JP2008133321A - Method for producing thermally decomposed oil from rubber-based waste and apparatus therefor - Google Patents

Abstract

<P>PROBLEM TO BE SOLVED: To provide a method and an apparatus effective for reducing the generation of an oil sludge in the case of mixing a thermally decomposed oil produced from a rubber-based waste and having a kinematic viscosity corresponding to that of a heavy oil with a commercially available grade A crude oil or gas oil. <P>SOLUTION: The method for producing a thermally decomposed oil from a rubber-based waste includes a thermal decomposition step 3 to thermally decompose a rubber-based waste to generate a thermally decomposed gas and a thermally decomposed oil production step 6 to cool the produced thermally decomposed gas and condense the heavy oil fraction in the thermally decomposed gas. In the above method, one or more kinds of waste plastics selected from polypropylene and polyethylene are thermally decomposed in the thermal decomposition step together with the rubber-based waste, the formed thermally decomposed oil is mixed in a thermally decomposed oil mixing step 14 placed after the thermally decomposed oil production step, the oil sludge formed by the mixing step is separated in an oil sludge separation step 17, and the thermally decomposed oil is recovered after the separation of the oil sludge. <P>COPYRIGHT: (C)2008,JPO&INPIT

Description

  The present invention relates to a method for producing pyrolysis oil and an apparatus for producing pyrolysis oil for effectively using rubber waste as a resource.

  Conventional methods for treating rubber waste, including scrap tires, have been centered on simple incineration and landfill, but the promotion of a recycling-oriented society has become a major social issue. Effective utilization technology of rubber waste is required. As a waste processing method for the purpose of effective utilization of rubber waste, for example, as described in Non-Patent Document 1, rubber waste is heated to a thermal decomposition temperature or higher in a pyrolysis furnace (usually 400 ° C. or higher). ) To produce pyrolysis gas and pyrolysis residue, then cool the pyrolysis gas in a later stage to separate and recover the pyrolysis oil contained in the pyrolysis gas. After being distilled into boiling fractions, it is used as pyrolysis oil, etc., pyrolysis gas after pyrolysis oil separation is used as fuel gas or chemical raw material gas, and pyrolysis residue is used as carbonaceous fuel, metal raw material, etc. A waste pyrolysis method has been proposed.

  As the pyrolysis furnace of the pyrolysis oil conversion method, external combustion type pyrolysis method represented by rotary kiln pyrolysis furnace, partial combustion type pyrolysis represented by fluidized bed pyrolysis furnace, moving bed pyrolysis furnace, etc. General methods such as the method can be applied, and when aiming for high calorie gas recovery, the external thermal pyrolysis method does not dilute the pyrolysis gas partially combusted by introducing combustion air or the pyrolysis gas by introducing fluidized gas Is particularly suitable.

  As a method for fractionating the pyrolysis oil recovered by cooling the pyrolysis gas, in addition to a general method in which the pyrolysis oil is introduced into a separate distillation tower and heated and condensed again, for example, described in Patent Document 1 As described above, a method has been proposed in which a distillation column having a plurality of fractionation stages is provided at the rear stage of the pyrolysis furnace, and fractionation is performed directly from a gaseous pyrolysis oil into a plurality of boiling fractions. Further, as a simpler fractionation method, for example, as described in FIG. 5 of Patent Document 2, a direct cooling type pyrolysis oil generator is provided at the rear stage of the pyrolysis furnace, and the pyrolysis gas is decomposed into the pyrolysis gas. The thermal cracking oil controlled to a specific boiling point range is condensed and recovered by directly exchanging heat with the cooling oil whose temperature is controlled in the oil generator, and the condensed and recovered thermal cracked oil is cooled as a pyrolysis gas cooling oil. The method of using as is proposed.

