CN1236804A - Process and apparatus for preparing petroleum products from waste plastics and rubber - Google Patents
Process and apparatus for preparing petroleum products from waste plastics and rubber Download PDFInfo
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- CN1236804A CN1236804A CN99114853A CN99114853A CN1236804A CN 1236804 A CN1236804 A CN 1236804A CN 99114853 A CN99114853 A CN 99114853A CN 99114853 A CN99114853 A CN 99114853A CN 1236804 A CN1236804 A CN 1236804A
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- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
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- Y02W30/62—Plastics recycling; Rubber recycling
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Abstract
A process and apparatus for preparing petroleum products from waste plastics and rubber is dosclosed. Its technological steps include smelting waste plastics at 200-250 deg.C and ordinary pressure to obtain molten plastics, cracking in the cracker containing rubber (0-50 vol.%) and catalyst (0.01-1% of raw materials) at 250-400 deg.C and ordinary pressure, condensing, fractionating and purifying to obtain liquefied gas, gasoline, or diesel oil. Said catalyst is the mixture of zinc, aluminium and nickel oxides. Its advantages is that after the non-harmful additive is added, its products have high quality (No.90-93 non-lead gasoline or No.0-10 diesel oil).
Description
The invention belongs to the method and apparatus of preparing petroleum products, particularly relate to the method and apparatus of a kind of plastic waste, waste rubber preparing petroleum products.
Depleted waste or used plastics rubbish, rubber tyre, because of the natural degradation time long, caused serious environmental to pollute, existent environment of people is threatened.For plastics and rubber with the polymer form are reduced into fuel oil,, inside and outside numerous scientific workers adopt various sides to carry out regeneration because of having done a large amount of work.Be to disclose a kind of aluminium hydroxide and quartz sand of adding respectively in 91100046.1 the method for petroleum products " waste or used plastics produce " as application number, at first molten the steaming used r-Al after the combustion
2O
3, quartz sand and alum clay constitute catalyzer quadric catalysis cleavage method, its process complexity, the suitability for industrialized production difficulty is big, and its raw material must clean processes such as pulverizing, production cost height, deficiency in economic performance in advance through water.And for example the patent No. be disclose in " with the device of waste plastic regeneration oil " of 94243269.x a kind of elder generation with plastic waste at high temperature on-catalytic cracking become gas, become the device of gasoline, diesel again by fixed catalytic, its industrial scale is little, and continuous production ability, cracking apparatus are fragile.
It is low to the objective of the invention is to design a kind of catalyzer adult, and raw materials pretreatment is simple, the product yield height, and the oil quality height, production efficiency is remarkable, the method and apparatus of the plastic waste of suitability for industrialized scale production, waste rubber preparing petroleum products.
The object of the present invention is achieved like this: the method for plastic waste, waste rubber preparing petroleum products, comprise catalytic pyrolysis, condensation, fractionation, washing, purifying, interpolation auxiliary agent, be characterized in that plastic waste directly adds in the oil bath melting still behind artificial sub-sieve silt, under normal pressure 200-250 ℃ temperature, be smelted into the molten shape liquid of plastics, send into cracking still through feed screw and carry out cracking; Be added with the catalyzer of the 0.1-1% of the waste rubber that is fractured into the 50-80mm fritter of the 0-50% that accounts for total volume and raw material gross weight in the cracking still, under normal pressure 250-400 ℃ condition, stir catalytic pyrolysis with the molten shape liquid of the plastic waste of sending here from the melting still; Catalyzer is the hopcalite of zinc, aluminium, nickel metallic element, and the per-cent that respectively accounts for the catalyzer total amount is ZnO:20-40%, r-Al
2O
3: 40-60%, NiO:10-20%, the 0.01-1% that presses for the first time the raw material gross weight adds cracking still, thereafter the 0.01-1% that adds the amount of plastic waste according to oil bath melting still adds from the make-up catalyst charging opening at feed screw rear portion, sends into cracking still with the molten shape liquid of plastics; 80 ℃ of condensed gas in the petrol and diesel oil mixed gas that the cracking still cracking produces are through the fractionation of still kettle two-stage separation column, carry out one-level, secondary condenser respectively and are condensed to that room temperature is carried out vapour, diesel oil separates.
