CN1236016C - Method and device for producing vapour, coal, diesel oil using waste plastic, rubber, machine oil - Google Patents
Method and device for producing vapour, coal, diesel oil using waste plastic, rubber, machine oil Download PDFInfo
- Publication number
- CN1236016C CN1236016C CN 03146751 CN03146751A CN1236016C CN 1236016 C CN1236016 C CN 1236016C CN 03146751 CN03146751 CN 03146751 CN 03146751 A CN03146751 A CN 03146751A CN 1236016 C CN1236016 C CN 1236016C
- Authority
- CN
- China
- Prior art keywords
- gasoline
- oil
- diesel oil
- kerosene
- tower
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired - Fee Related
Links
- 239000002283 diesel fuel Substances 0.000 title claims abstract description 34
- 238000000034 method Methods 0.000 title claims abstract description 33
- 239000002699 waste material Substances 0.000 title claims abstract description 29
- 239000004033 plastic Substances 0.000 title claims abstract description 24
- 229920003023 plastic Polymers 0.000 title claims abstract description 24
- 239000005060 rubber Substances 0.000 title claims abstract description 13
- 239000010721 machine oil Substances 0.000 title claims description 7
- 239000003245 coal Substances 0.000 title claims description 6
- 239000003502 gasoline Substances 0.000 claims abstract description 34
- 238000005336 cracking Methods 0.000 claims abstract description 29
- 239000003350 kerosene Substances 0.000 claims abstract description 20
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 14
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims description 39
- 239000003921 oil Substances 0.000 claims description 31
- 238000000926 separation method Methods 0.000 claims description 21
- 235000017166 Bambusa arundinacea Nutrition 0.000 claims description 14
- 235000017491 Bambusa tulda Nutrition 0.000 claims description 14
- 241001330002 Bambuseae Species 0.000 claims description 14
- 235000015334 Phyllostachys viridis Nutrition 0.000 claims description 14
- RTAQQCXQSZGOHL-UHFFFAOYSA-N Titanium Chemical compound [Ti] RTAQQCXQSZGOHL-UHFFFAOYSA-N 0.000 claims description 14
- 239000011425 bamboo Substances 0.000 claims description 14
- 239000010941 cobalt Substances 0.000 claims description 14
- 229910017052 cobalt Inorganic materials 0.000 claims description 14
- GUTLYIVDDKVIGB-UHFFFAOYSA-N cobalt atom Chemical compound [Co] GUTLYIVDDKVIGB-UHFFFAOYSA-N 0.000 claims description 14
- 238000006277 sulfonation reaction Methods 0.000 claims description 14
- 239000010936 titanium Substances 0.000 claims description 14
- 229910052719 titanium Inorganic materials 0.000 claims description 14
- MHAJPDPJQMAIIY-UHFFFAOYSA-N Hydrogen peroxide Chemical compound OO MHAJPDPJQMAIIY-UHFFFAOYSA-N 0.000 claims description 12
- 239000000243 solution Substances 0.000 claims description 11
- 238000007233 catalytic pyrolysis Methods 0.000 claims description 9
- 239000000571 coke Substances 0.000 claims description 9
- 238000005194 fractionation Methods 0.000 claims description 9
- 239000012535 impurity Substances 0.000 claims description 9
- 239000002994 raw material Substances 0.000 claims description 9
- 239000007864 aqueous solution Substances 0.000 claims description 8
- 239000007789 gas Substances 0.000 claims description 8
- 238000004519 manufacturing process Methods 0.000 claims description 8
- 238000001914 filtration Methods 0.000 claims description 7
- 239000011044 quartzite Substances 0.000 claims description 7
- 239000004576 sand Substances 0.000 claims description 7
- 238000004062 sedimentation Methods 0.000 claims description 7
- CIWBSHSKHKDKBQ-JLAZNSOCSA-N Ascorbic acid Chemical compound OC[C@H](O)[C@H]1OC(=O)C(O)=C1O CIWBSHSKHKDKBQ-JLAZNSOCSA-N 0.000 claims description 4
- 239000003463 adsorbent Substances 0.000 claims description 4
- 239000003054 catalyst Substances 0.000 claims description 4
- 239000007788 liquid Substances 0.000 claims description 4
- 239000000463 material Substances 0.000 claims description 4
- 239000002808 molecular sieve Substances 0.000 claims description 4
- 238000005554 pickling Methods 0.000 claims description 4
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 claims description 4
- 239000010913 used oil Substances 0.000 claims description 4
- 239000003513 alkali Substances 0.000 claims description 3
- 238000004140 cleaning Methods 0.000 claims description 3
- 239000004615 ingredient Substances 0.000 claims description 3
- 238000004523 catalytic cracking Methods 0.000 claims description 2
- 239000011259 mixed solution Substances 0.000 claims description 2
