TW201502174A - System and method for converting plastic/rubber to hydrocarbon fuel by thermo-catalytic process - Google Patents

Abstract

A system (100) of converting solid waste of plastic/rubber into hydrocarbon fuel, said system (100) comprising: (i) a thermal cracking reactor (110) for cracking the solid waste and a catalyst as feed at a temperature in the range of 200-475DEG C to obtain a catalytic thermal cracking product containing a gaseous hydrocarbon stream and a coke residue; and (ii) a condenser (120) for receiving said gaseous hydrocarbon stream and cooling said gaseous hydrocarbon steam to obtain an at least partly condensate stream containing a liquid hydrocarbon oil of smaller molecules and non-condensable gaseous hydrocarbons, wherein said thermal cracking reactor (110) having an operative top side-wall (103) and an operative bottom side-wall (105) is positioned in horizontal and comprising a feed inlet (104) at one end and a gas outlet (116) at an opposite end on said operative top side-wall (103), a residue outlet (118) at said operative bottom side-wall (105), and an agitator device (106) centrally positioned between said side-walls (103, 105) along the operative longitudinal axis of said reactor (110), and wherein the condenser (120) is in operative communication with said gas outlet (116) of said reactor (110). A method of converting plastic/rubber to hydrocarbon by thermal-catalytic process is also disclosed.

Description

System and method for converting plastic/rubber into hydrocarbon fuel by thermal catalysis

The present invention relates to a system and method for a thermal-catalytic process. In particular, the present invention relates to systems and methods for converting plastic/rubber waste into alternative hydrocarbon fuels (also known as hydrocarbon fuels) using a thermal catalytic process.

Industry and households have a large demand for fuel, but traditional fuels have limited resources, such as fossil fuels, crude oil, wood, natural gas, and nuclear materials (uranium). Traditional fuels cannot meet such high fuel demand at reasonable prices. In addition, there is growing concern about environmental issues that have led to increased use of renewable or waste sources as sustainable alternative fuels. Some of the well-known alternative fuels include biodiesel, bioalcohol (methanol, ethanol, butanol), chemical storage power (batteries and fuel cells), hydrogen, non-fossil methane, non-fossil natural gas, vegetable oil and other biomass resources.

One such source of waste, including potential and valuable resources, is plastic and rubber waste. Millions of tons of waste plastics and rubber are produced every year around the world. Due to concerns about air pollution, most countries ban the incineration of these wastes, and landfills also require a lot of space and can lead to pollution, which is difficult to dispose of. Therefore, the accumulation of these wastes poses a major environmental hazard. A preferred way to handle these waste materials is to recover useful carbonaceous materials therefrom. The recovered carbonaceous material can be used as a fuel source.

Several methods for producing hydrocarbon fuels from waste plastics or rubber have been proposed. These methods generally involve the decomposition of waste by catalytic and thermal cracking with or without a catalyst. The main obstacle to the recovery of carbonaceous materials from plastic/rubber waste is due to the high strength chemical bonds in the plastic/rubber macromolecules.

For example, a method of converting waste plastics into hydrocarbon oil is disclosed in U.S. Patent No. 6,774,271. The method comprises cracking the waste plastic in a thermal cracking reactor at a temperature of 270 to 800 ° C to obtain a portion of the gaseous and partially liquid hydrocarbons and residues. The liquid hydrocarbon is completely cracked into a gaseous hydrocarbon. The chlorine is removed from the gaseous hydrocarbons and then catalyzed by an acid catalyst. The catalytic cracking of the gaseous hydrocarbons is cooled to obtain a hydrocarbon oil.

Another method for obtaining hydrocarbon oils from plastic or rubber waste is disclosed in U.S. Patent No. 5,414,169. The method comprises: thermally cracking the waste material to obtain a thermal cracking product. The thermal cracking product is liquefied in the presence of a catalyst to cause a liquid phase cracking reaction of the liquefied product to produce a cracked product. The thus obtained cracked product was cooled to obtain a hydrocarbon oil.

