KR20090108414A - Apparatus and method for regeneration of hydrocarbon-based organic waste as refined oil by thermal cracking process - Google Patents

Abstract

PURPOSE: A method for regenerating hydrocarbons organic waste to refined oil by a thermal decomposition process and a device thereof are provided to produce the refined oil with a single process efficiently. CONSTITUTION: A method for regenerating hydrocarbons organic waste to refined oil by a thermal decomposition process includes the following steps of: heating high-viscosity residue supplied from a pressure reducing evaporator(34); separating hydrochloric acid gas, melting fuel oil, and non-melting hardening materials; and neutralizing the hydrochloric acid gas by a neutralization reactor(10).

Description

Apparatus and method for regeneration of hydrocarbon-based organic waste as refined oil by thermal cracking process}

The present invention relates to an apparatus and method for thermally decomposing various hydrocarbon-based organic wastes such as waste lubricating oil, waste synthetic resin, and waste tires into high-quality refined oil, and more particularly, to crushing, washing, drying, etc., solid hydrocarbon-based organic wastes. In the pyrolysis refining apparatus consisting of a pre-treatment unit, a demineralizer, a pyrolyzer, a solidifier, a solid impurity discharger, a methanol reactor, and a reduced pressure re-distiller, the solid hydrocarbon-based organic waste is first desalted, and then pyrolyzed to obtain distilled oil vapor at room temperature, and Methanol diluted with water is directly reacted to condense, and the condensed mixture is stirred for a certain time to agglomerate impurities such as tar, sulfur oxides and nitrogen oxides produced during the pyrolysis process, and the oil component is distilled under reduced pressure to produce fuel oil. And high-boiling oils, which are not distilled, are initially introduced as solid hydrocarbon-based organic waste. After mixing, desalting and pyrolysis, it is recycled again to produce fuel oil. In this process, a portion of the fuel is sent to a solidifier for final pyrolysis to extract oil components, and the remainder is melt solidified and discharged to the outside. The gas relates to an apparatus and method for regenerating hydrocarbon-based organic waste into refined oil by a pyrolysis process, characterized in that the gas is used to remove impurities and use it as its own fuel.

Efforts to obtain alternative fuel oils by pyrolyzing hydrocarbon-based organic wastes such as waste lubricating oil, waste synthetic resin, and waste tires have been developed in accordance with the times. However, there are very few places currently in commercial use.

The reason is that the waste raw materials for pyrolysis to produce alternative fuel oils are the worst wastes that are not worth recycling for other purposes, and the oil is produced through the pyrolysis process, but due to the viscosity, flash point, color, odor, etc. I'm being ignored by consumers.

Decomposed oils produced from waste synthetic resins or waste tires are polymerized by polymerizing short carbon ring molecules of low molecular weight hydrocarbons. It is not suitable for burning by a combustion mechanism for burners.

Pyrolysis process is difficult to maintain the device due to high temperature corrosion of the device due to the high use temperature. Thus, problems can be solved through the use of catalysts or hydrotreating to improve the quality of products or to lower the pyrolysis temperature, but it is only a theoretical technique due to the increase of equipment cost and maintenance cost. Due to high oil prices, alternative energy is urgently needed, but it is currently not commercialized and operated because of the above reasons.

Patent registration No. 10-0565540 is to react methanol and cracked oil of more than 99% purity at high temperature and high pressure twice in order to improve the quality of pyrolysis oil, and also to remove impurities by using methanol's high dissolving power. Although many studies have been conducted in various countries, the solvent extraction process using methanol should use 200-300% solvent of the raw material oil to separate the impurities by the specific gravity from the cracked oil which is the raw material oil, and the solvent extraction process should be followed to reuse the solvent.

Patent Registration No. 10-0693464 has a problem in that since it decomposes waste oil and solid hydrocarbon waste together at the beginning of the process, it is necessary to thermally decompose the low-viscosity portion which can be distilled without first decomposing waste oil, thereby consuming unnecessary energy.

The present invention is to solve the above-mentioned problems, condensed decomposition oil in the waste oil and distilled together to make it suitable for use for diesel or kerosene burner which generally uses the viscosity and flash point of the recycled oil, using methanol In order to dissolve and flocculate impurities of pyrolysis vapor, 10-30% by weight of dilute methanol is used without using high purity. Also, the impurities are not coagulated by methanol in advance to prevent impurities from distillation under reduced pressure without phase separation. Therefore, the diluted low concentration methanol is used only about 30 to 50% by weight based on the weight of the oil vapor and the waste oil, and the waste oil is distilled first on the low viscosity portion without pyrolysis from the beginning so that the viscosity and flash point of the refined fuel oil are commercially available. It is suitable for diesel burner and does not consume unnecessary energy. There are Jing.

