CN1075328A - Method and apparatus for continuous production of petroleum products from waste plastics - Google Patents
Method and apparatus for continuous production of petroleum products from waste plastics Download PDFInfo
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- CN1075328A CN1075328A CN 92100844 CN92100844A CN1075328A CN 1075328 A CN1075328 A CN 1075328A CN 92100844 CN92100844 CN 92100844 CN 92100844 A CN92100844 A CN 92100844A CN 1075328 A CN1075328 A CN 1075328A
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- catalytic cracking
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- 239000004033 plastic Substances 0.000 title claims abstract description 13
- 229920003023 plastic Polymers 0.000 title claims abstract description 13
- 238000000034 method Methods 0.000 title claims description 20
- 239000002699 waste material Substances 0.000 title abstract description 10
- 239000003209 petroleum derivative Substances 0.000 title abstract description 8
- 238000010924 continuous production Methods 0.000 title description 5
- 238000004523 catalytic cracking Methods 0.000 claims abstract description 33
- 239000003054 catalyst Substances 0.000 claims abstract description 22
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 11
- 239000003546 flue gas Substances 0.000 claims abstract description 11
- 238000004140 cleaning Methods 0.000 claims abstract description 10
- 238000004519 manufacturing process Methods 0.000 claims abstract description 4
- 239000013502 plastic waste Substances 0.000 claims description 15
- 239000007789 gas Substances 0.000 claims description 13
- 238000007747 plating Methods 0.000 claims description 13
- 239000002994 raw material Substances 0.000 claims description 9
- 238000010438 heat treatment Methods 0.000 claims description 7
- -1 polyethylene Polymers 0.000 claims description 6
- 239000003245 coal Substances 0.000 claims description 5
- 239000002283 diesel fuel Substances 0.000 claims description 5
- 239000003208 petroleum Substances 0.000 claims description 5
- 238000010410 dusting Methods 0.000 claims description 4
- 239000004698 Polyethylene Substances 0.000 claims description 3
- 239000004743 Polypropylene Substances 0.000 claims description 3
- 239000004793 Polystyrene Substances 0.000 claims description 3
- 239000000446 fuel Substances 0.000 claims description 3
- 229920000573 polyethylene Polymers 0.000 claims description 3
- 229920001155 polypropylene Polymers 0.000 claims description 3
- 229920002223 polystyrene Polymers 0.000 claims description 3
- 238000007670 refining Methods 0.000 claims description 3
- 239000000779 smoke Substances 0.000 claims description 3
- 229920001083 polybutene Polymers 0.000 claims description 2
- 238000010304 firing Methods 0.000 claims 1
- 238000005984 hydrogenation reaction Methods 0.000 claims 1
- 239000002904 solvent Substances 0.000 claims 1
- 239000000047 product Substances 0.000 abstract description 30
- 238000000746 purification Methods 0.000 abstract description 6
- 239000000428 dust Substances 0.000 abstract description 4
- 239000012263 liquid product Substances 0.000 abstract description 4
- 238000005194 fractionation Methods 0.000 abstract description 3
- 230000003197 catalytic effect Effects 0.000 abstract 1
- 238000005520 cutting process Methods 0.000 abstract 1
- 229910052799 carbon Inorganic materials 0.000 description 13
- 239000003921 oil Substances 0.000 description 10
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 8
- 239000003502 gasoline Substances 0.000 description 7
- 239000002956 ash Substances 0.000 description 5
- 238000005336 cracking Methods 0.000 description 5
- 230000035611 feeding Effects 0.000 description 5
- 239000000463 material Substances 0.000 description 5
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 5
- 239000004215 Carbon black (E152) Substances 0.000 description 4
- 238000006243 chemical reaction Methods 0.000 description 4
- 239000000284 extract Substances 0.000 description 4
- 229930195733 hydrocarbon Natural products 0.000 description 4
- 150000002430 hydrocarbons Chemical class 0.000 description 4
- 238000009826 distribution Methods 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 239000003350 kerosene Substances 0.000 description 3
- 239000007788 liquid Substances 0.000 description 3
- 239000010813 municipal solid waste Substances 0.000 description 3
- 238000000926 separation method Methods 0.000 description 3