Another method is the catalytic cracking of waste plastics, which is disclosed in U.S. Patent No. 8,350,104, in which a polyethylene composed of linear chain molecules can be decomposed at low temperatures and produces little residue. The method includes charging waste plastic as a raw material in a reaction vessel, and heating the particulate sulfurized catalytic cracking (FCC) catalyst to 350 to 500 ° C to decompose and gasify the waste particles in contact with the catalyst.

Another method of making a hydrocarbon-containing fluid is disclosed in U.S. Patent Publication No. 2011/0124932, which comprises melting a large amount of solid waste plastic material in an aerobic environment to produce a waste plastic melt and distilling at least a portion of the waste. The plastic melt gives a hydrocarbon distillate and collects the hydrocarbon distillate.

A catalyst for the low temperature pyrolysis of hydrocarbon-containing polymeric materials, primarily for recycled rubber waste, is disclosed in U.S. Patent No. 6,743,746. The catalyst is made of carbonaceous iron particles of fine carbon particles and ultra-dispersed iron particles. The catalyst also contains a metallic carbon component.

A process for gasifying a rubber to separate a gasified rubber into a usable component is disclosed in U.S. Patent No. 6,538,166. This process involves heating the rubber to obtain a vaporized rubber in a negative pressure environment at a temperature of 340 to 510 °C. The venturi separator sprays a vaporized rubber with an oil having a boiling point above 175 ° C, and the oil is incorporated into a heavy oil that vaporizes the rubber hydrocarbon component. The remainder of the gasified rubber is condensed, causing the hydrocarbon portion of the light oil to liquefy and separate from the hydrocarbon gas.

The main disadvantage of the conventional method is that it is difficult to control the conversion process in which solid waste is converted into a gaseous state. In addition, raw materials often require pretreatment, which increases processing time, labor, and energy consumption. In general, the conversion process involves two separate steps of thermal cracking and catalytic cracking. It needs to be done at high temperatures, so this process requires very high energy. The known catalysts have low efficiency, especially at low temperatures, and carbonization mostly occurs at high temperatures, and the oil recovery rate is reduced due to excessive loss in the dry gas. In addition, the product thus obtained has low oxidation stability. Moreover, known methods of rubber gasification are harmful to the environment because they release sulfur compounds, carcinogenic carbon black and other toxic substances. Therefore, a simple, safe and effective method must be used to convert waste plastic/rubber into hydrocarbon fuel, providing stable operation, easy maintenance, and increased catalyst activity.

In order to achieve the object, it is an object of the present invention to provide a system (100) for converting a plastic/rubber solid waste into a hydrocarbon fuel, the system (100) comprising: (i) a thermal cracking reactor (110), The catalyst is pyrolyzed and the catalyst is added at a temperature of 200-475 ° C to obtain a catalytic pyrolysis product comprising a gaseous hydrocarbon stream and a coke residue; and (ii) a condenser (120) for receiving the gaseous hydrocarbon stream and Cooling the gaseous hydrocarbon stream results in an at least partially condensed stream comprising a smaller molecular liquid hydrocarbon oil and a non-condensable gaseous hydrocarbon, wherein the thermal cracking reactor (110) has an operable top side wall (103) And a horizontally disposed operative bottom side wall (105) including a feed opening (104) at one end of the operable top side wall (103) and an opposite end gas outlet (116); at the operable bottom side wall (103) a residue outlet (118); and a stirrer device (106) located at a central position between the operable longitudinal axis of the reactor (110) and the side walls (103, 105), and a condenser (120) And is operatively coupled to the gas outlet (116) of the reactor.