Journal of the Japan Rubber Association, Vol. 59, No. 10, page 565, Fig. 1 (1986) "Glossary of Petroleum Glossary 2nd Edition", p. 5 (Shoshobo) “PETROTECH” Vol. 27, No. 8, p. 670, FIG. "Coal and heavy oil, its chemistry and application", page 91, Figure 2.26 (Kodansha Scientific) "Coal and heavy oil, its chemistry and application", page 126, line 17 to page 127, line 1 (Kodansha Scientific) “PETROTECH” Vol. 27, No. 8, 670 pages, lines 26-33 “Boiler Fuel and Combustion”, page 28, line 21 to page 29, line 5 (Kyoritsu Publishing Co., Ltd.) "Boiler Research" No.171, page 11, table 11 (1978) JP 53-57180 A JP-A-8-11024 JP-A-5-331470 JP-A-2-238091

  However, as a problem of the existing method for pyrolyzing oily waste of rubber-based waste, the present inventors thermally decomposed the rubber-based waste, and the pyrolysis gas is converted to A heavy oil level using the fractionation method of Patent Document 2. When a pyrolysis oil having a kinematic viscosity and a flash point is produced and mixed with a commercially available heavy oil A specified in JIS-K-2205, oil sludge sludge is mixed in the mixture oil. We found that there are problems that occur. The generation of oil mud sludge causes clogging troubles in the burner nozzle and filter of the combustion equipment, the oil supply piping, etc., and is a troublesome problem in terms of operational stability.

Therefore, the present inventors investigated the properties of pyrolysis oil for the purpose of elucidating the cause of oil sludge generation when mixing pyrolysis oil produced from rubber waste with commercial A heavy oil. Is similar to A heavy oil at a flash point of 60 ° C. or higher and a kinematic viscosity of around 2 × 10 ⁻⁵ m ² / sec (measurement temperature 50 ° C., measurement method JIS-K2283), but the chemical composition of pyrolysis oil is It is an oil mainly composed of aromatic hydrocarbons and containing an asphaltene component, and has been found to be close to C heavy oil rather than A heavy oil. Here, the asphaltene component is a component that is insoluble in n-heptane and soluble in benzene or toluene as described in Non-Patent Documents 2 to 5, and is a heavy aromatic hydrocarbon having a polar group. It is kind. Therefore, as described in Non-Patent Document 6, Non-Patent Document 7, etc., the cause of oil mud sludge generation when mixing pyrolysis oil equivalent to heavy oil produced from rubber waste with commercial A heavy oil is Like the case, it is considered to be due to the asphaltene component. In other words, the asphaltene component in pyrolysis oil is usually highly dispersed by forming a stable colloidal state surrounded by aromatic marten oil, which is a high molecular weight aromatic hydrocarbon coexisting in large amounts. When A heavy oil, which contains a lot of paraffinic oil with high affinity with arabic marten oil and low affinity with asphaltene component, is mixed with pyrolysis oil, the stability of the asphaltene component in the mixed oil decreases and aggregates It is thought that it precipitates as oil sludge sludge.

  As a method for reducing the generation of oil sludge caused by asphaltene components, as described in, for example, Patent Document 3, Patent Document 4, and Non-Patent Document 8, oil mud when C heavy oil is mixed with A heavy oil, light oil, or the like For the purpose of suppressing sludge generation, a method of adding a heavy oil additive having a sludge dissolution function, a sludge condensation suppression function by a surface active action, and the like is known. However, as a problem when applying heavy oil additives to pyrolysis oils of rubber waste, the use of additives leads to an increase in the production cost of pyrolysis oil, so competition for heavy oil substitute oils that use waste as raw materials One of the reasons is that the low price, which is an important factor supporting the power, is lost.

  Therefore, the present invention is a simple and capable of reducing the generation of oil mud sludge when mixing pyrolysis oil for A heavy oil produced from rubber-based waste with commercially available A heavy oil and light oils that are the main base material of A heavy oil. It is an object of the present invention to provide a method and apparatus for pyrolysis oil conversion, that is, a method and apparatus for producing pyrolysis oil from rubber waste.