- 238000010008 shearing Methods 0.000 description 3
- 241000282326 Felis catus Species 0.000 description 2
- 229910021536 Zeolite Inorganic materials 0.000 description 2
- 238000009835 boiling Methods 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 description 2
- 239000000945 filler Substances 0.000 description 2
- 239000010881 fly ash Substances 0.000 description 2
- 239000000295 fuel oil Substances 0.000 description 2
- 230000004927 fusion Effects 0.000 description 2
- 239000007791 liquid phase Substances 0.000 description 2
- 230000008018 melting Effects 0.000 description 2
- 238000002844 melting Methods 0.000 description 2
- 238000010298 pulverizing process Methods 0.000 description 2
- 238000011084 recovery Methods 0.000 description 2
- 230000008929 regeneration Effects 0.000 description 2
- 238000011069 regeneration method Methods 0.000 description 2
- 230000001105 regulatory effect Effects 0.000 description 2
- 239000010457 zeolite Substances 0.000 description 2
- 229920002472 Starch Polymers 0.000 description 1
- 229910000831 Steel Inorganic materials 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 239000005864 Sulphur Substances 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 150000001335 aliphatic alkanes Chemical class 0.000 description 1
- 150000001336 alkenes Chemical class 0.000 description 1
- 150000004945 aromatic hydrocarbons Chemical class 0.000 description 1
- 229910001570 bauxite Inorganic materials 0.000 description 1
- 230000005540 biological transmission Effects 0.000 description 1
- 239000011449 brick Substances 0.000 description 1
- 238000006555 catalytic reaction Methods 0.000 description 1
- 239000000571 coke Substances 0.000 description 1
- 238000004939 coking Methods 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 238000000280 densification Methods 0.000 description 1
- 238000001035 drying Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 238000009776 industrial production Methods 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 239000002808 molecular sieve Substances 0.000 description 1
- 239000012188 paraffin wax Substances 0.000 description 1
- 235000019809 paraffin wax Nutrition 0.000 description 1
- 235000019271 petrolatum Nutrition 0.000 description 1
- 229920000915 polyvinyl chloride Polymers 0.000 description 1
- 239000004800 polyvinyl chloride Substances 0.000 description 1
- 239000000376 reactant Substances 0.000 description 1
- 230000035484 reaction time Effects 0.000 description 1
- 238000010992 reflux Methods 0.000 description 1
- 238000012827 research and development Methods 0.000 description 1
- 239000004576 sand Substances 0.000 description 1
- 239000002893 slag Substances 0.000 description 1
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 description 1
- 239000008107 starch Substances 0.000 description 1
- 235000019698 starch Nutrition 0.000 description 1
- 238000010025 steaming Methods 0.000 description 1
- 239000010959 steel Substances 0.000 description 1
- 238000003756 stirring Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
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- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
- Separation, Recovery Or Treatment Of Waste Materials Containing Plastics (AREA)
Abstract
An industrial process for continuously producing serial petroleum products from waste plastics includes waste plastics purification, the first stage of catalytic cracking and its product fractionation, and the second stage of catalytic cracking and its product rectification. The first stage is at 400-550 deg.c and normal pressure, and catalyst A is used. The second stage temperature is 300-380 deg.c and normal pressure, and catalyst B or 2MS-5 is used. The continuous purifying device for the film waste plastics consists of a cutting machine, a dust remover, a cleaning machine and a squeezing machine. The first stage catalytic cracker is a coal-fired boiler with flue gas jacket. The catalyst is cheap and easy to obtain, the processing cost is low, the yield of liquid products reaches 70-78%, the variety of oil products is easy to adjust, and no three-waste pollution is caused.
Description
The present invention relates to a kind of is that feedstock production goes out lower boiling hydrocarbon ils with the plastic waste, and then is the method and apparatus of raw material at the serial petroleum products of industrial production with this hydrocarbon ils.