Plastic waste, the device of waste rubber preparing petroleum products, by cracking still, the storage slag ladle, condenser, still kettle, separation column, washing tower, storage tanker is formed, it is characterized in that: an oil bath melting still is arranged, the still wall has chuck, inner coil pipe is arranged in the still, chuck all has valve to be connected with thermal medium oil transport pipe with inner coil pipe, thermal medium oil adopts the overheated cylinder stock oil of 62#, squeeze into melting still chuck and inner coil pipe by circulating oil pump, in the melting still agitator is arranged, the agitator central shaft passes melting still top, rotate by motor drives, separation net is arranged at melting still bottom, places plastic waste on the net, and melting still bottom valve is connected with the screw feeding machine inlet capable; A feed screw is arranged at the bottom of the melting still, opening for feed is connected with melting still bottom valve, discharge port is connected with the cracking still feed valve, skin has insulation jacket, deep fat valve on the insulation jacket is connected with thermal medium oil transport pipe, and the feed screw rear portion also is provided with a make-up catalyst charging opening that can add catalyzer at any time in the ratio that adds raw material weight; Spiral tapping machine is equipped with in the bottom of cracking still, and residual cake valve is connected with the storage slag ladle, and the storage slag ladle is provided with chuck outward and is connected with water-cooled tube.
Method and apparatus by a kind of plastic waste provided by the invention, waste rubber preparing petroleum products, use the catalyzer cost low, raw material only needs sub-sieve to remove silt, rubber is cut into piece to be handled simple, product yield Gao Keda 60-80%, gasoline quality reaches 90-93# non-lead gasoline for car standard, and production efficiency is remarkable, commercial scale production degree height.
The present invention has following accompanying drawing:
Fig. 1 is melting of the present invention, cracking output petrol and diesel oil contaminated product apparatus structure synoptic diagram and schematic flow sheet;
Fig. 2 is the present invention low boil gasoline output apparatus structure synoptic diagram and schematic flow sheet;
Fig. 3 is the present invention's distillation, fractionated vapour, diesel oil tripping device structural representation and schematic flow sheet.
Embodiment of the present invention are described with reference to the accompanying drawings.The method and apparatus of a kind of plastic waste, waste rubber preparing petroleum products, raw material comprises: the waste of polyethylene, polypropylene, polybutene, polystyrene, polyester and natural rubber goods.Raw material is removed silt through sub-sieve, paper, cloth, metal impurities, and the plastics effective content reaches 90% substantially, and waste rubber is broken into the 50-80mm fritter after removing metal.The overheated cylinder stock oil of medium deep fat 64# with about 300 ℃ of oil temperature, squeeze into the chuck and the inner coil pipe heating melting still of oil bath melting still with circulating oil pump, in still, add plastic waste, 200-250 ℃ of still temperature plastics are carried out fusion under the normal pressure, wait to hold and melt the plastics liquid level and be higher than in the melting still behind the separation net, start stirring, and open the deep fat valve of the chuck of feed screw 2, make the feeding route of feed screw 2 be preheated to 250 ℃.Start feed screw 2, open melting still 1 bottom valve and cracking still 3-1,3-2 feed valve, the catalyzer that adds the 0.01-1% of the waste rubber of this still volumetrical 0-50% and plastic waste gross weight in cracking still 3-1, the 3-2 in advance, and build to light a fire under the normal pressure and be warmed to 250-400 ℃, when continuously advancing the plastic waste fused solution, keep the cracking still temperature at 300-350 ℃ and start stirring, plastic waste and waste rubber promptly in cracking still 8-1,3-2 constantly cracking produce the petrol and diesel oil mixed gas.Catalyzer is the hopcalite of zinc, aluminium, nickel metallic element, and the per-cent that respectively accounts for the catalyzer total amount is ZnO:20-40%, r-Al
2O