- 238000007670 refining Methods 0.000 abstract description 9
- 238000012856 packing Methods 0.000 abstract description 4
- 239000000295 fuel oil Substances 0.000 abstract description 2
- 239000013043 chemical agent Substances 0.000 abstract 1
- 238000011038 discontinuous diafiltration by volume reduction Methods 0.000 abstract 1
- 239000010705 motor oil Substances 0.000 abstract 1
- 239000003209 petroleum derivative Substances 0.000 abstract 1
- 239000010453 quartz Substances 0.000 abstract 1
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N silicon dioxide Inorganic materials O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 abstract 1
- 238000009833 condensation Methods 0.000 description 6
- 230000005494 condensation Effects 0.000 description 6
- 238000005516 engineering process Methods 0.000 description 5
- 238000010521 absorption reaction Methods 0.000 description 4
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 3
- 238000001816 cooling Methods 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 241000282326 Felis catus Species 0.000 description 2
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 2
- 238000006555 catalytic reaction Methods 0.000 description 2
- 230000033001 locomotion Effects 0.000 description 2
- 230000000630 rising effect Effects 0.000 description 2
- 239000002594 sorbent Substances 0.000 description 2
- JIAARYAFYJHUJI-UHFFFAOYSA-L zinc dichloride Chemical compound [Cl-].[Cl-].[Zn+2] JIAARYAFYJHUJI-UHFFFAOYSA-L 0.000 description 2
- 241000370738 Chlorion Species 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
- 239000004480 active ingredient Substances 0.000 description 1
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 1
- 238000004939 coking Methods 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000002309 gasification Methods 0.000 description 1
- 229910052500 inorganic mineral Inorganic materials 0.000 description 1
- 229910052742 iron Inorganic materials 0.000 description 1
- 239000011707 mineral Substances 0.000 description 1
- 235000010755 mineral Nutrition 0.000 description 1
- TVMXDCGIABBOFY-UHFFFAOYSA-N octane Chemical compound CCCCCCCC TVMXDCGIABBOFY-UHFFFAOYSA-N 0.000 description 1
- 239000013502 plastic waste Substances 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 239000004575 stone Substances 0.000 description 1
- 239000008399 tap water Substances 0.000 description 1
- 235000020679 tap water Nutrition 0.000 description 1
- 238000010792 warming Methods 0.000 description 1
- 239000011592 zinc chloride Substances 0.000 description 1
- 235000005074 zinc chloride Nutrition 0.000 description 1
Images
Landscapes
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The present invention relates to a method and a device for producing gasoline, kerosene and diesel oil by using waste plastics, rubber and engine oil. The device orderly comprises a cracking kettle, a fixed bed, a packing tower and a fractionating tower, wherein the top of the fractionating tower is connected to a gasoline fraction quencher which is orderly connected with a condenser, an oil-water separator, a filter and a gasoline refining tower; the gasoline refining tower is orderly connected to the filter and a finished product tank; the kerosene fraction at the middle part of the fractionating tower and the diesel oil fraction at the lower part are respectively and orderly connected to the condenser, the oil-water separator, the filter and the refining tower; heavy oil components at the tower bottom of the fractionating tower are returned to the cracking kettle. The present invention adopts quartz and sandstones in cracking; the fixed bed adopts a one-step method; chemical agents for removing taste and changing color are added to the fractionating process. The present invention has the advantages of small investment for equipment, volume reduction, simple work procedure and shortened productive period; obtained petroleum products have good quality and high yield.
Description
Technical field
The present invention relates to utilize depleted plastics, rubber, machine oil to produce the method and the device of vapour, coal, diesel oil.
Background technology
Utilize the technical approach of waste plastic extracting gasoline, kerosene, diesel oil many, make waste plastic obtain recycling, turn waste into wealth.Generally be that plastic waste is carried out catalytic pyrolysis, each component of fractionation then.No matter but any technical approach all exists the oil quality that obtains poor, the disadvantage that the production cycle is long, so that influenced applying of technology.