The quantity of plastic garbage and day sharp increase have now caused worldwide environmental pollution, and various countries are for handling this rubbish, and will use up enormous expenditure every year.In order to eliminate plastic garbage to the pollution of environment and and then turn waste into wealth the method that countries in the world all utilize in the various waste plastics recoveries of research and development.The U.S., Japan and Germany disclose the patent of many this respects in succession, still, up to the present do not see the report of industrial-scale production as yet.
Associated patent has US3,956,414 it be to generate hydrocarbon ils with the method for thermally splitting, can't carry out because of containing a large amount of carbon laydowns of a large amount of paraffin waxes and reactor in the product.US4,108,730 and US4,175,211st, will plastic waste and high boiling petroleum distillate (heavy oil that generates as catalytic cracking) congruent melting after carry out catalytic cracking and generate hydrocarbon ils.US4,118,281st, plastic waste is mixed with the heavy circulation component of coker, make it to starch attitudeization or congruent melting, this mixture of first coking, above-mentioned coke chemicals of catalytic cracking and obtain the gasoline of high yield again.Aforesaid method be unable to do without the heavy crude overhead product add, and its consumption can not use by secondary very greatly again, so can't found the factory in the place away from refinery, applying of this method is restricted.
The technology the most close with the present invention is the patent US4 of Japanese 1989.7.25 at U. S. application, 851,801, this method is divided into two sections, first section thermally splitting, temperature 390-500 ℃, be reflected under the liquid phase state and carry out, conduct heat for improving, adding granularity in the reactant that is in liquid phase is the inorganic inert material of 1-10MM, as zeolite, bauxite etc.; Second section is again first section product to be carried out catalytic cracking with zeolite catalysts such as ZMS-5 molecular sieves.Laboratory scale feeding rate is 680-706 gram/time, liquid yield 50-60%, and gas recovery ratio about 37%, alkane accounts for 38.4% in the liquid product, and alkene accounts for 14.2%, and aromatic hydrocarbons accounts for 4.5%.Its shortcoming is second section must adopt expensive ZMS-5 sieve peg-raking catalyst, and liquid product yield is low, and only is Bench test, also has a very long segment distance apart from industrial application.
Task of the present invention is to develop that a kind of catalyzer is that cheaply be easy to get, that liquid yield is high, the commercial run and the equipment with waste or used plastics continuous production series petroleum products of purpose product adjustable ratio.
The commercial run and the specific equipment thereof that with the waste or used plastics are raw material continuous production series petroleum products are as follows.
1) purification of raw materials is handled:
Available raw material comprises: polyethylene, polypropylene, polybutene, polystyrene and polyvinyl chloride.Raw material is standby through shearing or pulverizing, dedusting, after cleaning, extract or drying.
2) first stage catalytic cracking:
Raw material after the above-mentioned purification and catalyst A are with 500-800: 1 ratio enters the catalytic cracking still continuously, and the product after the cracking is gaseous state or steam state is discharged continuously, and disposable catalyst A and carbon residue are regularly discharged at the bottom of still.Temperature in the kettle is 400-550 ℃, and pressure is normal pressure or a little higher than normal atmosphere, and reaction time is about 10 to 20 minutes.Plastic waste enters fractionating column after the evaporation of fusion, catalytic cracking and product thereof.
3) fractionation of first section product:
Above-mentioned gaseous state or steam state product are carried out fractionation, can get high heating value gas (non-condensable gas), liquefied gas and petroleum naphtha, can obtain the above mixed fraction of heavy gas oil from the tower middle and lower part, can get heavy oil fraction at the bottom of the tower from cat head.The ratio of three kinds of cuts of upper, middle and lower can be regulated according to the requirement of final purpose product.If require vapour, coal, three kinds of oil products of bavin, can be with the straight-through rectifying tower of middle and lower part overhead product, the bottom overhead product heats after second stage catalytic cracking enters rectifying tower again; If require mainly to obtain gasoline products, with after middle part and the heating of bottom overhead product all by entering rectifying tower behind second stage catalytic cracking again.
