | 2000-07-13 | A process for producing gasoline and diesel from waste plastics and/or heavy oil |
| KR1020027000608A KR20020052168A (en) | 1999-07-16 | 2000-07-13 | A process for producing gasoline and diesel from waste plastics and/or heavy oil |
| BR0012623-3A BR0012623A (en) | 1999-07-16 | 2000-07-13 | Process for producing gasoline and diesel from waste plastics and / or heavy oil |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN99216787U CN2408118Y (en) | 1999-07-16 | 1999-07-16 | Equipment for producing gasoline and diesel oil by using waste plaste and/or heavy oil |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN2408118Y true CN2408118Y (en) | 2000-11-29 |
Family
ID=5297315
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN99216787U Expired - Fee Related CN2408118Y (en) | 1999-07-16 | 1999-07-16 | Equipment for producing gasoline and diesel oil by using waste plaste and/or heavy oil |
Country Status (8)
| Country | Link |
|---|---|
| EP (1) | EP1228165A4 (en) |
| JP (1) | JP2003528937A (en) |
| KR (1) | KR20020052168A (en) |
| CN (1) | CN2408118Y (en) |
| AU (1) | AU5801500A (en) |
| BR (1) | BR0012623A (en) |
| CA (1) | CA2379529A1 (en) |
| WO (1) | WO2001005908A1 (en) |
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-
1999
- 1999-07-16 CN CN99216787U patent/CN2408118Y/en not_active Expired - Fee Related
-
2000
- 2000-07-13 BR BR0012623-3A patent/BR0012623A/en not_active Application Discontinuation
- 2000-07-13 EP EP00943524A patent/EP1228165A4/en not_active Withdrawn
- 2000-07-13 WO PCT/CN2000/000196 patent/WO2001005908A1/en not_active Ceased
- 2000-07-13 KR KR1020027000608A patent/KR20020052168A/en not_active Withdrawn
- 2000-07-13 JP JP2001511126A patent/JP2003528937A/en active Pending
- 2000-07-13 AU AU58015/00A patent/AU5801500A/en not_active Abandoned
- 2000-07-13 CA CA002379529A patent/CA2379529A1/en not_active Abandoned
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2008131600A1 (en) * | 2007-04-28 | 2008-11-06 | Bin Niu | A process and a device for continuous cracking waste plastics |
| CN101805630A (en) * | 2010-05-21 | 2010-08-18 | 雪合来提 | Fluidizing bed type waste plastic continuous oil refining device with environment protection and high efficiency |
Also Published As
| Publication number | Publication date |
|---|---|
| WO2001005908A1 (en) | 2001-01-25 |
| AU5801500A (en) | 2001-02-05 |
| EP1228165A1 (en) | 2002-08-07 |
| BR0012623A (en) | 2003-04-08 |
| EP1228165A4 (en) | 2004-01-28 |
| JP2003528937A (en) | 2003-09-30 |
| KR20020052168A (en) | 2002-07-02 |
| CA2379529A1 (en) | 2001-01-25 |
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Addressee: Zhou Jifu Document name: Notice of registration |
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Address after: 102403 Beijing Fangshan District glass town ancestral village Beijing Li Kun chemical plant Patentee after: Zhou Dingli Address before: No. 2, unit 3, building 7, No. 602, Heng Fu Street, Fengtai District, Beijing Patentee before: Zhou Jifu |
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| C19 | Lapse of patent right due to non-payment of the annual fee | ||
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