Summary of the invention
It is good that technical problem to be solved by this invention provides a kind of production oil quality, and utilize depleted plastics, rubber or machine oil with short production cycle are produced the method for vapour, coal, diesel oil.
The method of utilizing depleted plastics, rubber or machine oil to produce vapour, coal, diesel oil of the present invention is characterized in that: comprising:
(1) adds the quartzite and the grains of sand in the scrap feed material, under 50～480 ℃, carry out catalytic pyrolysis, the add-on of quartzite is 0.3～1.5% of a cracking stock weight, the add-on of the grains of sand is 0.1～0.5% of a cracking stock weight, and described scrap feed material comprises waste plastic or contains the raw material of waste plastic, waste rubber or used oil;
(2) gaseous fraction that obtains of cracking further catalytic cracking in fixed bed, obtain product vapour, described cracked gas is process coke layer removal of impurities earlier in fixed bed, pass through Pall ring, adsorbent layer, catalyst layer then successively, the thickness of coke layer is 20～50 centimetres, and catalyzer adopts the 5A molecular sieve;
(3) product vapour carries out fractionation, collect gasoline, kerosene, diesel oil distillate respectively, add sulfonation titanium mountain valley with clumps of trees and bamboo cobalt, sodium hydroxide, hydrogen peroxide mixed solution in the fractionation process, added in separation column every 5～8 hours: the aqueous solution of 200ppm sulfonation titanium mountain valley with clumps of trees and bamboo cobalt, the aqueous solution of sulfonation titanium mountain valley with clumps of trees and bamboo cobalt is just lysigenous by sulfonation titanium mountain valley with clumps of trees and bamboo cobalt and water; 10% sodium hydroxide solution 1.5kg; 10% hydrogen peroxide 3 ‰, the sodium hydroxide solution amount in 10%;
Gasoline, kerosene, diesel oil distillate are made with extra care respectively.
Catalytic pyrolysis carries out in cracking still in above-mentioned (1) step, the quartzite and the grains of sand in following cracking process earlier 100 ℃ of left and right sides parallel motions, curved operation when reaching 150 ℃, translational motion up and down in the time of 250 ℃, its course of action
The one, play and accelerate the cracked effect; The 2nd, to the raw material reaming, work to get through passage; The 3rd, remove the iron component in the raw material, improve oil quality; The 4th, reduce the coking of cracking still; The 5th, help improving the yield of oil product; The 6th, shorten the production cycle.Particularly the ferro element in the raw material is removed, this is that prior art institute is insurmountable, and the existence one of ferro element is that equipment is had infringement, the 2nd, easily combine with chlorion, and produce impurity, influence the quality of oil product.Cracking stock one of the present invention is directly to utilize waste plastic (all available except that igelite), waste rubber, the 2nd, be main raw material with the waste plastic, in the prior art all disclosed be that the batching of raw material all can with the waste plastic.The needed catalyzer of cracking is according to the disclosed various components of prior art.Cracking temperature is temperature-rise period gradually, just collects these gas fractions from beginning have gas fraction to produce beginning.The catalytic pyrolysis temperature is concerning waste plastic, and optimal temperature is 60～460 ℃, and concerning waste rubber, optimal temperature is 80～480 ℃, and concerning used oil, optimal temperature is 50～380 ℃.
The gas fraction that produces from cracking still enters the further catalysis of fixed bed, cracking, absorption, two fixed beds of the general employing of prior art, carry out according to the two-step approach operation, the present invention adopts one-step technology, promptly adopt a fixed bed, cracked gas earlier through a coke layer removal of impurities, passes through Pall ring, adsorbent layer, catalyst layer then successively in fixed bed, the thickness of coke layer is 20～50 centimetres, and catalyzer adopts common 5A molecular sieve.The present invention has at first passed through a coke layer in fixed bed, removes impurity, so only need adopt a fixed bed can reach requirement.The catalysis that is taken place in fixed bed, cracking, absorption are according to the prior art mode.