Another object of the present invention is to provide a method of converting a plastic/rubber solid waste into a hydrocarbon fuel, the method comprising the steps of: (i) placing the solid waste together with the catalyst in a horizontally placed thermal cracking reactor (110) Wherein the cleavage reactor (110) is provided with an operable top side wall (103) and an operable bottom side wall (105), a residue outlet (118) on the operable bottom side wall (103), A feed port (104) at one end of the operable top side wall (103) and a gas outlet (116) at the opposite end, and an agitator device (106), located in the operative longitudinal axis and side wall of the reactor (110) a central location between 105); (ii) thermally cracking the solid waste in the reactor at a temperature of 200 to 475 ° C to obtain a product of catalytic thermal cracking of a gaseous hydrocarbon stream and coke residue; (iii) Receiving a gaseous hydrocarbon stream in the condenser (120) and discharging the coke residue from step (ii) at the residue outlet (118); (iv) cooling the gaseous hydrocarbon stream in the condenser (120) to provide a more Small points An at least partially condensed stream of liquid hydrocarbon oil and non-condensable gaseous hydrocarbons; and (v) delivering purified non-condensable gaseous hydrocarbons to a combustion chamber (134) for combustion.

Accordingly, it is still another object of the present invention to provide a system and method for converting plastic/rubber solid waste into hydrocarbon fuel with great efficiency.

Another object of the present invention is to provide a system and method for converting plastic/rubber solid waste into a hydrocarbon fuel which is simple, cost effective, energy efficient, and produces minimal residue and by-products.

Moreover, it is another object of the present invention to provide a system and method for converting plastic/rubber solid waste into a hydrocarbon fuel that provides improved catalyst activity.

It is yet another object of the present invention to provide a system for converting a plastic/rubber solid waste into a hydrocarbon fuel, further comprising an oil reservoir (142) operatively coupled to the condenser (120) to receive the condenser ( 120) Receiving a condensed stream.

Still another object of the present invention is to provide a method for converting a plastic/rubber solid waste into a hydrocarbon fuel, wherein the catalyst is selected from the group consisting of aluminum ruthenate, bismuth ruthenate, bismuth ruthenate, calcium ruthenate, and iron ruthenate. , magnesium citrate, manganese citrate, potassium citrate, sodium citrate, zirconium silicate, copper citrate, tin citrate, iron citrate, lead citrate, tungsten citrate, bismuth citrate, lithium niobate, aluminum , antimony, copper, iron, lead, magnesium, manganese, nickel, tin, tungsten, zinc, aluminum oxide, antimony oxide, copper oxide, iron oxide, lead oxide, magnesium oxide, manganese oxide, nickel oxide, tin oxide, tungsten oxide , zinc oxide, aluminum carbonate, calcium carbonate, sodium carbonate, barium carbonate, copper carbonate, iron carbonate, lead carbonate, magnesium carbonate, manganese carbonate, nickel carbonate, tin carbonate, tungsten carbonate, zinc carbonate, tantalum carbide, calcium carbide, natural And synthetic zeolite, alumina, fuller's earth, bauxite, metal borate, metal boride, ZSM-5 catalyst, FCC Y type catalyst, NiMo/γ-alumina, NiW loaded with amorphous yttrium aluminum, cobalt loading Activated carbon (Co-AC), DHC-8 (industrial bismuth aluminum catalyst), HZSM-5 catalyst, activated red mud, calcined kaolin The group Eckalite-1, Silton CPT-30, Silton MT 100, Mizukasieves Y-420, Re Y-type zeolite, an acidic alumina, Na Y-type zeolite and zeolite-type H Y thereof.

Another object of the present invention is to provide a process for converting a plastic/rubber solid waste into a hydrocarbon fuel, wherein the catalyst comprises at least one metal citrate, at least one metal oxide, at least one zeolite type compound, and at least one a mixture of additives.

It is still another object of the present invention to provide a method for converting a plastic/rubber solid waste into a hydrocarbon fuel, wherein the catalyst particle size is from 0.1 mm to 10 mm.