  As a result of intensive studies on methods for reducing the generation of oil mud sludge when mixing pyrolysis oil for A heavy oil produced from rubber waste with commercially available A heavy oil and light oil, After mixing one or more types of waste plastics of polypropylene and polyethylene, and pyrolyzing with a rubber waste in a pyrolysis furnace, the pyrolysis gas is cooled with a pyrolysis oil recovery device and in the pyrolysis gas When the heavy oil fraction is condensed, a pyrolysis oil having a flash point and kinematic viscosity equivalent to A heavy oil including paraffinic oil derived from waste plastic pyrolysis products can be produced. Because the paraffinic oil component derived from waste plastic and the asphaltene component derived from rubber waste coexist in the gaseous state, the pyrolysis oil obtained by condensation of pyrolysis gas is paraffin. We found that oil with low stability of asphaltenes mixed with oil and asphaltene components at a micro level is generated, and asphaltene components contained in rubber waste pyrolysis oil are separated into oil mud sludge in advance, The present method for recovering pyrolyzed oil after separation of oil sludge as product oil was invented.

  In order to solve the problem, the gist of the present invention is as follows (1) to (5).

  (1) The first invention is a pyrolysis step of pyrolyzing rubber waste to generate pyrolysis gas, and cooling the generated pyrolysis gas to condense a heavy oil fraction in the pyrolysis gas. In the method for producing pyrolysis oil from rubber waste having a pyrolysis oil production step for producing pyrolysis oil, at least one of polypropylene and polyethylene together with rubber waste in the pyrolysis step A pyrolysis treatment of the waste plastic, and a pyrolysis oil mixing step for mixing the pyrolysis oil produced at the latter stage of the pyrolysis oil production step, and an oil mud sludge separation step for separating the oil mud sludge produced by the mixing, It is characterized by recovering pyrolyzed oil after separation of oil sludge sludge.

  (2) The second invention is characterized in that the waste plastic is “other plastic container packaging” defined by the Containers and Packaging Recycling Law.

  (3) The third invention is characterized in that the average residence time of the pyrolysis oil in the pyrolysis oil production step is 1 hr or more.

  (4) The fourth invention is characterized in that the pyrolysis oil produced by the method according to any one of (1) to (3) is further mixed with A heavy oil or light oil. To do.

  (5) The fifth invention is a pyrolysis furnace in which one or more types of waste plastics of polypropylene and polyethylene are mixed with rubber waste and pyrolyzed to generate pyrolysis gas, and the generation A pyrolysis oil generator that cools the pyrolysis gas and condenses a heavy oil fraction in the pyrolysis gas to generate pyrolysis oil, a pyrolysis oil mixing device that mixes the generated pyrolysis oil, and And an oil mud sludge separation device for separating and removing the oil mud sludge generated in the mixing device.

  According to the present invention, it is possible to reduce the generation of oil mud sludge when a pyrolysis oil equivalent to heavy oil produced by pyrolysis treatment of rubber waste is mixed with commercially available A heavy oil or light oils which are main base materials of A heavy oil. Possible pyrolysis oils can be produced.

  FIG. 1 is a block diagram showing an example of an equipment configuration for carrying out the method for pyrolyzing and converting a rubber waste according to the first embodiment of the present invention and the apparatus for pyrolyzing oil.

  The rubber waste 1-a and one or more types of waste plastics 1-b of polypropylene and polyethylene are quantitatively supplied into the pyrolysis furnace 3 using a waste feeder 2 such as a screw feeder, Pyrolysis treatment is performed in the cracking furnace 3 to generate a pyrolysis gas 4 and a pyrolysis residue 5 composed of combustible gas and oil. The method of the pyrolysis furnace 3 is not particularly limited, and a general pyrolysis method such as an external heat rotary kiln type pyrolysis furnace or a fluidized bed type pyrolysis furnace is applicable. Regarding the pyrolysis temperature condition, if the temperature is raised too much, gasification will progress too much and the oil yield will decrease, and there is also concern about aromatization due to cyclization reaction of waste plastic pyrolysis oil mainly composed of paraffin oil. Therefore, the furnace temperature is preferably about 750 ° C. or less.