Through the gaseous fraction that obtains behind the fixed bed, preferably, gas is filtered once more through a packing tower, absorption impurity carries out fractionation then.Fractionation is carried out in separation column, and the cut that cat head is 195～198 ℃ is a gasoline fraction, and the cut that the middle part is 200～230 ℃ is a kerosene(oil)fraction, and the cut that the bottom is 300～360 ℃ is a diesel oil distillate.For the undesirable taste of removing each oil product that obtains and the transparency that changes oil product, in fractionation process, in separation column, added every 5～8 hours: the aqueous solution of 200ppm sulfonation titanium mountain valley with clumps of trees and bamboo cobalt, the aqueous solution of sulfonation titanium mountain valley with clumps of trees and bamboo cobalt is just lysigenous by sulfonation titanium mountain valley with clumps of trees and bamboo cobalt and water; 10% sodium hydroxide solution 1.5kg; 10% hydrogen peroxide 3 ‰, the sodium hydroxide solution amount in 10%.
The gasoline fraction that fractionates out is earlier through condensation, be condensed to 160～180 ℃, liquid ingredient returns separation column, through being condensed to 30～60 ℃, oily water separation is carried out in sedimentation to gaseous fraction then again, and oil product more after filtration, at last gasoline is made with extra care under 30～50 ℃, add atlapulgite in the treating process, its amount is: 1～5% of gasoline weight, promptly produce the atlapulgite that 1 ton of gasoline adds 0.01～0.05 ton.The effect of atlapulgite is removal of impurities and the color that changes gasoline, increase transparency, boosting of octane rating.
The diesel oil distillate that fractionates out is earlier through condensation, sedimentation, filtration, make with extra care at last, 2～5% 98% the vitriol oil that adds diesel oil distillate weight in the treating process earlier carries out pickling, 1～3% 96% the sodium hydroxide solution that adds diesel oil distillate weight then carries out alkali cleaning, adds the cetane number booster of 1 of diesel oil distillate weight～5 ‰ at last.Can improve diesel-fuel cetane number like this.
The kerosene(oil)fraction that fractionates out carries out routine at last and makes with extra care earlier through condensation, sedimentation, filtration in treating tower.
Realize a whole set of production equipment of above-mentioned technology, comprise cracking still successively, fixed bed, packing tower, separation column, the cat head of separation column is by pipe connection gasoline fraction quencher, quencher connects condenser, condenser connects water-and-oil separator, water-and-oil separator connects strainer, strainer connects the gasoline refining tower, the gasoline refining tower connects strainer successively, the finished product jar, the middle part kerosene(oil)fraction of separation column connects condenser successively, water-and-oil separator, strainer, the kerosene treating tower, the kerosene treating tower connects strainer successively, the finished product jar, the bottom diesel oil distillate of separation column connects condenser successively, water-and-oil separator, strainer, the diesel refining tower, the diesel refining tower connects strainer successively, the finished product jar is connected to cracking still by pipeline at the bottom of the tower of separation column.
Described quencher is that gasoline fraction is carried out condensation, is the jar shape, comprises inlet tube and outlet tube, spiral coil cooling tube, and the quencher top sets out oil pipe (entering condenser), the bottom is provided with " U " shape return line that feeds in the separation column.
Advantage of the present invention:
It is more that whole technology is removed being provided with of impurity, not only guaranteed quality product, and facility investment is simple, volume can dwindle, and the production cycle has been shortened in work simplification.The oil quality that obtains is good: the transparency height, can arrive the same effect of mineral water, and sulphur content is low, belongs to white gasoline, can reach GB 93# gasoline standard.The yield height, the amount of the total oil product that obtains is 65% of a waste plastic weight, if produce with waste oil, yield can reach 80～83%.Pollution-free, waste plastic, rubber need not clean directly into cracking still, have overcome that prior art need be cleaned and the deficiency of wasting a large amount of clear water can be produced the waste liquid gasification, as energy utilization in the production process.The present invention is particularly useful for the processing to waste plastic.
Description of drawings
Fig. 1 is technical process of the present invention and device synoptic diagram;
Fig. 2 is the structural representation of quencher.
Among the figure: 1 spiral coil cooling tube, 2 flanges, 3 Inlet and outlet water valves, 4 rising pipes, 5 water inlet pipes, 6 light benzine oil outlet pipe 7 " U " type return lines, 8 flanges
Embodiment
Below describe the present invention in detail with waste plastic, but do not limit the present invention.