100‧‧‧ system

102‧‧‧Motor

103‧‧‧ top side wall

104‧‧‧ Feed inlet

105‧‧‧ bottom side wall

106‧‧‧Agitator device

108‧‧‧ heating device

110‧‧‧ Thermal Cracking Reactor

112‧‧‧ rod support

114‧‧‧ rod support

116‧‧‧ gas export

118‧‧‧ Remnant exports

120‧‧‧Condenser

122‧‧‧First temperature gauge

123‧‧‧Second temperature meter

124‧‧‧Water outlet

126‧‧ ‧ water inlet

128‧‧‧ bracket

130‧‧‧Pressure gauge

132‧‧‧ Non-condensable gas outlet

134‧‧‧ combustion chamber

136‧‧‧flame

138‧‧‧burner bracket

140‧‧‧ oil outlet

142‧‧‧ oil storage tank

143‧‧‧Washing unit

144‧‧‧Washing unit

145‧‧‧Water washing unit

S1~S6‧‧‧Steps

The various other objects, features and advantages of the present invention will be more fully understood, Parts, and: FIG. 1 is a schematic view showing a thermal cracking apparatus according to the present invention; FIG. 2 is a flow chart showing a simplified explanation of a thermal cracking process according to the present invention; and FIG. 3 is a view showing the present invention according to the present invention. Conversion of the feed to give a schematic of the gaseous hydrocarbon.

The word "comprising", or variations thereof, such as "including" or "comprising", is used to mean the element, the whole or the steps, or a group of elements, whole or steps. It does not exclude any other elements, elements or steps, or elements, elements or steps of a group.

The use of the terms "at least" or "at least one" or "an" or "an" or "an"

Any discussion of documents, acts, materials, devices, articles, or similar items that have been included in this specification is for the purpose of providing the content of the disclosure, and should not be construed as any or all of Partially or in connection with the technical knowledge of the field of disclosure, as it exists anywhere prior to the priority date of this application.

The numerical values of various physical parameters, dimensions, or quantities referred to herein are merely approximations, and it is contemplated that values that are higher/lower than those assigned to such parameters, sizes, or quantities fall within the scope of the present disclosure, unless otherwise stated in the specification. The specific opposite statement.

The present invention contemplates a system and method thereof for efficiently producing small hydrocarbon clean hydrocarbon oils having high calorific value from solid plastic or rubber waste. The system of the present invention is simple to use, cost effective, saves energy, and produces minimal residue and by-products. The system of the present invention can further increase the activity of the catalyst. This method provides better control of the temperature of the liquid fraction, thereby greatly increasing the efficiency and yield of the cracking process.

A preferred embodiment of a system and method for converting solid plastic or rubber waste to hydrocarbon oil in accordance with the present invention is shown in Figure 1 of the accompanying drawings. The system is used for batch processing to convert solid plastic/rubber materials into hydrocarbon fuels, referenced 100 in Figure 1 for reference. System 100 includes a thermal cracking reactor 110 for performing cracking of feed to solid plastic/rubber waste in the presence of a catalyst. Reactor 110 is placed horizontally and includes an operable top sidewall 103 and an operable bottom sidewall 105. A feed inlet 104 is provided at one end of the operable top side wall 103 and a gas outlet 116 is provided at a second opposite end of the operable top side wall 103. Residue outlet 118 is disposed on the operable bottom side wall 105. The agitator device 106 is disposed along an operable longitudinal axis of the reactor 110 and is centrally located between the sidewalls 103 and 105. The screw agitator device 106 is operated by the motor 102. The horizontally placed reactor 110 is supported by rod supports 112 and 114. Reactor 110 includes a heating device 108. A first temperature gauge 122 is provided in reactor 110 to monitor the temperature conditions of reactor 110.

The solid plastic/rubber waste is represented by SW and the catalyst is represented by CT, both of which are fed into the reactor 110 through the feed inlet 104. Alternatively, heavy oil can be added with the feed. After the feed, all of the air is discharged from the reactor 110 to create a vacuum. The ratio of CT catalyst to solid waste is usually 0.01:1 to 0.05:1. The catalyst preferably has a particle size of from 0.1 mm to 10 mm, and the solid waste material is pulverized to a particle size of less than 20 mm.