A demineralizer for heating high-viscosity vacuum residue from solid hydrocarbon-based organic waste and a reduced pressure distillation unit to separate chlorine gas, molten raw material oil and unmelted cured product, a neutralization reactor for neutralizing chlorine gas from the demineralizer, and the demineralizer Pyrolysis to separate the raw oil from pyrolysis to separate the distilled cracked oil and the high boiling point undecomposed high viscosity material, methanol from the methanol input machine and waste oil from the waste oil input machine and oil vapor from the pyrolysis machine were mixed and contacted. The condensed, non-condensed gas fraction goes to the upper condenser and condenses from the vapor condensation tower and the vapor condensation tower, which alternately sends a methanol mixture containing the condensed and reflux condensate to the methanol reactor. A methanol reactor for aggregating impurities by stirring the prepared methanol mixture, Methanol mixture with condensed impurities is distilled under reduced pressure in the All Reactor. The undistilled, undistilled, high-viscosity, depressurized residue oil is sent to the demineralizer, and the distillate gas is sent to the vacuum distillation condenser connected at the top. A vacuum distillation unit for use as a regenerated fuel oil, a gas purifier for dissolving uncondensed gas from a reduced pressure distillation condenser and an uncondensed gas from an oil vapor condensation reaction column in methanol to remove tar and use it as a fuel gas of its own; A solidizer which heats the coke separated from the high viscosity undigested oil and the pyrolysis heater from the pyrolyzer and sends the distilled gas back to the reflux reaction column and sends the pyrolyzed distilled solid residue powder to the coke separator, and a solidifier Of Solid Waste Powder from Water Circulation by Water Circulation Pump It is collected in the filter to remove the coke powder, and in that the gas component consists of a coke oven separator for circulating groups solidified by the gas circulation blower characterized.

As described above, according to the present invention, in the production of refined fuel oil by continuously pyrolyzing hydrocarbon-based organic waste such as waste lubricating oil, waste synthetic resin, and waste tire, the user of refined fuel oil may use commercial oil such as kerosene or diesel without modification or adjustment of burner. It is possible to produce refined fuel oil of viscosity and flash point in a single process, and in the production of oil, any process can be operated continuously from input to production without interruption, and the final residue of hydrocarbon-based organic waste is recycled to general waste. By minimizing other environmental pollution, the source of secondary pollution from pyrolysis treatment is eliminated.

Hereinafter, the configuration according to the present invention in detail with reference to the drawings.

The present invention is a device for producing refined oil of a quality suitable for use for diesel or kerosene burner by regenerating waste oil such as solid hydrocarbon-based organic waste such as waste synthetic resin, waste tire and waste lubricating oil as shown in Figures 1 to 3 The present invention relates to a demineralizer (1) for heating a high-viscosity vacuum residue from solid hydrocarbon-based organic waste and a reduced pressure distillation unit (34) to separate chlorine gas, molten raw material oil, and a non-melt hardened product, and the demineralizer (1). A neutralization reactor (10) for neutralizing chlorine gas from the reactor, a pyrolyzer (14) for thermally decomposing molten raw material oil from the demineralizer (1) into distilled cracked steam and a high boiling point undecomposed high viscosity material, The methanol from the methanol injector 25 and the waste oil from the waste oil injector 26 and the oil vapor from the pyrolyzer 14 are mixed and contacted to condense the oil vapor. Condensed methanol from the vapor condensation reaction tower 23 and the vapor condensation reaction tower 23 which condensate in the vapor condenser 24 and send the methanol mixture containing the refluxed condensate to the methanol reactors 32a and 32b alternately. Methanol reactors 32a and 32b which agitate the mixture so that impurities such as odors, pigments and tars, and the like are not distilled in the vacuum distillation unit 34 and aggregated into a polymer material, and the methanol reactors 32a and 32b. Distillation under reduced pressure distillation of the methanol mixture in which the impurities are condensed into the polymer material, and the undistilled high-pressure distillate residue is sent to the desalination unit (1), and the distillation gas is sent to the reduced-pressure distillation condenser (41) connected to the upper portion. And condensation of the distillation gas from the reduced pressure distillation unit (34) so that the condensed oil can be used as recycled fuel oil, and the uncondensed gas is sent to the gas purifier (28) and the reduced pressure distillation condenser (41). Uncondensed gas from the steam condensation reaction tower and the uncondensed gas from the steam condensation reaction column 23 to remove the tar component by using methanol as a fuel gas 28 and the high viscosity from the pyrolysis 14 The coke separated from the undigested oil and the pyrolysis heater 15 is heated and distilled gas is sent to the reflux reaction tower 18 and the pyrolyzed and the remaining solid residue powder is sent to the coke separator 54, and The coke separation contact tower 55 and the water sprayer 56 at the upper portion thereof, and the coke separation cooler 57 and the filter 58 at the lower portion thereof are provided so that the solidifier is circulated by water circulation by the water circulation pump 59. The pyrolysis solid waste powder from (47) is separated into coke powder, collected by the filter (58), and the gas component is composed of a coke separator (54) sent to the solidifying machine (47) by a gas circulation blower (60). .