3: 40-60%, NiO:10-20%.After petrol and diesel oil mixed gas process cracking still 3-1, the fly-ash separator dedusting of 3-2 top, entering skin has the first-stage condenser 6-1 of condensate pipe, 6-2, a part is condensed into 80 ℃ of liquid and enters contaminated product medial launder 7-1,7-2, water from 7-1, the eliminating of 7-2 bottom, and oil is interior standby to contaminated product basin 8 from 7-1, the outlet overflow of 7-2 middle and upper part.Uncondensed gas is from 6-1, in discharging and enter, top, 6-2 lower end is provided with the secondary condenser 10-1 of condensation water channel, between the 10-2 tubulation, the liquid that is chilled to room temperature is from 10-1, bottom, 10-2 upper end stream is from the low gasoline tundish 11-1 that boils, 11-2, from 11-1, the overflow of 11-2 middle and upper part enters the middle and lower part (being incorporated with the sulfuric acid liquid of half tower height degree among the washing tower 12-1 in advance) of washing tower 12-1, enter washing tower 12-2 middle and lower part from the overflow of 12-1 middle and upper part, pack in advance among the 12-2 sodium hydroxide solution of half tower height degree enters the low gasoline basin 14 that boils from washing tower 12-2 middle and upper part overflow again and stores standby.Coagulating gas among condenser 10-1, the 10-2 comes out to enter volume tank 13-1 from top, 10-1,10-2 upper end, below the 13-2 water surface, entering to burn the cracking still process furnace from top outlet eliminating again and utilizing.Because operate continuously melting still 1 needs to replenish adding plastic waste raw material, therefore need make-up catalyst, feed screw 2 rear portions are provided with the make-up catalyst charging opening, and from then on charging opening stably carries out to guarantee scission reaction by the 0.01-1% make-up catalyst of the weight that adds raw material.Residue reaches some amount and will produce detrimentally affect to scission reaction in cracking still 3-1, the 3-2, stops charging, keeps cracking temperature to rise to 400 ℃ gradually, waits and does not have the oil outflow substantially, gas generatedly stops stove fire when minimum, is cooled to naturally about 300 ℃.Start spiral tapping machine 4-1,4-2 when at this moment agitator stirs among cracking still 3-1, the 3-2, and open residual cake valve, residue in the still is discharged in storage slag cylinder 5-1, the 5-2, open the cooling water temperature of storage slag ladle external jacket, close residual cake valve and spiral tapping machine 5-1,5-2 when deslagging finishes, at this moment can continue to throw waste rubber and catalyzer in the cracking still 3-2 and send into the above operation of plastics fused solution repetition.Cracking system equipment of the present invention is two covers, can switch when purpose is slagging-off, uses an other cover cracking system, with carrying out continuously of guaranteeing to produce.Its technical process and equipment configuration structure are as shown in Figure 1 and Figure 2.Mixing oil in the contaminated product basin 8, in oil pump 9 input still kettles 15, utilize the thermal oil coil pipe in the still kettle 15 to be heated to about 200 ℃, vaporised gas through 16 fractionation of two-stage separation column enter one-level, secondary condenser 19-1,19-2 are chilled to room temperature, boiling point 190 ℃ with interior be gasoline.Treat to open the primary fractionator outlet valve when gasoline goes out to the greatest extent substantially, open still kettle 15 hot-oil jacket and be warming up to 320 ℃ gradually, steam diesel oil and be chilled to room temperature through one-level, two utmost point condenser 17-1,17-2.The gasoline that comes out from secondary condenser 19-2 enters into gasoline basin 21 after washing tower 20-1,20-2 washing standby.The diesel oil that comes out from secondary condenser 17-2 enters diesel storing and is processed oil after washing tower 18-1,18-2 washing, as shown in Figure 3.To hang down in the gasoline basin 14 that boils the low gasoline proportionality that boils and allocate into in the gasoline basin 21, and add the certain proportion additive and be gasoline product.Still kettle 15 distilled gasolines when diesel oil reaches a certain amount of, will accumulate the promptly smoked oil of a certain amount of high oil that boils, and it be emitted from still kettle 15 bottoms with pump squeeze into the plastics melting still 1 with the plastics melting, and this will improve smelting efficiency, also reduce the generation of refuse.