4) second stage catalytic cracking:
Enter the fixed-bed reactor that catalyst B or ZMS-5 are housed after the overhead product heating of above-mentioned separation column bottom or middle part and bottom, temperature of reaction is 300-380 ℃, and pressure is a little more than normal atmosphere.Pull up catalyst activity reduction after to a certain degree, the carbon distribution of burning catalyst surface with warm air makes its regeneration.Regeneration temperature is 380-430 ℃.
5. the rectifying of the second stage catalytic cracking product
On different column plates,, control certain temperature and reflux ratio so that obtain liquefied gas, gasoline, kerosene and diesel oil according to the requirement of purpose product.Tower bottoms is less than 1%.
The embodiments of the invention accompanying drawings is as follows:
Fig. 1 is a schematic flow sheet of the present invention.
Fig. 2 is the first stage catalytic cracking still synoptic diagram.
Fig. 3 is the A-A sectional drawing of Fig. 2.
Fig. 4 is a refining plant synoptic diagram of the present invention.
As shown in Figure 1, plastic waste cleans, extracts by extracting machine 5 at last through shears or pulverizer 1 shearing or pulverizing, dusting machine 2 dedustings, first clear 3 and whole cleaning machine 4.Plastic waste after the purification and a certain proportion of catalyst A are delivered in the feeding screw 7 of the first stage catalytic cracking still 9 by travelling belt 6, with dipleg 8 that above-mentioned feeder 7 links to each other by reducing in, plastic waste is by densification, oven dry and even fusion, form one section material envelope, first section cracked product can not moved back in the feeder 7.The size of the described first stage catalytic cracking reactor 9 is 1400 * 4300, inlet amount is 10 tons/day, raw material is 500-800 with the ratio of the weight of catalyst A: 1, and what of catalyst A addition are decided by the character (polyethylene, polypropylene or polystyrene) and the distribution of the finished product of plastics.The still interior reaction temperature is 400-550 ℃, and pressure is 0.3 kg/cm (gauge pressure), and the material mean residence time is 10-20 minute.One section crackate is steam state and enters fractionating column 11, the carbon deposit that plastics inlet amount about 10% is arranged approximately on the surface of catalyst A, when the catalyst A that has the carbon deposit non-activity build long-pending amount reach cracking still 9 chamber internal volumes 1/4～1/3 the time, regularly discharge from the slag-drip opening 31 of Fig. 2.Because the slag envelope of certain depth is arranged at bottom, still chamber, bits are loose bodies of similar sand, thus can in continuously feeding, carry out deslagging, thereby realized first section continuous catalysis cracking.One section crackate enters from the bottom of filler fractionating column 11, overhead fraction is through condenser 17, gas-liquid separator 13 is told liquefied gas a, the part of a is as the fuel of the combustion heater of the second stage catalytic cracking reactor, 14 shells, and a part is compressed, sell as finished product after the condensation, bottling.The petroleum naphtha c(petroleum naphtha that separator 13 is told), a part pumps in the tower as product gasoline with pump 16.The heating coil 12 that heavy gold-plating lease making condenser 17, pump 16 are delivered in one section cracking still 9 at the bottom of the tower of fractionating column is heated to the top of delivering to two stage catalytic cracking reactors 14 about 300 ℃; The above cut of separation column 11 diesel oil can tower directly into fractionate 15 at the bottom of so that obtain more diesel oil gold-plating branch.The catalyst B that granularity is 3mm is housed in the second stage catalytic cracking reactor 14, and its size is 1400 * 4700, and temperature of reaction is 300～380 ℃, and reaction pressure is 0.2 kg/cm, and input rate is 8-9 ton/sky.Second stage reactor 14 is arranged in parallel two covers, when the activity of catalyst B descends, switches, and feeds warm air b from the top and burns the carbon deposit on catalyst B surface, discharges flue gas h.The product of two stage catalytic crackings enters general filler fractionate 15, and cat head gets the gasoline gold-plating and divides d, and the branch line of tower gets the kerosene gold-plating and divides e, solar oil gold-plating to divide f and heavy gas oil gold-plating to divide g, this nothing of tower base Residual oil.