Waste plastic enters cracking still, carries out catalytic pyrolysis in cracking still, and catalyzer is adsorbed on the active ingredient zinc chloride on the particulate state alumina carrier with pickling process and makes.Temperature in the kettle is warming up to 460 ℃ gradually from normal temperature, collects gaseous fraction since 60 ℃.Add the quartzite and the grains of sand with raw material in cracking still, quartzite is 1% of a cracking stock weight, and the grains of sand are 0.2% of cracking stock weight.The gas fraction that the process cracking obtains, enter fixed bed, interior coke layer, Pall ring, adsorbent layer, the catalyst layer of upwards being followed successively by from the bottom of fixed bed, the thickness of coke layer is 20～50 centimetres, sorbent material adopts stone bar sorbent material, thickness is 60～100 centimetres, and catalyzer adopts the 5A molecular sieve, and thickness is 80～120 centimetres.Gaseous fraction through obtaining behind the fixed bed enters packing tower, and gaseous fraction is filtered once more, and absorption impurity enters separation column then.The cut that fractionator overhead is 195～198 ℃ is a gasoline fraction, and the cut that the middle part is 200～230 ℃ is a kerosene(oil)fraction, and the cut that the bottom is 300～360 ℃ is a diesel oil distillate.Injected every 5～8 hours to separation column from the top of separation column: the aqueous solution of 200ppm sulfonation titanium mountain valley with clumps of trees and bamboo cobalt, the aqueous solution of sulfonation titanium mountain valley with clumps of trees and bamboo cobalt is just lysigenous by sulfonation titanium mountain valley with clumps of trees and bamboo cobalt and water; 10% sodium hydroxide solution 1.5kg; 10% hydrogen peroxide 3 ‰, the sodium hydroxide solution amount in 10%.Be that heavy oil component returns cracking still and refines at the bottom of the tower of separation column.
The gasoline fraction that fractionates out enters quencher (as Fig. 2), feed tap water in the quencher, be condensed to 160～180 ℃, liquid ingredient returns separation column by " U " shape return line and continues fractionation, gaseous fraction enters condenser condenses to 30～60 ℃ again by pipeline (light benzine oil outlet pipe 6), enter water-and-oil separator then, oily water separation is carried out in sedimentation, oil product enters strainer again and filters, the most laggard treating tower is made with extra care under 30～50 ℃ gasoline, add atlapulgite in the treating process, its amount is: produce 1 ton of gasoline and add 1～5% atlapulgite.Gasoline after refining enters the finished product jar after filtration.
The kerosene(oil)fraction that fractionates out carries out routine refining (kerosene directly enters condenser among Fig. 1, need not enter quencher) at last earlier through condensation, sedimentation, filtration in treating tower.
The diesel oil distillate that fractionates out still passes through condensation, sedimentation, filtration earlier, make with extra care at last, 2～5% 98% the vitriol oil that adds diesel oil distillate weight in the treating process earlier carries out pickling, 1～3% 96% the sodium hydroxide solution that adds diesel oil distillate weight then carries out alkali cleaning, adds the cetane number booster of 1 of diesel oil distillate weight～5 ‰ at last.
As Fig. 2, quencher comprises water inlet pipe 5, rising pipe 4, two flanges 8 and two flange intermediary spiral coil cooling tubes 1, and the quencher top is provided with light benzine oil outlet pipe 16 and enters condenser, bottom and be provided with and feed separation column tower intravital " U " shape return line 7.
The device and the working process of producing gasoline, diesel oil, kerosene with waste old and used oil are the same.
Claims (8)
1, a kind of method of utilizing depleted plastics, rubber or machine oil to produce vapour, coal, diesel oil is characterized in that: comprising:
(1) adds the quartzite and the grains of sand in the scrap feed material, under 50～480 ℃, carry out catalytic pyrolysis, the add-on of quartzite is 0.3～1.5% of a cracking stock weight, the add-on of the grains of sand is 0.1～0.5% of a cracking stock weight, and described scrap feed material comprises waste plastic or contains the raw material of waste plastic, waste rubber or used oil;
(2) gaseous fraction that obtains of cracking further catalytic cracking in fixed bed, obtain product vapour, described cracked gas is process coke layer removal of impurities earlier in fixed bed, pass through Pall ring, adsorbent layer, catalyst layer then successively, the thickness of coke layer is 20～50 centimetres, and catalyzer adopts the 5A molecular sieve;
(3) product vapour carries out fractionation, collect gasoline, kerosene, diesel oil distillate respectively, add sulfonation titanium mountain valley with clumps of trees and bamboo cobalt, sodium hydroxide, hydrogen peroxide mixed solution in the fractionation process, added in separation column every 5～8 hours: the aqueous solution of 200ppm sulfonation titanium mountain valley with clumps of trees and bamboo cobalt, the aqueous solution of sulfonation titanium mountain valley with clumps of trees and bamboo cobalt is just lysigenous by sulfonation titanium mountain valley with clumps of trees and bamboo cobalt and water; 10% sodium hydroxide solution 1.5kg; 10% hydrogen peroxide 3 ‰, the sodium hydroxide solution amount in 10%;
(4) gasoline, kerosene, diesel oil distillate are made with extra care respectively.