  The pyrolysis gas 4 generated in the pyrolysis furnace 3 is introduced into a pyrolysis oil generator 6 provided at the rear stage of the pyrolysis furnace 3 and counterflows with the pyrolysis gas cooling medium 10 after passing through the indirect cooling heat exchanger. The pyrolysis oil 7 is produced by condensing the heavy oil fraction contained in the pyrolysis gas by contacting them, and the produced pyrolysis oil 7 is temporarily stored in the pyrolysis oil generator 6. The pyrolysis gas 11 after the pyrolysis oil condensation collects light oil components, gas purification, etc. in the subsequent steps and collects the combustible gas. As a method of bringing the pyrolysis gas 4 and the pyrolysis gas cooling medium 10 after passing through the indirect cooling heat exchanger into contact with each other in a countercurrent manner, steam condensation, gas absorption, such as a packed tower method, a wet wall method, a spray method, a scrubber method, etc. The general method used in is applicable. The pyrolysis oil 7 temporarily stored in the pyrolysis oil generator 6 is subsequently introduced into a pyrolysis oil mixing device 14 equipped with a stirrer 13, and the pyrolysis oil 15 is stirred and mixed in the pyrolysis oil mixing device 14. Then, the asphaltene component in the pyrolysis oil is precipitated as oil mud sludge. The pyrolyzed oil in which the asphaltene component is converted to oil mud sludge is sent to the oil mud sludge separation device 17 by the oil feed pump 16, and the oil mud sludge 18 is separated and removed, and then recovered as product oil 19.

  The function required for the pyrolysis oil mixing step is to mix the pyrolysis oil in order to bring the asphaltene components in the pyrolysis oil into contact and agglomerate with each other. There is no limitation, and a general mixing means of liquid fluid can be applied. In addition to the method using the mixing tank equipped with the stirring device of FIG. 1, for example, as shown in FIG. 2, a pyrolysis oil storage tank 22, a pyrolysis oil circulation line 25, a liquid feed pump 24, and an oil mud sludge separation device 20 are provided. A method of mixing the cracked oil by circulating it between the pyrolyzed oil recovery device 6 and the pyrolyzed oil temporary storage tank 22 is also applicable. On the other hand, a mixing means based on molecular vibration such as an ultrasonic vibrator is not preferable because aggregation of asphaltene components may be inhibited.

  As the processing time in the pyrolysis oil mixing step, it is desirable that the average residence time of pyrolysis oil in the pyrolysis oil mixing device is 1 hr or more, and when the average residence time is shortened to 1 hr or less, asphaltene component particle growth May be insufficient.

As a method for adjusting the average residence time of pyrolysis oil in the pyrolysis oil mixing step, for example, the pyrolysis oil volume in the pyrolysis oil mixing device 14, the pyrolysis oil temporary storage tank 22, or the pyrolysis oil generation device 6 is used. Is maintained at a constant level using a liquid level meter or the like, and the extraction speed of the pyrolysis oil from the pyrolysis oil mixing device 14 or the pyrolysis oil temporary storage tank 22 is measured. Continuous tank reactor, such as a method of adjusting the extraction rate of pyrolysis oil so that the volume of pyrolysis oil in the device or the pyrolysis oil temporary storage tank) / (pyrolysis oil extraction rate) ≦ 1 hour is satisfied It is possible to apply a method considered as a residence time adjusting means.

  The method of the oil / sludge sludge separators 17 and 20 is not particularly limited, and existing sludge and sludge separation methods such as a centrifugal separation method and a filter filtration method can be applied.