As shown in FIGS. 1 and 2, the demineralizer 1 has a demineralizer screw 4 installed therein, and a demineralized screw feeder 2 to which a solid hydrocarbon-based organic waste is supplied to the front exterior. And a reduced-pressure residue inlet (3) for injecting the reduced-pressure residue oil from the reduced-pressure distillation machine (34) conveyed by the residue-oil supply pump (45) is formed in the front upper portion. The depressurized residue oil is mixed and transferred by the internal desalination screw (4), and the desalination heating jacket (jacket) is enclosed on the outer circumferential surface thereof to 300 to 330 ° C by the heat medium of the desalting heating jacket (9). It is heated, and a partition (8) is installed on the upper part of the inner circumferential surface of the demineralizer (1), and the vacuum residue oil is contained to the partition (8). In the conventional patent registration No. 10-0551939, EPS (Expanded Poly Styrene) gel is applied. Make separately Although it is used as a sealant, in the present invention, the vacuum residue acts as a sealant.) The chlorine gas generated inside the demineralizer 1 is flowed backward to prevent it from going out of the partition 8, and the chlorine gas outlet 5 formed at the rear upper part thereof. It is to be sent to the neutralization reactor (10) through, the molten raw material conveyed by the desalination screw (4) is discharged through the raw material outlet (6) formed on the back and the pyrolysis by the raw material feed pump (13) It is supposed to send to (14).

In addition, the demineralizer 1 has a hardened product outlet 7 through which metal and other hardened products which are not melted are discharged at the rear lower portion thereof.

The neutralization reactor 10 is filled with caustic soda (NaOH) to neutralize the chlorine gas, and is circulated by the neutralization circulation pump 11 to facilitate the neutralization reaction and neutralized sludge to the neutralization reactor (10) lower Is discharged, and an exhaust blower 12 for discharging the gas collected on the neutralization reactor 10 to the outside is installed outside.

The pyrolyzer 14 is a vertical cylindrical shape of a narrow cone (cone) in the lower portion, the pyrolysis heater 15 is installed in the center of the pyrolyzer 14 in the inner horizontal direction, the pyrolysis heater 15 ) Is heated by the pyrolysis burner 16, the exhaust gas outlet 17 is formed, the reflux reaction tower 18 and the reflux condenser 19 is built in the upper portion of the pyrolyzer 14 in the upper side and A reflux refrigerant cooler 20, a reflux refrigerant cooler fan 21, and a refrigerant circulation pump 22 are connected to each other to cool the heat medium of the reflux condenser 19, and the melt from the demineralizer 1 is melted. The raw material oil is filled inside by the raw material feed pump 13, heated by the pyrolysis heater 15, and pyrolyzed to 380 to 450 ° C., and steam (oil vapor) of the pyrolyzed distillate is at the upper reflux reaction tower 18. To the lower portion of the pyrolyzer (14) Filled with the thermal decomposition is separated from the outer circumferential surface of the opening 15, the coke is to be sent to the solidification exchanger (47) by the solidification of the feed pump (46).

The oil vapor raised to the reflux reaction tower 18 is condensed while passing through the reflux reaction tower 18 and the reflux condenser 19. In the reflux reaction tower 18, oil vapor rising by the condensed oil from the reflux condenser 19 is condensed. First, the condensed and uncondensed oil vapor rises to the reflux condenser 19 and condenses again, and the condensed high boiling point material falls back to the pyrolyzer 14, and the non-condensed oil vapor in the reflux condenser 19 is vapor condensation reaction tower (23). Is transferred to).

The steam condensation reaction tower 23 is provided with a steam condenser 24 at the top thereof, and the waste oil and pyrolysis machine from the methanol and waste oil input machine 26 diluted to 10-30% by weight from the methanol input machine 25. The oil vapor from (14) is collected and brought into contact with each other, and the oil vapor from the pyrolyzer (14) is condensed by contacting the waste oil and methanol at room temperature in the vapor condensation reaction tower (23) and not condensed in the vapor condensation reaction tower (23). The non-condensed steam is condensed from the steam condenser 24 to the top and refluxed to the steam condensation reaction tower 23, the condensate, waste oil and methanol mixture is connected to the bottom of the steam condensation reaction tower (23) methanol reactor (32a) The uncondensed gas, which is sent to the pulverizer 32b and is not condensed in the vapor condenser 24, is transferred to the gas purifier 28 by the gas discharge blower 27.