2, method according to claim 1 is characterized in that (1) step cracking temperature is temperature-rise period gradually.
3, method according to claim 1, the cut that it is characterized in that 195～198 ℃ of (3) step fractionator overhead is a gasoline fraction, and the cut that the middle part is 200～230 ℃ is a kerosene(oil)fraction, and the cut that the bottom is 300～360 ℃ is a diesel oil distillate.
4, according to claim 1 or 3 described methods, it is characterized in that gasoline fraction is condensed to 160～180 ℃, liquid ingredient returns separation column, gaseous fraction is again through being condensed to 30～60 ℃, oily water separation is carried out in sedimentation then, and oil product is made with extra care under 30～50 ℃ gasoline more after filtration at last, add atlapulgite in the treating process, its amount is: 1～5% of gasoline weight.
5, according to claim 1 or 3 described methods, it is characterized in that diesel oil distillate makes with extra care, 2～5% 98% the vitriol oil that adds diesel oil distillate weight in the treating process earlier carries out pickling, 1～3% 96% the sodium hydroxide solution that adds diesel oil distillate weight then carries out alkali cleaning, adds the cetane number booster of 1 of diesel oil distillate weight～5 ‰ at last.
6, method according to claim 1 is characterized in that it being raw material production gasoline, kerosene, the diesel oil that utilizes waste plastic or contain waste plastic, and the catalytic pyrolysis temperature in (1) step is 60～460 ℃.
7, method according to claim 1 is characterized in that it being to utilize waste rubber to produce gasoline, kerosene, diesel oil, and the catalytic pyrolysis temperature in (1) step is 80～480 ℃.
8, method according to claim 1 is characterized in that it being to utilize discarded machine oil to produce gasoline, kerosene, diesel oil, and the catalytic pyrolysis temperature in (1) step is 50～380 ℃.
Priority Applications (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 03146751 CN1236016C (en) | 2003-04-25 | 2003-06-24 | Method and device for producing vapour, coal, diesel oil using waste plastic, rubber, machine oil |
| PCT/CN2004/000663 WO2005017069A1 (en) | 2003-06-24 | 2004-06-22 | A process and a device for producing gasoline, kerosene and diesel oil from waste plastic, rubber and machine oil |
| US10/562,370 US20060287560A1 (en) | 2003-06-24 | 2004-06-22 | Process and a device for producing gasoline, kerosene and diesel oil from waste plastic, rubber and machine oil |
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN03112347 | 2003-04-25 | ||
| CN03112347.3 | 2003-04-25 | ||
| CN 03146751 CN1236016C (en) | 2003-04-25 | 2003-06-24 | Method and device for producing vapour, coal, diesel oil using waste plastic, rubber, machine oil |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1513949A CN1513949A (en) | 2004-07-21 |
| CN1236016C true CN1236016C (en) | 2006-01-11 |
Family
ID=34276243
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 03146751 Expired - Fee Related CN1236016C (en) | 2003-04-25 | 2003-06-24 | Method and device for producing vapour, coal, diesel oil using waste plastic, rubber, machine oil |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1236016C (en) |
Families Citing this family (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EA201001602A1 (en) * | 2008-04-07 | 2011-06-30 | Рудольф В. Ганнерман Энд Питер В. Ганнерман | METHOD FOR TURNING BIOGAS TO LIQUID FUEL |
| CN101531948B (en) * | 2009-04-10 | 2012-08-29 | 熊道陵 | New technology for catalytically cracking light diesel oil from waste motor oil |
| CN101851523B (en) * | 2010-06-01 | 2013-02-20 | 上海劲飚环保科技有限公司 | Continuous waste plastics refining unit |
| CN101928585A (en) * | 2010-08-23 | 2010-12-29 | 周建华 | Equipment and process for catalyzing and purifying fuel oil under gas phase by using waste rubber and plastic and waste engine oil |