The types of waste plastics 1-b suitable for thermal decomposition treatment with rubber waste 1-a include the container packaging recycling method that uses polypropylene and polyethylene as main components in addition to industrial waste plastics such as polypropylene and polyethylene. “Other plastic containers and packaging (hereinafter abbreviated as“ Ripula ”)” is specified. The appropriate value for the mixing ratio of waste plastic 1-b varies depending on the properties of the waste plastic and the properties of the oil mixed with the pyrolysis oil. It is desirable to employ a method in which each pyrolyzed oil is generated, and an appropriate value is obtained by performing a sludge generation amount evaluation test using the oil to be mixed and the pyrolyzed oil. As an example of an appropriate value, a pyrolysis oil having a kinematic viscosity of 2 × 10 ⁻⁶ m ² / sec obtained by mixing a plastic waste with a rubber waste and thermally decomposing it is commercially available heavy oil A (kinematic viscosity 2.4 × 10 ^-6 m ² / sec, density 0.86 g / cm ³ , xylene equivalent 0, aniline point 62 ° C.) It is possible to greatly reduce sludge generation when mixing oil and A heavy oil. Moreover, also when mixing with light oils which are the main base material of A heavy oil, it becomes possible to reduce the sludge generation | occurrence | production at the time of mixing with pyrolysis oil by using this invention similarly to the case of A heavy oil. .