Embodiment 1
Plastic waste 200Kg behind sub-sieve adds in the melting still, and normal pressure keeps 210 ℃ of melting still temperature, and plastics are through fusion, stirring, preheating feed screw to 250 ℃, and unlatching feed screw and melting still bottom valve, the plastics fused solution is sent into cracking still.Preset 0.02% catalyzer of the fritter waste rubber of this still volume 10% and plastic waste amount in the cracking still, normal pressure keeps 280 ℃ of cracking still temperature down, carries out catalytic pyrolysis with the plastics liquation of sending into.Catalyzer by ZnO be 40%, r-Al
2O
3Be 50%, NiO 10% forms.The cracked mixed gas is condensed to 80 ℃ liquid mixing oil through first-stage condenser, stores standby by the contaminated product basin.Coagulate gas and be cooled to the liquid of room temperature, obtain the low gasoline that boils through washing tower washing back, with hanging down the gasoline tank storage of boiling through secondary condenser.Mixing oil is squeezed in the still kettle through oil pump in the contaminated product basin, is heated to 200 ℃ of left and right sides vaporised gas through the fractionation of two-stage separation column, is cooled to room temperature by the condensed in two stages device, obtains gasoline through the washing tower washing, sends into into gasoline tank and stores.Still kettle temperature rise to 320 ℃ vaporised gas is cooled to room temperature through the condensed in two stages device, and the washing tower washing obtains finished diesel fuel.To hang down the gasoline proportionality that boils allocates into into and obtains gasoline product in the gasoline.In the melting still continuous smelting plastic waste, the melting still adds new plastic waste, adds inlet by 0.02% make-up catalyst from the feed screw rear portion that adds amount of plastic simultaneously and replenishes the adding catalyzer.
Embodiment 2
Plastic waste 500Kg adds in the melting still, normal pressure keeps 230 ℃ of melting still temperature, presetting the fritter waste rubber in the cracking still is this still volumetrical 20%, catalyzer is 0.2% of a plastic waste amount, normal pressure heats up and keeps 350 ℃ of cracking still temperature, carry out cracking with the molten plastic liquid of sending into by the feed screw of 250 ℃ of preheatings, catalyzer by ZnO be 20%, r-Al
2O
3Be 60%, NiO 20% forms.The mixed gas that cracking goes out obtains gasoline product, diesel oil after by identical technical process of embodiment 1 and device processes.
Embodiment 3
Plastic waste 1000Kg adds in the melting still, normal pressure keeps 250 ℃ of melting still temperature that plastics are carried out melting, presetting fritter rubber in the cracking still is this still volumetrical 50%, catalyzer is 0.8% of a plastic waste amount, keep useless 380 ℃ of cracking still normal pressure temperature, the plastics fused solution of sending here with feed screw insulation carries out cracking in cracking still, catalyzer by ZnO be 30%, r-Al
2O
3Be 55%, NiO 15% forms.The mixed gas that cracking goes out obtains gasoline product, diesel oil after by identical technical process of embodiment 1 and device processes.