The catalyst is typically a mixture comprising at least one metal cerate, at least one metal oxide, at least one zeolite-type compound, and at least one additive. The catalyst is selected from the group consisting of aluminum citrate, bismuth ruthenate, bismuth ruthenate, calcium citrate, iron citrate, magnesium citrate, manganese citrate, potassium citrate, sodium citrate, zirconium citrate, copper citrate, tin citrate. , iron citrate, lead citrate, tungsten citrate, bismuth ruthenate, lithium niobate, aluminum, bismuth, copper, iron, lead, magnesium, manganese, nickel, tin, tungsten, zinc, aluminum oxide, cerium oxide, oxidation Copper, iron oxide, lead oxide, magnesium oxide, manganese oxide, nickel oxide, tin oxide, tungsten oxide, zinc oxide, aluminum carbonate, calcium carbonate, sodium carbonate, barium carbonate, copper carbonate, iron carbonate, lead carbonate, magnesium carbonate, Manganese carbonate, nickel carbonate, tin carbonate, tungsten carbonate, zinc carbonate, barium carbide, calcium carbide, natural and synthetic zeolite, alumina, bleaching earth, bauxite, metal borate, metal boride, ZSM-5 catalyst, FCC Y-type catalyst, NiMo/γ-alumina, NiW loaded with amorphous yttrium aluminum, cobalt-loaded activated carbon (Co-AC), DHC-8 (industrial yttrium aluminum catalyst), HZSM-5 catalyst, activated red mud, calcined kaolin , Eckalite-1, Silton CPT-30, Silton MT 100, Mizukasieves Y-420, Re Y zeolite, acid alumina, Na Y zeolite and A group consisting of H Y zeolites.

The feed is gradually pushed down through the agitator unit 106 along the operable longitudinal axis of the reactor 110 to completely vaporize the hydrocarbons in the solid waste. The feed can be cracked at a temperature of 200 to 475 ° C to obtain a catalytic thermal cracking product containing a gaseous hydrocarbon stream and coke residue.

According to a preferred embodiment of the invention, the mechanism of catalytic thermal cracking is as follows: - end chain cleavage: decomposition of the polymer from the end groups, successively obtaining the corresponding monomers; - random chain cleavage: long chain polymer / hydrocarbon chain Random decomposition into lower length hydrocarbon fragments; - chain stripping: elimination of reactive substituents or pendant groups on the polymer chain, resulting in the evolution of the cleavage product, which also carbonizes the polymer.

During the reaction, solid molecules permeate the catalyst and adsorb in the active zone. The catalyst provides a large amount of active surface and better selectivity. The catalyst facilitates the cracking of the plastic at lower temperatures than conventional pyrolysis processes. Therefore, the catalyst residence time is reduced and the reaction rate is increased.

The coke residue is withdrawn from the residue outlet 118 and the gaseous hydrocarbon stream is withdrawn from the gas outlet 116. A second temperature gauge 123 is provided to monitor the gaseous hydrocarbon stream exiting reactor 110 as GH. Condenser 120 is in operative communication with gas outlet 116 of reactor 110 for receiving a gaseous hydrocarbon stream. The condenser receives cold water having a temperature between 5 and 25 ° C through the water inlet 126, and cools the gaseous hydrocarbon stream to obtain a stream containing at least partially condensed liquid hydrocarbon oil containing less molecules and non-condensable gaseous hydrocarbons. . The heated water thus obtained is discharged from the water outlet 124. The condenser 120 is supported by a bracket 128. An oil reservoir 142 is provided in operative communication with the condenser 120 to receive the condensed stream. The condensed stream from condenser 120 is collected in oil sump 142. The oil reservoir 142 is provided with a pressure gauge 130. The liquid hydrocarbon oil can be discharged through the oil outlet 140. Non-condensable gaseous hydrocarbons are transported through the scrubbing unit. The washing unit is selected from a sodium hydroxide (1% to 5% solution) washing unit 143, calcium hydroxide (1% to 5% solution) washing unit 144, and water washing unit 145. The scrubbing unit is disposed in operative communication with the sump 142 for receiving non-condensable gaseous hydrocarbons for purification. The washing unit is provided with a pressure gauge 130. The purified non-condensable gaseous hydrocarbons are then delivered to the combustion chamber 134 through the non-condensable gas outlet 132. Combustion chamber 134 is adapted to combust non-condensable gases as flame 136. The combustion chamber 134 is supported by a burner bracket 138.