| CN102504865A (en) * | 2011-11-15 | 2012-06-20 | 安徽盈荣生物能源科技有限公司 | Method for refining diesel oil or gasoline by using waste oil |
| CN103834428A (en) * | 2014-02-28 | 2014-06-04 | 成都大漠石油机械有限公司 | Waste oil treatment system with high efficient utilization rate |
| CN103834425A (en) * | 2014-03-06 | 2014-06-04 | 周文彬 | Safe and environment-friendly oil refining equipment and technology for harmless recycling of plastic garbage |
| CN104611007B (en) * | 2015-02-25 | 2016-05-11 | 烟台荣盛压力容器制造有限公司 | A kind of waste lubricating oil refines petrol and diesel oil device |
| CN109749757A (en) * | 2017-11-06 | 2019-05-14 | 胡嘉庆 | A kind of the regeneration matter product set and its preparation method of scrap rubber/plastics |
| CN110511523A (en) * | 2019-09-06 | 2019-11-29 | 叙永智同再生科技有限公司 | Warm-mixed asphalt modifying agent and preparation method thereof |
-
2003
- 2003-06-24 CN CN 03146751 patent/CN1236016C/en not_active Expired - Fee Related
Also Published As
| Publication number | Publication date |
|---|---|
| CN1513949A (en) | 2004-07-21 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| US8366912B1 (en) | Method for producing base lubricating oil from waste oil | |
| CN1247743C (en) | Method and system for continuous production of gasoline, kerosene and diesel from waste plastics | |
| CN1236016C (en) | Method and device for producing vapour, coal, diesel oil using waste plastic, rubber, machine oil | |
| CN105198687A (en) | Options To Reduce Fouling In Mto Downstream Recovery | |
| WO2005017069A1 (en) | A process and a device for producing gasoline, kerosene and diesel oil from waste plastic, rubber and machine oil | |
| AU2013243037B2 (en) | Method for separating olefins with gentle cleavage | |
| CN1854272A (en) | Method for reducing finished product mobile oil and refining gasoline and diesel from waste mobile oil and its apparatus thereof | |
| CN111001194B (en) | High-temperature continuous ashing-free treatment method and system for catalytic cracking slurry oil | |
| CN1164547C (en) | Multi-product alcohol refining process | |
| CN1261552C (en) | Method for continuous producing fuel oil from deposed lubricant | |
| CN207628144U (en) | Containing solid hydrocarbon gas cooling purifying device | |
| CN1209441C (en) | Separation method of catalytic gasoline quality improved oil and gas and its installation | |
| US20200331169A1 (en) | Heat and Energy Integrated Continuous Process for Plastic Waste Recovery | |
| CN1342630A (en) | Process for preparing high-purity n-pentane | |
| CN1030504C (en) | Heavy oil catalytic distillation method | |
| RU2003136849A (en) | METHOD FOR TRANSFORMING HYDROCARBONS TO A FRACTION HAVING AN IMPROVED OCTAN NUMBER AND A FACTION WITH A HIGH CETANE NUMBER | |
| CN1293027C (en) | Process for preparing hydrocarbon product by synthetic gas using skeleton catalyst paste phase technology | |
| CN1233800C (en) | Method and equipment for multieffect heavy oil catalytic cracking and gasoline transnaturing | |
| CN1212371C (en) | Method and device for catalytic gasoline upgrading and olefin reduction with high light oil yield | |
| CN223163384U (en) | Waste lubricating oil regeneration device based on multistage catalytic pretreatment | |
| CN1093162C (en) | Process for producing vaseline using waste plastics as raw material | |
| CN102295942A (en) | Shale oil hermetical recovery method and device in oil shale destructive distillation system | |
| CN1160288C (en) | Rectifying and dewatering process for preparing hydrofluochloric hydrocarbon | |
| RU27082U1 (en) | INSTALLATION FOR PRODUCING ISOBUTANE FROM HYDROCARBON RAW MATERIALS | |
| RU66743U1 (en) | INSTALLING OBTAINING AN ODORANT FROM HYDROCARBONS |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20060111 |
|
| CF01 | Termination of patent right due to non-payment of annual fee |