Claims (2)
1. the method for a plastic waste, waste rubber preparing petroleum products comprises catalytic pyrolysis, condensation, fractionation, washing, purifying, interpolation auxiliary agent, it is characterized in that:
A). plastic waste directly adds in the oil bath melting still behind artificial sub-sieve silt, is smelted into the molten shape liquid of plastics under normal pressure 200-250 ℃ temperature, sends into cracking still through feed screw and carries out cracking;
B). be added with the catalyzer of the 0.1-1% of the waste rubber that is fractured into the 50-80mm fritter of the 0-50% that accounts for total volume and raw material gross weight in the cracking still, under normal pressure 250-400 ℃ condition, stir catalytic pyrolysis with the molten shape liquid of the plastic waste of sending here from the melting still;
C). catalyzer is the hopcalite of zinc, aluminium, nickel metallic element, and the per-cent that respectively accounts for the catalyzer total amount is ZnO:20-40%, r-Al
2O
3: 40-60%, NiO:10-20%, the 0.01-1% that presses for the first time the raw material gross weight adds cracking still, thereafter the 0.01-1% that adds the amount of plastic waste according to oil bath melting still adds from the make-up catalyst charging opening at feed screw rear portion, sends into cracking still with the molten shape liquid of plastics;
D). 80 ℃ of condensed gas in the petrol and diesel oil mixed gas that the cracking still cracking produces are through the fractionation of still kettle two-stage separation column, carry out one-level, secondary condenser respectively and are condensed to that room temperature is carried out vapour, diesel oil separates.
2. press the device of the method for the described plastic waste of claim 1, waste rubber preparing petroleum products, form, it is characterized in that by cracking still, storage slag ladle, condenser, still kettle, separation column, washing tower, storage tanker:
A). an oil bath melting still is arranged, the still wall has chuck, and inner coil pipe is arranged in the still, and chuck all has valve to be connected with thermal medium oil transport pipe with inner coil pipe, thermal medium oil adopts the overheated cylinder stock oil of 62#, squeeze into melting still chuck and inner coil pipe by circulating oil pump, in the melting still agitator is arranged, the agitator central shaft passes melting still top, rotate by motor drives, separation net is arranged at melting still bottom, places plastic waste on the net, and melting still bottom valve is connected with the screw feeding machine inlet capable;
B). a feed screw is arranged at the bottom of the melting still, opening for feed is connected with melting still bottom valve, discharge port is connected with the cracking still feed valve, skin has insulation jacket, deep fat valve on the insulation jacket is connected with thermal medium oil transport pipe, and the feed screw rear portion also is provided with a make-up catalyst charging opening that can add catalyzer at any time in the ratio that adds raw material weight;
C). spiral tapping machine is equipped with in the bottom of cracking still, and residual cake valve is connected with the storage slag ladle, and the storage slag ladle is provided with chuck outward and is connected with water-cooled tube.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN99114853A CN1101450C (en) | 1999-05-06 | 1999-05-06 | Process and apparatus for preparing petroleum products from waste plastics and rubber |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN99114853A CN1101450C (en) | 1999-05-06 | 1999-05-06 | Process and apparatus for preparing petroleum products from waste plastics and rubber |
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| CN1236804A true CN1236804A (en) | 1999-12-01 |
| CN1101450C CN1101450C (en) | 2003-02-12 |
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| CN99114853A Expired - Fee Related CN1101450C (en) | 1999-05-06 | 1999-05-06 | Process and apparatus for preparing petroleum products from waste plastics and rubber |
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Cited By (12)
| Publication number | Priority date | Publication date | Assignee | Title |