The methanol reactors 32a and 32b alternately store the condensate, waste oil and methanol mixture from the steam condensation reaction column 23 for 8-10 hours at low speed, and react the odor, dye and tar material under reduced pressure distillation. It is reacted with methanol so as not to be distilled from the agglomerate and agglomerates into a polymer, and is then sent to the vacuum distillation unit 34 by the impurity agglomeration raw material oil supply pump 33.

The methanol reactors 32a and 32b may be any one of the methanol reactor 32a and the methanol reactor 32b.

The vacuum distillation unit 34 uses the "oil distillation unit" of the "oil diffusion vacuum distillation apparatus and method" filed by the present inventors and registered in Korean Patent No. 0739414. The vacuum distillation unit 34 is shown in FIGS. 1 and 3. As described above, a cylindrical vacuum distillation casing 35 is provided, and the vacuum distillation casing 35 has an impurity agglomeration raw material inlet 36 connected to an impurity agglomeration raw material oil supply pump 33 on an upper side thereof, and has an upper top. At the side, a reduced pressure distillation gas outlet 37 is connected to the reduced pressure distillation condenser 41, and a reduced pressure residue outlet 40 is connected to the undistilled residue oil reservoir 44 at the lower side thereof. Heating medium is circulated to surround the heating jacket 38 for heating the reduced pressure distillation casing 35 to a predetermined temperature, and the driving motor is brought into contact with the inner circumferential surface of the reduced pressure distillation casing 35 inside the reduced pressure distillation casing 34. A plurality of plate-shaped inner coating blades 39 rotated are installed to uniformly apply the impregnated agglomerate raw material oil in which the impurities are aggregated in the methanol reactors 32a and 32b to the inner circumferential surface of the vacuum distillation casing 35 to efficiently distill. It is supposed to be done.

The vacuum distillation unit 34 has a low boiling point and viscosity so that the oil vapor from the pyrolysis unit 14, which cannot be used as fuel oil, is mixed with a part of waste oil having a high boiling point and viscosity and cannot be used as fuel oil. It is distilled under reduced pressure to match the boiling point and viscosity of the condensed oil. When distilling at normal pressure, it should be heated to 380 ~ 420 ℃, but the reduced pressure distillation machine 34 is depressurized by the pressure reducing pump 42 and heated to low temperature of 220 ~ 250 ℃ by the heating medium of the heating jacket 38 surrounded by the outside. The distilled and distilled gas is to be sent to the vacuum distillation condenser 41 connected to the upper outside.

The vacuum distillation condenser 41 cools and condenses the distillation gas from the vacuum distillation unit 34 by a refrigerant such as cooling water, and condensed condensed oil is stored in the refinery oil storage tank 43 to be used as refined oil, and the vacuum distillation condenser ( The uncondensed gas not condensed in 41 is sent to the gas purifier 28 together with the gas from the oil vapor condenser 24 conveyed by the gas discharge blower 27 by the decompression pump 42 and the tar contained in the gas. The impurity component is dissolved and removed in methanol circulated by the gas purifier circulating pump 29, compressed in the gas compressor 30, and stored in the gas storage tank 31 to be used as its own fuel gas.

The high-viscosity depressurized residue oil distilled from the reduced-pressure distillation unit 34 is collected in the undistilled residue oil tank 44 and is fed to the reduced-pressure residue inlet 3 of the desalter 1 by the residue oil supply pump 45. Transferred.

The solidifier 47 is formed from a cylindrical solidification chamber 49 which is horizontally installed, and a pyrolysis vessel 14 having a solidification container 48 placed therein in a horizontal direction and transported by a solidification supply pump 46. The raw material oil, which is a high viscosity undecomposed oil, is introduced into the solidification vessel 48 by the solidification screw feeder 50, and the internal solidification vessel 48 is heated by the solidification burner 52 provided under the solidification chamber 49. After distillation, the distilled distillation gas is transferred to the reflux reaction tower (18), and when the distillation is completed, the combustion of the solidification burner (52) is stopped, and the solid residue powder inside the remaining solidification container (48) through pyrolysis is coke separator (54). Transfer to).

On the other hand, the exhaust gas by the solidification burner 52 is discharged to the solidification burner gas outlet 53 formed in the upper part of the solidification chamber 49.