Described catalyst A and B are the product of Shanxi plasticizing head factory, public sale, and marque is respectively SSHZ-1 and SSHZ-2.
As shown in Figures 2 and 3,19 is one section crackate outlet, 20 is the inlet of oil heater 12 at the bottom of separation column 11 towers, 21 is chimney, 22 is the outlet of well heater 12,23 is fire door, 24 is the ash removing hole of flue gas chuck 30,25 is fire grate, and 26 is the lime-ash door, and 27 is the center smoke pipe, 28 is flue damper, 29 is a stage catalytic cracking reactor annular cavity, and 30 is the flue gas chuck, and the conical part of this chuck and Cylinder part is parallel to post axis, garden on week along cone generatrices and garden steel plate is divided into four spaces, flue gas rises to baffle plate 28 from center smoke pipe 27, return the chuck bottom downwards along the left and right sides chuck 30 of Fig. 2 then, last, flue gas is that the left and right sides chuck of Fig. 3 is back to flue gas pipe connecting 32 and enters chimney 21 and discharge by the front and back chuck of Fig. 2.The bottom of cracking still 9 is as general flue gas chuck normal-pressure boiler, and lining of fire brick burns at fire grate 25 upper coal feedings all around, and ash content is discharged from ash door 26.Dipleg 30 behind the feeding screw 7 inserts in the still chamber 29.
As shown in Figure 4,33 is the plastic waste travelling belt, and 34 is motor, 35 is interior garden platform shape cylinder, 36 is that taking off of eccentric pattern grabbed on the cylinder 35, and 37 is dust absorption fan, and 28 is garden platform shape dust-absorbing tube, 39 is carrier pipe, 40 is belt clamping device, and 41 is water inlet, and 42 is water vent, 43 is pulley belt, and 44 is driving motor.
Plastic waste is from travelling belt 33 to shears 1, through carrier pipe 39 to fly-ash separator 2, through carrier pipe 39 to first cleaning machine 3 again through carrier pipe 39 to whole cleaning machine 4, after carrier pipe 39 to extract 5 extract standby.
The interior garden platform shape cylinder of dusting machine 2 is driven through belt 43 and belt pulley 44 by motor 34, and the interior cylinder of first cleaning machine 3 is driven by the belt and the belt pulley of fly-ash separator, and first cleaning machine drives the interior cylinder of whole cleaning machine 4 again.Cylinder drives and rotates synchronously by a motor 34 in described three garden platform shapes.
Plastics to be clean are grabbed 36 the continuous transmission of stirring along cylinder outer wall by centrifugal force and taking off, and earlier by 37 and 38 dust suctions, the back adds water by 41 to be cleaned in transport process, and dust-containing water is discharged by 42.
Described purification system realized film material shearing, dedusting, clean and extract the process serialization.This continuous operation for follow-up equipment is vital.This device has not only been realized serialization, and treatment capacity also can be very big, and treatment capacity also can be regulated in a big way.The degree of purification height, degree of extracting height.
The result of final purpose product is as follows:
Gasoline: 10%: 78 ℃ (≤79 ℃), 50%: 134 ℃ (≤145 ℃), 90%: 182 ℃ (≤195 ℃), do 230 ℃ (should be 205 ℃), loss amount 3.5%(≤4.5%), residual quantity 0.8%(≤1.5%), acidity 3mgkoH/1000ml(≤3), mechanical impurity and moisture do not have (nothing), existent gum 4.4mg/1000ml(≤5).Index in the above-mentioned bracket is the national standard of No. 70 gasoline.Hence one can see that, except that doing, all reaches GB.
Solar oil: 50%: 285 ℃ (≤300 ℃), 90%: 327 ℃ (≤355 ℃), acidity 6mgKOH/1000ml(≤100), existent gum 68mg/100ml, water soluble acid or sulphur do not have (nothing), ash content 0.3%(≤0.3%), thing carbon residue 0.3%(≤0.3% is stayed in 10% steaming), 80 ℃ of interior points (〉=65 ℃).Index in the above-mentioned bracket is the national standard of solar oil, and hence one can see that, all reaches GB.