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| WO2002057391A1 (en) * | 2001-01-22 | 2002-07-25 | Chen, Yanping | Method and system of converting waste plastics into hydrocarbon oil |
| WO2002061015A1 (en) * | 2001-01-29 | 2002-08-08 | Umesh Arun Zadgaonkar | A process and apparatus for manufacture of liquid fuel from waste plastic and refinery waste |
| WO2007038903A1 (en) * | 2005-10-06 | 2007-04-12 | Green Pluslink Company Limited | An industrially continuous pyrolysis equipment for waste and old tyre |
| CN100441664C (en) * | 2005-11-16 | 2008-12-10 | 张展洪 | Method of preparing boiler fuel from metal bath cracking waste tyre rubber and plastics |
| CN101892062A (en) * | 2010-07-23 | 2010-11-24 | 欧阳林 | Rotary continuous catalytic pyrolysis equipment and process |
| CN102464991A (en) * | 2010-11-16 | 2012-05-23 | 李栋 | Environment-friendly continuous-mode oil refining method |
| CN102585872A (en) * | 2011-11-30 | 2012-07-18 | Enfc株式公司 | Oil production system using waste material and catalyst thereof |
| CN102925189A (en) * | 2012-11-23 | 2013-02-13 | 韩玉龙 | Internal heating spiral propulsion type waste plastic cracking device |
| CN103614159A (en) * | 2013-11-26 | 2014-03-05 | 杨金国 | Tire oil purifying device and method |
| CN104479721A (en) * | 2014-12-29 | 2015-04-01 | 江苏健神生物农化有限公司 | Fuel oil preparation technique utilizing waste plastics |
| CN104560099A (en) * | 2014-12-29 | 2015-04-29 | 江苏健神生物农化有限公司 | Preparation technology for preparing fuel oil by utilizing waste rubber |
| WO2018195997A1 (en) * | 2017-04-28 | 2018-11-01 | 陈颂华 | Polystyrene foam densification recycling apparatus and method of operation thereof |
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| CN1123822A (en) * | 1995-07-24 | 1996-06-05 | 宋俊儒 | Method and apparatus for producing petroleum products from mixture of waste plastics and rubbers |
| CN1201064A (en) * | 1997-05-29 | 1998-12-09 | 王飞鹏 | Technology and catalyst for producing fuel oil using waste plastics |
| CN1106441C (en) * | 1997-06-06 | 2003-04-23 | 李万春 | Method for producing diesel oil and gasoline from waste rubber |
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1999
- 1999-05-06 CN CN99114853A patent/CN1101450C/en not_active Expired - Fee Related
Cited By (15)
| Publication number | Priority date | Publication date | Assignee | Title |
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| 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 |
| WO2002061015A1 (en) * | 2001-01-29 | 2002-08-08 | Umesh Arun Zadgaonkar | A process and apparatus for manufacture of liquid fuel from waste plastic and refinery waste |
| WO2007038903A1 (en) * | 2005-10-06 | 2007-04-12 | Green Pluslink Company Limited | An industrially continuous pyrolysis equipment for waste and old tyre |
| CN100441664C (en) * | 2005-11-16 | 2008-12-10 | 张展洪 | Method of preparing boiler fuel from metal bath cracking waste tyre rubber and plastics |
| CN101892062A (en) * | 2010-07-23 | 2010-11-24 | 欧阳林 | Rotary continuous catalytic pyrolysis equipment and process |
| CN102464991A (en) * | 2010-11-16 | 2012-05-23 | 李栋 | Environment-friendly continuous-mode oil refining method |
| WO2012065342A1 (en) * | 2010-11-16 | 2012-05-24 | Li Dong | Environment-friendly method for refining oil continuously |
| CN102585872A (en) * | 2011-11-30 | 2012-07-18 | Enfc株式公司 | Oil production system using waste material and catalyst thereof |
| CN102585872B (en) * | 2011-11-30 | 2016-06-01 | 韩国燃油之城股份有限公司 | Use oily production system and the catalyst thereof of useless raw material |
| CN102925189A (en) * | 2012-11-23 | 2013-02-13 | 韩玉龙 | Internal heating spiral propulsion type waste plastic cracking device |
| CN103614159A (en) * | 2013-11-26 | 2014-03-05 | 杨金国 | Tire oil purifying device and method |
| CN104479721A (en) * | 2014-12-29 | 2015-04-01 | 江苏健神生物农化有限公司 | Fuel oil preparation technique utilizing waste plastics |
| CN104560099A (en) * | 2014-12-29 | 2015-04-29 | 江苏健神生物农化有限公司 | Preparation technology for preparing fuel oil by utilizing waste rubber |
| WO2018195997A1 (en) * | 2017-04-28 | 2018-11-01 | 陈颂华 | Polystyrene foam densification recycling apparatus and method of operation thereof |
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| CN1101450C (en) | 2003-02-12 |
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