The coke separator 54 has a vertically cylindrical cylindrical water sprayer 56 for showering the solid residue powder from the solidifying machine 47 with water by means of circulating water and collecting it from the bottom thereof. There is a separation contact tower 55, and below the coke separation cooler 57, the lower portion of the coke separator 54 has a filter 58 for filtering and collecting the coke powder showered in the sprayed water, the outside The water circulation pump 59 is connected to circulate water to the top of the coke separator 54 to the water circulation pump 59 so that the coke powder continues to shower. In addition, the remaining non-condensable gas generated from the coke separator 54 is circulated by the gas circulation blower 60 to the solidification vessel 48 of the solidification vessel 47 and coke the solid residue powder inside the solidification vessel 48. It serves as a carrier for conveying to separator 54.

In addition, the coke separator 54 may collect the oil to be recycled to the waste oil injector 26 when the oil condensed on the surface of the water by the coke separator cooler (57).

The method of the present invention is described as follows.

The pulverized and dehydrated solid hydrocarbon organic waste is introduced into the demineralization screw feeder (2) of the demineralizer (1), and the depressurized residue oil supplied from the residue oil supply pump (45) of the vacuum distillation unit (34) is decompressed. When introduced into the private inlet (3), the internal demineralization screw (4) of the demineralizer (1) is transferred to the rear while mixing the input material, 300 ~ 330 from the demineralization heating jacket (9) wrapped around the outside to the heat medium It heats to 0 ° C. to melt solid hydrocarbon organic waste such as waste synthetic resin and waste tire, and separates chlorine gas and sends the chlorine gas to the neutralization reactor 10 through the chlorine gas outlet 5 formed at the rear upper portion of the desalter 1. The inside of the demineralizer (1) is maintained at atmospheric pressure, and the mixed molten raw material oil is introduced into the pyrolyzer (14) by the raw material feed pump (13) through the raw material outlet (6), and the metal does not melt and other costs. The molten cured product is discharged out through the cured product outlet 7.

At this time, the demineralizer (1) is provided with a partition (8) in the upper front of the inner circumferential surface, the partition (8) is filled with a decompression residue oil so that the solid waste synthetic resin is demineralized by a debase screw (4). Continuously flowing into the inside of 1) chlorine gas generated from the inside is not flowed back out of the chlorine gas outlet (5) is discharged only to the neutralization reactor (10). The vacuum residue is distilled under reduced pressure at 220-250 ° C. in the vacuum distillation process. The vacuum distillation temperature corresponds to 380-420 ° C. when distilled at atmospheric pressure. Since no distillation of the oil occurs, no gas is generated and the input temperature of the vacuum residue is 250 ° C or less, so there is no problem of mixing chlorine gas and oil. (In the case of Patent Registration No. 10-0551939 or Patent Registration No. 10-0693464) May have a problem in that chlorine gas and oil are mixed to separate chlorine from the oil again.)

When heating only the synthetic resin in the desalting process, it is hard to discharge chlorine due to hardening of the outer skin while the heat dissipating surface is carbonized, but it is much easier to discharge chlorine because it does not harden the outer skin when heated together with the liquid residue. . That is, since the decompression residue oil and the solid waste synthetic resin, which have a boiling point higher than the chlorine decomposition temperature, are heated together, only the chlorine is decomposed and distilled without carbonization and distillation due to the high heat transfer effect. 8) It is sealed so as not to go out, so that the solid hydrocarbon-based organic waste is continuously introduced. (The conventional EPS gel or waste oil is capable of heat transfer or sealing, but when chlorine is separated, chlorine and oil are distilled at the same time. )

When the molten raw material oil from the desalting machine (1) is supplied to the pyrolyzer (14) from the raw material feed pump (13), the injected raw material oil is pyrolysis heater (15) installed horizontally in the vertical pyrolyzer (14). It thermally decomposes to 380 ~ 450 ℃.

The crude oil is decomposed and distilled by thermal energy from the pyrolysis heater 15 and is transferred to the reflux condenser 19 located above the pyrolysis heater 15 by the gas discharge blower 27. The internal pressure is atmospheric pressure and the distilled gas is condensed as it goes up to the reflux reactor 18 and the reflux condenser 19 located above the pyrolysis heater 15, and the high boiling point material is returned to the pyrolyzer 14 again. . The heat medium of the reflux condenser 19 is controlled by the reflux refrigerant cooler 20 and the reflux refrigerant cooling fan 21 and circulated by the refrigerant circulation pump 22.

If the decomposition continues in the pyrolyzer 14, since a solid material such as coke increases due to decomposition, the decomposition rate is slowed down, so that a certain amount is solidified with a solidification supply pump 46 at a predetermined time to make the thermal decomposition stable. Send to flag 47.

The solidifier 47 is provided with the solidification container 48 and the solidification chamber 49 around the outside.

The solidification vessel 48 is a high-viscosity undigested oil introduced therein is heat-decomposed to 650 ~ 750 ℃ higher than the decomposition temperature in the pyrolyzer 14, the distilled gas is refluxed through the solidification distillation gas outlet 51 Are transferred to 18. Solid residue powder melted through the pyrolysis is transferred to the coke separator 54 while circulating the solidification vessel 48 and the coke separator 54 by the gas circulation blower (60).