Heavy gas oil and kerosene reality show excellent property with the result.
Mainly consisting of of reacted gas: H
219.92%, O
20.13%, N
20.44%, CO1.98%, CH
420.35%, C
2H
421.05%C
2H
69.93%, C
3H
610.19%, C
3H
84.5%, C
4H
84.91%, C
4H
102.18%, anti--C
4H
80.68%, suitable-C
4H
80.49%, the summation of vapour, coal, three kinds of product yields of diesel oil is up to 70-78%, and its ratio can be adjusted with sizable amplitude as required.Reacted gas yield 10-12%, the carbon distribution of catalyst surface accounts for about 10%.
In sum, to have reached be the purpose of raw material continuous production series petroleum products on technical scale with the plastic waste in the present invention.Quality product reaches state specified standards.Liquid product yield is up to 70-78%.The kind of oil product can be adjusted as required.The catalyzer wide material sources cheaply are easy to get, and its expense only accounts for below 5% of total cost, with coal heating, reduce greatly than the cost of gas fuel.The basic three-waste free discharge of whole process.
Claims (8)
1, a kind of is the method for raw material production petroleum series product with the plastic waste, it is characterized in that it is made up of following process steps:
1) plastic waste is purified,
2) at normal pressure or a little more than normal atmosphere and the 400-550 ℃ of following catalyst A that adopts the plastics after purifying are carried out first stage catalytic cracking,
3) product of branch gold-plating first stage catalytic cracking,
4) at normal pressure or a little more than under normal pressure and 300-380 ℃, with catalyst B gold-plating is gone out thing and carry out second stage catalytic cracking.
5) the smart gold-plating second stage catalytic cracking product.
2, method as claimed in claim 1 or 2 is characterized in that described plastic waste is polyethylene, polypropylene, polybutene or polystyrene.
3, method as claimed in claim 1 or 2 is characterized in that the whole heavy endss behind the branch gold-plating after the indirect heating, carry out second stage catalytic cracking again in the first stage catalytic cracking still chamber.
4, method as claimed in claim 1 or 2 is characterized in that the heavy ends behind the branch gold-plating carries out second stage catalytic cracking after the indirect heating again in the first stage catalytic cracking still chamber, and the above cut of a part of diesel oil directly enters rectifying tower.
5, method as claimed in claim 1 or 2 is characterized in that the petroleum naphtha hydrogenation behind minute gold-plating making solvent oil after refining.
6, method as claimed in claim 1 or 2 is characterized in that a liquefied gas part behind the branch gold-plating is as the fuel of second stage catalytic cracking.
7, a kind of catalytic cracking still of implementing the described method of claim 1, it is characterized in that it being the coal firing boiler of a band flue gas chuck, flue gas rises to baffle plate 28 from center smoke pipe 27, the top that the bottom that drops to chuck 30 is then returned chuck 30 is again gone into chimney 21 through flue gas pipe connecting 32 and is discharged, heavy divides well heater 12 at the bottom of in the one stage catalytic cracking still chamber 29 fractionating column being set, and dipleg 8 inserts in the stage catalytic cracking still chamber 29.