(Example 1)
Example of producing pyrolysis oil equivalent to heavy oil by simultaneously treating rubber waste 1-a at a treatment scale of 80 t / day and volumetric plasticizer 1-b at a treatment scale of 20 t / day using the present invention shown in FIG. Indicates. The pyrolysis furnace 3 uses an externally heated rotary kiln equipped with an LNG-fired hot air generator, and the pyrolysis oil generator 6 brings the pyrolysis gas 4 into contact with the cooling medium in countercurrent to condense the oily components as pyrolysis oil 7. In addition, a direct heat exchange method in which the pyrolysis oil 7 generated and used as the cooling medium 8 for the pyrolysis gas was used, and the oil mud sludge separation device 17 was a centrifuge. Waste is charged into the pyrolysis furnace 3 to generate pyrolysis gas 4 and pyrolysis residue 5, and the pyrolysis gas 4 is introduced into the pyrolysis oil generator 6 to come into contact with the pyrolysis gas cooling media 8 and 10. As a result, about 20 m ³ / day of pyrolysis oil 7 was obtained. The obtained pyrolyzed oil 7 is stirred and mixed in the pyrolyzed oil mixing device 14 with an average residence time of 1 hr to precipitate oil mud sludge, and the precipitated oil mud sludge is separated and removed by the centrifugal separator 17, and the oil mud sludge 18 is separated. Was recovered as product oil 19. The recovered product oil has a flash point of 60 ° C to 90 ° C and a kinematic viscosity (measured temperature of 50 ° C) of 1.0 x 10 ^{-5 to} 2.5 x 10 ^-5 m ² / sec (10 to 25 cSt). It was an oil having a low viscosity. Commercial oil A heavy oil (kinematic viscosity 2.4 × 10 ⁻⁶ m ² / sec, density 0.86 g / cm ³ , xylene equivalent 0, aniline point 62 ° C.) is mixed with product oil, and product oil: heavy oil A mixture ratio Of 9: 1.6: 4.3: 7.1: 9, the sludge precipitation amount under the four conditions was evaluated, and the sludge precipitation amount after 50 hours of the mixed oil was 0.1 at any mixing ratio. It was below mass%.
(Example 2)
Using the present invention shown in FIG. 2, similar to Example 1, the rubber waste 1-a is treated simultaneously at a treatment scale of 80 t / day, and the volume of rippla 1-b is treated at a treatment scale of 20 t / day. The example which manufactured cracked oil is shown. The pyrolysis furnace 3 uses an externally heated rotary kiln equipped with an LNG-fired hot air generator, and the pyrolysis oil generator 6 brings the pyrolysis gas 4 into contact with the cooling medium 10 in a counterflow to condense the oily components as pyrolysis oil. In addition, a direct heat exchange method in which the pyrolysis oil 7 generated and used as the cooling medium 8 of the pyrolysis gas is used, and the oil mud sludge separation device 20 uses a centrifuge. The waste 1 is charged into the pyrolysis furnace 3 to generate pyrolysis gas 4 and pyrolysis residue 5, and the pyrolysis gas 4 is introduced into the pyrolysis oil generator 6 and brought into contact with the pyrolysis gas cooling medium 10. As a result, about 20 m ³ / day of pyrolysis oil 7 was obtained. The obtained pyrolysis oil 7 is circulated between the pyrolysis oil recovery apparatus and the pyrolysis oil temporary storage tank 22 with an average residence time of 1 hr to precipitate oil mud sludge, and the precipitated oil mud sludge 21 is separated by the centrifugal separator 20. The pyrolysis oil 23 after removal and separation of the oil mud sludge was recovered as product oil 26. The recovered product oil has a flash point of 60 ° C to 90 ° C and a kinematic viscosity (measured temperature of 50 ° C) of 1.0 x 10 ^{-5 to} 2.5 x 10 ^-5 m ² / sec (10 to 25 cSt). It was an oil having a low viscosity. Commercial oil A heavy oil (kinematic viscosity 2.4 × 10 ⁻⁶ m ² / sec, density 0.86 g / cm ³ , xylene equivalent 0, aniline point 62 ° C.) is mixed with product oil, and product oil: heavy oil A mixture ratio Of 9: 1, 6: 4, 3: 7, and 1: 9, the sludge precipitation amount after 50 hours of the mixed oil was 0.1 at any mixing ratio. It was below mass%.
(Example 3)
In Example 3, the average residence time of the pyrolysis oil in the pyrolysis oil mixing device was 0.5 hr, and the other conditions were the same as in Example 1. An example is shown in which a pyrolysis oil equivalent to heavy oil is produced at the same processing scale of 20 t / day. The pyrolysis oil after separation of the oil / sludge sludge was recovered as a product oil, and the same as in Example 1, a commercially available heavy oil A (kinematic viscosity 2.4 × 10 ⁻⁶ m ² / sec, density 0.86 g / cm ³ , xylene equivalent) 0, aniline point 62 ° C.), and the amount of sludge deposited under four conditions of product oil: A heavy oil mixing ratio of 9: 1, 6: 4, 3: 7, 1: 9 was evaluated. After 50 hours, the amount of sludge deposited was 0.1% by mass or less under a 9: 1 mixture ratio of product oil: A heavy oil, 0.3% by mass under a 6: 4 condition, and 0. A pyrolysis oil having a mixing stability with A heavy oil lower than that of Example 1 and Example 2 was obtained at 5% by mass and a mixing ratio of 1: 9 under 0.1% by mass. The cause of the sludge generation behavior as described above is that the stability of the asphaltene component in the mixed oil is still maintained under the condition where the mixing ratio of the A heavy oil is low (product oil: A heavy oil 9: 1). As the A fuel oil mixture ratio increases (product oil: A fuel oil 6: 4), the stability of the asphaltene component decreases and sludge precipitation occurs. This is probably because when the fuel oil reaches 1: 9), the concentration and content of the asphaltene component are lowered, and sludge formation is less likely to occur.
(Comparative Example 1)
As Comparative Example 1, an example is shown in which the present invention shown in FIG. 1 is used to treat rubber waste alone to produce pyrolysis oil equivalent to heavy oil at a treatment scale of 100 t / day. As in Example 1, the pyrolysis furnace uses an externally heated rotary kiln equipped with an LNG-fired hot air generator, and the pyrolysis oil generator makes the pyrolysis gas contact with the cooling medium countercurrently, as in Example 1. A direct heat exchange system using the oily component as a pyrolysis oil and using the generated pyrolysis oil as a cooling medium for the pyrolysis gas was used. Waste is charged into a pyrolysis furnace to generate pyrolysis gas and pyrolysis residue, and the pyrolysis gas is introduced into the pyrolysis oil generator and brought into contact with the pyrolysis gas cooling medium so that the pyrolysis oil is about 15 m. ³ / day. The obtained pyrolyzed oil was stirred and mixed in the pyrolyzed oil mixing device for an average residence time of 1 hr and then passed through a centrifugal separator, and the pyrolyzed oil after passing through the centrifugal separator was recovered as product oil. The recovered product oil had a flash point of 60 ° C. to 90 ° C. and a kinematic viscosity (measured temperature of 50 ° C.) of 1.0 × 10 ^{−5 to} 2.5 × 10 ⁻⁵ m ² / sec (10 to 25 cSt). Similarly, it was an oil having a low viscosity of A heavy oil class. Commercial oil A heavy oil (kinematic viscosity 2.4 × 10 ⁻⁶ m ² / sec, density 0.86 g / cm ³ , xylene equivalent 0, aniline point 62 ° C.) is mixed with product oil, and product oil: heavy oil A mixture ratio The sludge precipitation amount under four conditions of 9: 1, 6: 4, 3: 7, and 1: 9 was evaluated. The sludge precipitation amount after 50 hours of the mixed oil was 9: 0.1% by mass or less under one condition, 0.5% by mass with a mixing ratio of 6: 4, 1% by mass with a mixing ratio of 3: 7, and 0.1% by mass or less with a mixing ratio of 1: 9. The pyrolysis oil with low mixing stability with A heavy oil compared with Examples 1-3 was obtained.