On the other hand, the two solidifiers 47 can be installed alternately as needed.

The coke powder, which is a solid residue material from the solidification vessel 48 introduced into the coke separation contact tower 55 of the coke separator 54, is separated from the water spray pump 56 by the water circulation pump 59 and the coke separation contact. It is collected by the filter 58 by forced circulation to the tower 55, coke separation cooler 57 and the filter (58).

In addition, the coke powder collected in the filter 58 may be alternated with two filters to remove the coke powder as necessary, or may be continuously discharged onto the surface by a screw for feeding.

In the pyrolyzer (14), the boiling point of which the adjusted boiling point is condensed by mixing and contacting the low concentration methanol aqueous solution of 10-30% by weight diluted with waste oil and water at room temperature in the steam condensation reaction tower (23).

At this time, the amount of methanol aqueous solution diluted to 10 to 30% by weight is added to 30 to 50% by weight based on the weight of the oil vapor and the waste oil transferred from the reflux condenser 19 of the pyrolyzer 14.

The uncondensed vapor is condensed in the vapor condenser 24, and alternately stored in the methanol reactors 32a and 32b, and reacted with the steam and methanol by stirring at low speed for 8 to 10 hours. In this process, unsaturated hydrocarbons, sulfur oxides, and nitrogen compounds contained in the oil vapor pyrolyzed in the pyrolyzer 14 become high molecular materials by reaction with methanol so that odors, colors, and tars are not distilled from the vacuum distillation unit 34. Aggregate and separate.

The impurity agglomeration raw material oil which has completed the liquid impurity agglomeration reaction is sent to the pressure distillation distillation unit 34 by the impurity agglomeration raw material oil supply pump 33 and re-distilled under reduced pressure.

The vacuum distillation unit 34 of the present invention distills the thermally unstable impurity agglomeration raw material oil at a low pressure of 220 to 250 ° C., and the reduced pressure distillation gas is sent to the vacuum distillation condenser 41 to condense the refined oil into a refined oil storage tank 43. The non-condensed gas, which is not condensed in the reduced pressure distillation unit 34, is transferred to the gas purifier 28 through the reduced pressure pump 42.

In addition, since the pyrolysis oil vapor obtained by pyrolysis and low boiling point pyrolysis distilled together with the non-pyrolysis viscosity and high boiling point waste oil can be produced as fuel oil having the same viscosity and boiling point as kerosene or diesel.

The uncondensed gas discharged from the vacuum distillation condenser 41 and the vapor condenser 24 is used as its own fuel, but the uncondensed gas has no problem as a fuel, but the uncondensed gas has a large number of unsaturated hydrocarbons, and the unsaturated hydrocarbon is converted into a polymer. The coal condensed to produce tar, which is attached to the gas safety device and the combustion device, may cause breakdown and accident of the device. Therefore, the uncondensed gas transferred by the pressure reducing pump 42 and the gas discharge blower 27 of the present invention In the gas purifier 28 filled with 90 to 99% by weight of high purity methanol, the gas containing impurities such as tar is purified, compressed into the gas compressor 30, and stored in the gas storage tank 31 to be used as its own fuel.

1 is a process flow diagram according to the present invention.

2 is an explanatory diagram of a demineralizer according to the present invention.

3 is an explanatory view of a reduced pressure distillation machine according to the present invention.

<Description of Symbols for Major Parts of Drawings>

1. Demineralizer 2. Demineralizer Screw Feeder

3. Decompression residue inlet 4. Demineralization screw

5. Chlorine gas outlet 6. Raw material outlet

7. Cured product outlet 8. Partition

9. Demineralized heating jacket 10. Neutralization reactor

11. Neutralization circulation pump 12. Exhaust blower

13. Raw material feed pump 14. Pyrolysis machine

15. Pyrolysis heater 16. Pyrolysis burner

17. Exhaust gas outlet 18. Reflux tower

19. Reflux condenser 20. Reflux refrigerant cooler

21. Refrigerant refrigerant cooling fan 22. Refrigerant circulation pump

23. Steam Condensation Reaction Tower 24. Steam Condenser

25. Methanol input machine 26. Waste oil input machine

27. Gas discharge blower 28. Gas purifier

29. Gas purifier circulation pump 30. Gas compressor

31. Gas reservoirs 32a, 32b. Methanol reactor

33. Impurity coagulation raw material oil supply pump 34. Vacuum distillation

35. Vacuum distillation casing 36. Impurity coagulation raw material inlet

37. Vacuum distillation gas outlet 38. Heating jacket

39. Internal coating blade 40. Decompression residue outlet

41. Vacuum distillation condenser 42. Pressure reducing pump

43. Refined oil storage tank 44. Undistilled residue oil tank

45. Residual oil supply pump 46. Solidification supply pump

47. Solidifying container 48. Solidifying container

49. Solidification Chamber 50. Solidifying Screw Feeder

51. Solidified distillation gas outlet 52. Solidified burner

53. Solidified burner gas outlet 54. Coke separator

55. Coke Separation Contact Tower 56. Water Sprayer

57. Coke Separator Cooler 58. Filter

59. Water circulation pump 60. Gas circulation blower

Claims (9)