8, implement the plastic waste refining plant of the described method of claim 1, it is characterized in that it is made up of stapling machine, dusting machine, cleaning machine and the machine of extracting, described dusting machine and cleaning machine are made of circle halfpace inner sleeve, and urceolus is fixed, and three inner cores are rotated synchronously by a driven by motor.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 92100844 CN1075328A (en) | 1992-02-12 | 1992-02-12 | Method and apparatus for continuous production of petroleum products from waste plastics |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 92100844 CN1075328A (en) | 1992-02-12 | 1992-02-12 | Method and apparatus for continuous production of petroleum products from waste plastics |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN1075328A true CN1075328A (en) | 1993-08-18 |
Family
ID=4938822
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 92100844 Withdrawn CN1075328A (en) | 1992-02-12 | 1992-02-12 | Method and apparatus for continuous production of petroleum products from waste plastics |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1075328A (en) |
Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO1995006682A1 (en) * | 1993-08-28 | 1995-03-09 | Hainan Yuecheng Development Corp. | A process for producing gasoline and diesel fuel oil from waste plastics and its apparatus |
| WO1997006224A1 (en) * | 1995-08-08 | 1997-02-20 | Li Xing | A process for producing gasoline, diesel fuel and carbon black from waste rubber and/or waste plastics |
| WO2000018852A1 (en) * | 1998-09-24 | 2000-04-06 | Zhou, Dingli | Process and apparatus for producing hydrocarbons from city garbage and/or organic waste material |
| WO2001005908A1 (en) * | 1999-07-16 | 2001-01-25 | Enercon Technologies, Inc. | A process for producing gasoline and diesel from waste plastics and/or heavy oil |
| CN1068032C (en) * | 1998-08-27 | 2001-07-04 | 邢力 | Hydrocarbon preparing method and equipment using household refuse and/or organic waste |
| CN1074447C (en) * | 1999-06-08 | 2001-11-07 | 周鼎力 | Process and equipment for producing gasoline and diesel oil with waste plastics and/or heavy oil |
| WO2002057391A1 (en) * | 2001-01-22 | 2002-07-25 | Chen, Yanping | Method and system of converting waste plastics into hydrocarbon oil |
| CN102344823A (en) * | 2011-09-06 | 2012-02-08 | 六盘水师范学院 | Method for co-liquefaction of coal and waste plastics under mild condition |
| CN113102449A (en) * | 2021-03-31 | 2021-07-13 | 河南科技大学 | Method for fully recycling oversize materials of household garbage |
-
1992
- 1992-02-12 CN CN 92100844 patent/CN1075328A/en not_active Withdrawn
Cited By (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO1995006682A1 (en) * | 1993-08-28 | 1995-03-09 | Hainan Yuecheng Development Corp. | A process for producing gasoline and diesel fuel oil from waste plastics and its apparatus |
| WO1997006224A1 (en) * | 1995-08-08 | 1997-02-20 | Li Xing | A process for producing gasoline, diesel fuel and carbon black from waste rubber and/or waste plastics |
| CN1068032C (en) * | 1998-08-27 | 2001-07-04 | 邢力 | Hydrocarbon preparing method and equipment using household refuse and/or organic waste |
| WO2000018852A1 (en) * | 1998-09-24 | 2000-04-06 | Zhou, Dingli | Process and apparatus for producing hydrocarbons from city garbage and/or organic waste material |
| AU760143B2 (en) * | 1998-09-24 | 2003-05-08 | Dingli Zhou | Process and apparatus for producing hydrocarbons from city garbage and/or organic waste material |
| CN1074447C (en) * | 1999-06-08 | 2001-11-07 | 周鼎力 | Process and equipment for producing gasoline and diesel oil with waste plastics and/or heavy oil |
| WO2001005908A1 (en) * | 1999-07-16 | 2001-01-25 | Enercon Technologies, Inc. | A process for producing gasoline and diesel from waste plastics and/or heavy oil |
| WO2002057391A1 (en) * | 2001-01-22 | 2002-07-25 | Chen, Yanping | Method and system of converting waste plastics into hydrocarbon oil |
| US6774271B2 (en) | 2001-01-22 | 2004-08-10 | Tianfu Jiang | Method and system of converting waste plastics into hydrocarbon oil |
| CN102344823A (en) * | 2011-09-06 | 2012-02-08 | 六盘水师范学院 | Method for co-liquefaction of coal and waste plastics under mild condition |
| CN102344823B (en) * | 2011-09-06 | 2014-01-01 | 六盘水师范学院 | Method for co-liquefaction of coal and waste plastics under mild condition |
| CN113102449A (en) * | 2021-03-31 | 2021-07-13 | 河南科技大学 | Method for fully recycling oversize materials of household garbage |
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