  Moreover, the result similar to the case of the above-mentioned A heavy oil was obtained also about the light oil which is the main base material of A heavy oil.

It is a block diagram which shows the equipment example of the apparatus which concerns on 1st invention of this invention. It is a block diagram which shows another example of an installation of the apparatus which concerns on 1st invention of this invention.

Explanation of symbols

1-a Rubber waste 1-b Waste plastic 2 Waste supply device 3 Pyrolysis furnace 4 Pyrolysis gas 5 Pyrolysis residue 6 Pyrolysis oil generator 7 Pyrolysis oil 8 Pyrolysis gas cooling medium 9 Indirect cooling heat Exchanger 10 Pyrolysis gas cooling medium after passing through indirectly cooled heat exchanger 11 Pyrolysis gas after pyrolysis oil condensation 12 Pyrolysis oil transfer line 13 Stirrer 14 Pyrolysis oil mixing device 15 Pyrolysis oil 16 Liquid feed pump 17 Oil mud sludge separator 18 Oil mud sludge 19 Product oil 20 Oil mud sludge separator 21 Oil mud sludge 22 Pyrolysis oil temporary storage tank 23 Pyrolysis oil 24 Liquid feed pump 25 Pyrolysis oil circulation line 26 Product oil

Claims (5)

  Pyrolysis process that pyrolyzes rubber waste to generate pyrolysis gas, and pyrolysis that cools the generated pyrolysis gas and condenses the heavy oil fraction in the pyrolysis gas to produce pyrolysis oil In the method for producing pyrolyzed oil from rubber waste having an oil production step, one or more kinds of waste plastics such as polypropylene and polyethylene are pyrolyzed together with rubber waste in the pyrolysis step, A pyrolysis oil mixing step for mixing the pyrolysis oil generated after the pyrolysis oil generation step and an oil mud sludge separation step for separating the oil mud sludge generated by the mixing are provided, and the pyrolysis oil after the oil mud sludge separation is provided. A method for producing pyrolytic oil from rubber waste, characterized in that it is collected.   2. The method for producing pyrolytic oil from rubber waste according to claim 1, wherein the waste plastic is "other plastic container and packaging" defined by the Container and Packaging Recycling Law.   The method for producing pyrolytic oil from rubber waste according to claim 1 or 2, wherein an average residence time of the pyrolytic oil in the pyrolytic oil production step is 1 hr or more.   The pyrolysis oil produced by the method according to any one of claims 1 to 3 is further mixed with A heavy oil or light oil to produce the pyrolysis oil from rubber waste. Method.   A pyrolysis furnace that mixes one or more types of waste plastics of polypropylene and polyethylene with rubber waste and pyrolyzes it to generate pyrolysis gas, and heats the generated pyrolysis gas by cooling it. A pyrolysis oil generator for condensing a heavy oil fraction in cracked gas to generate pyrolysis oil, a pyrolysis oil mixing device for mixing the generated pyrolysis oil, and an oil mud sludge generated in the mixer An apparatus for producing pyrolysis oil from rubber waste, comprising an oil mud sludge separation device for separating and removing.

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