In the apparatus for regenerating hydrocarbon-based organic waste such as waste lubricating oil, waste synthetic resin, and waste tire into refining oil by a pyrolysis process, the solid hydrocarbon-based organic waste and the high-viscosity reduced-pressure residue oil from the vacuum distillation unit 34 are heated to chlorine gas and A demineralizer (1) for separating the molten raw material oil and a non-melt cured product, a neutralization reactor (10) for neutralizing chlorine gas from the demineralizer (1), and a molten raw material oil from the demineralizer (1) Pyrolyzer 14 for separating pyrolyzed and distilled cracked steam and high boiling point undecomposed high viscosity material, methanol from methanol injector 25 and waste oil from waste oil injector 26 and vapor from pyrolyzer 14 To condense the vapor by mixing and condensing the uncondensed gas part in the upper vapor condenser 24 and sending the methanol mixture containing the refluxed condensate to the methanol reactor 32a and 32b. Methanol reactors 32a and 32b for aggregating impurities by stirring the steam condensation reaction tower 23 and the condensed methanol mixture from the vapor condensation reaction tower 23 and impurities in the methanol reactors 32a and 32b. This coagulated impurity coagulant crude oil was distilled under reduced pressure to transfer the undistilled, unvisible, high viscosity, high-viscosity residue to the demineralizer (1), and distilled gas to the reduced-pressure distillation condenser (41) connected to the upper portion. The non-condensed gas condenses the distillation gas from the vacuum distillation unit 34 and the distillation gas from the vacuum distillation unit 34 to the gas purifier 28 so that the condensed oil is used as the regeneration fuel oil. 28, the depressurized distillation condenser 41 and the uncondensed gas from the depressurized distillation condenser 41 and the uncondensed gas from the oil vapor condensation reaction tower 23 are dissolved in methanol to remove tar components and The gas purifier 28 and the high-viscosity undecomposed material from the pyrolyzer 14 are heated and sent back to the reflux reaction tower 18, where the pyrolyzed and residual solid residue powder is coke separator 54. The solidifying unit 47 and the solids debris powder from the solidifying unit 47 are separated into coke powder by the water circulation by the water circulation pump 59 and collected by the filter 58, and the gas component is gas. An apparatus for regenerating hydrocarbon-based organic waste into refined oil by a pyrolysis process, comprising a coke separator (54) sent to a solidifying machine (47) by a circulation blower (60). The demineralizer screw (4) is provided with a demineralization screw (4) therein and a demineralization screw feeder (2) provided with a solid hydrocarbon-based organic waste is provided at the front outside. Depressurized residue inlet (3) into which the depressurized residue oil from the reduced-pressure distillation machine (34) conveyed by the residue oil supply pump (45) is formed, the solid hydrocarbon-based organic waste and the depressurized residue oil are removed from the inside. It is mixed and conveyed by the base screw (4), the outer circumferential surface is surrounded by a desalting heating jacket (9) is heated by the heat medium of the desalting heating jacket (9), the chlorine gas is separated by thermal decomposition to the rear upper portion The molten raw material oil discharged to the formed chlorine gas outlet (5), and transported by the desalination screw (4) is discharged through the raw material outlet (6) formed on the rear side and the pyrolyzer (14) by the raw material oil feed pump (13). Bo) The demineralizer (1) is a device for regenerating hydrocarbon-based organic waste into refined oil by a pyrolysis process, characterized in that a hardened product outlet (7) through which a non-melt hardened product is discharged is formed at a rear lower portion thereof. . [3] The chlorine gas according to claim 1 or 2, wherein the demineralizer 1 is provided with a partition 8 at an upper portion in front of the inner circumferential surface thereof, and a vacuum residue is contained to the partition 8 so that the chlorine gas separated by heat decomposition is separated into a partition ( 8) A device for regenerating hydrocarbon-based organic waste into refined oil by a pyrolysis process, characterized in that it is prevented from flowing out to the outside and sent to the neutralization reactor (10) through a chlorine gas outlet (5) formed at the rear upper portion. According to claim 1, wherein the coke separator 54 is provided with a water sprayer 56, a coke separation contact tower 55, a coke separation cooler 57 and a filter 58 in the top, the water circulation in the outside A pump 59 is connected to pyrolyze the hydrocarbon-based organic waste, characterized in that the solid waste powder from the solidifier 47 is water showered with a water sprayer 56 to collect coke powder in the filter 58. An apparatus for regeneration into refined oil by a process. In the method for regenerating hydrocarbon-based organic waste such as waste lubricant, waste synthetic resin, and waste tire into refined oil by pyrolysis process, solid hydrocarbon-based organic waste and reduced-pressure residue oil are introduced into the desalting machine (1), and the desalting screw ( 4) by heating while mixing and transporting to melt the solid hydrocarbon-based organic waste into the raw material oil, separates the chlorine gas and sends it to the neutralization reactor (10) through the chlorine gas outlet (5), the molten raw material oil feed pump (13) The non-melt cured product which is not melted, is discharged to the outside, and the molten raw material oil from the demineralizer 1 is transferred to the pyrolysis heater 15 from the pyrolyzer 14 by Heated and pyrolyzed to 380 ~ 450 ℃ and condensed as it goes up to the reflux reaction tower 18 and reflux condenser 19, the condensed high-boiling material is refluxed back to the pyrolyzer (14), pyrolyzer (14) Undistilled from Solids such as crude oil and coke are collected in the lower portion and transferred to the solidifying unit 47 by the solidifying supply pump 46, and the high viscosity undigested oil and the solids from the pyrolysis unit 14 are solidified containers of the solidifying unit 47 ( 48) in the solidification chamber (49) by heat decomposition and distillation to 650 ~ 750 ℃ is sent to the reflux reaction tower 18, the solid residue powder is not distilled coke separator (54) by the gas circulation blower (60) The coke powder, which is transferred to the coke separation contact tower 55 of the coke separator and is solid waste from the solidifying machine 47, is lowered by water spraying of the water sprayer 56 at the top of the coke separator 54, and the filter 58. Collected in the reflux condenser 19, the condensed steam not condensed in the reflux condenser 19 is condensed by mixing contact with the waste oil and methanol at room temperature in the steam condensation reaction tower 23, the uncondensed vapor is condensed in the steam condenser 24 With methanol condensation mixture In the methanol reactors 32a and 32b, a liquid impurity agglomeration reaction is carried out by reacting with methanol to agglomerate impurities into polymers. The uncondensed gas which is not condensed in the vapor condenser 24 is used as its own fuel, and the liquid impurity After completion of the coagulation reaction, the impurity coagulation raw material oil is sent to the impurity coagulation material oil supply pump 33 to the vacuum distillation unit 34 to distill the pressure under reduced pressure to distill the thermally unstable impurity coagulation raw material oil at 220 to 250 ° C. The condensate is sent to the vacuum distillation condenser 41, and the non-condensed gas that is not condensed is used as its own fuel, and the refined oil condensed in the vacuum distillation condenser 41 is transferred to the refinery oil storage tank 43 to be used as fuel oil. A method of regenerating hydrocarbon-based organic waste into refined oil by a pyrolysis process. The method of claim 5, wherein the liquid impurity agglomeration reaction is a low-molecular stirring in the methanol reactor (32a) (32b), unsaturated hydrocarbons, sulfur oxides, nitrogen compounds contained in the steam pyrolyzed in the pyrolysis heater (15) is polymerized by methanol A method of regenerating hydrocarbon-based organic waste into refined oil by pyrolysis, characterized in that the substance is agglomerated to separate odors, colors and tars from the distillation under reduced pressure distillation (34). 6. The method of claim 5, wherein the reduced pressure distillation in the reduced pressure distillation unit (34) is carried out under reduced pressure distillation of the pyrolysis vapor component having a low viscosity and boiling point and the waste oil component having a high viscosity and boiling point from the pyrolyzer (14). A method of regenerating hydrocarbon-based organic waste into refined oil by a pyrolysis process, characterized in that it can be used as a fuel oil having a viscosity and boiling point. The method of claim 5, wherein in the steam condensation reaction tower 23, the methanol in contact with the mixed steam and waste oil is diluted 10 to 30% by weight and the input amount is 30 to 50% by weight relative to the weight of the oil and waste oil. A method of regenerating hydrocarbon-based organic waste into refined oil by a pyrolysis process. The non-condensed gas discharged from the vacuum distillation condenser 41 and the steam condenser 24 includes impurities such as tar in the gas purifier 28 filled with high purity methanol of 90 to 99% by weight. A method of regenerating hydrocarbon-based organic waste into refined oil by a pyrolysis process, characterized in that the gas is separated and purified, compressed into a gas compressor (30), and stored in a gas storage tank (31) for use as a fuel of its own.

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