The process yield of plastic waste is 70-85% oil, 10-20% coke and 5-10% non-condensable gas. The manufacturing yield of rubber waste is 40-50% oil, 30-50% coke and 5-10% non-condensable gas. Hydrocarbon oils are suitable as raw materials for the production of polymers, petroleum, or as industrial processes. Liquid fuel or as a fuel for internal combustion engines (such as boilers) or as a marine fuel. Coke can be used as fuel for industries such as thermal power plants and metallurgy.

Figure 2 is a flow chart showing a simplified illustration of a thermal cracking process in accordance with the present invention. According to the invention, the method comprises the following steps:

Step S1: (i) feeding the solid waste together with the catalyst into a horizontally placed thermal cracking reactor 110, wherein the cracking reactor 110 is provided with an operable top side wall 103 and an operable bottom side wall 105, operable A residue outlet 118 on the bottom side wall 103, having a feed port 104 and an opposite end gas outlet 116 at one end of the operable top side wall 103, and an agitator assembly 106 located at the operative longitudinal axis and side wall of the reactor 110 The center position between 103 and 105.

Step S2: (ii) The solid waste is cracked in a reactor at a temperature of 200 to 475 ° C to obtain a catalytic pyrolysis product containing a gaseous hydrocarbon stream and a coke residue CR.

Step S3: (iii) receiving a gaseous hydrocarbon stream in condenser 120 and discharging coke residue CR from step (ii) S2 from residue outlet 118.

Step S4: (iv) cooling the gaseous hydrocarbon GH stream in the condenser 120 to obtain an at least partially condensed stream of liquid hydrocarbon oil containing smaller molecules and non-condensable gaseous hydrocarbon GH;

Step S5: (v) collecting the condensed stream in the sump and delivering the non-condensable gaseous hydrocarbon to the scrubbing unit to purify the non-condensable gaseous hydrocarbon GH.

Step 6: (vi) Transfer the purified non-condensable gaseous hydrocarbons to a combustion chamber (134) for combustion.

Figure 3 is a schematic representation showing the conversion of a feed according to the present invention to give a gaseous hydrocarbon.

As shown, the solid waste is represented by SW and the catalyst is represented by CT, both of which are fed to reactor 110. Alternatively, heavy oil representing HO can be added with the feed. The products of this process include hydrocarbon gas GH and coke residue CR.

The analysis of the various fuel samples obtained by the process of the invention described herein is set forth in Tables 1-5.

The results shown in the above examples clearly demonstrate that the present invention is well adapted to achieve this object, and achieve the objectives and advantages mentioned, as well as the inherent benefits therein. The present invention can be modified by those skilled in the art, and such modifications are intended to be included within the spirit and scope of the invention as defined in the appended claims.

100‧‧‧ system

102‧‧‧Motor

103‧‧‧ top side wall

104‧‧‧ Feed inlet

105‧‧‧ bottom side wall

106‧‧‧Agitator device

108‧‧‧ heating device

110‧‧‧ Thermal Cracking Reactor

112‧‧‧ rod support

114‧‧‧ rod support

116‧‧‧ gas export

118‧‧‧ Remnant exports

120‧‧‧Condenser

122‧‧‧First temperature gauge

123‧‧‧Second temperature meter

124‧‧‧Water outlet

126‧‧ ‧ water inlet

128‧‧‧ bracket

130‧‧‧Pressure gauge

132‧‧‧ Non-condensable gas outlet

134‧‧‧ combustion chamber

136‧‧‧flame

138‧‧‧burner bracket

140‧‧‧ oil outlet

142‧‧‧ oil storage tank

143‧‧‧Washing unit

144‧‧‧Washing unit

145‧‧‧Water washing unit

Claims (10)

A system (100) for converting a plastic/rubber solid waste into a hydrocarbon fuel, the system (100) comprising: (i) a thermal cracking reactor (110) for the solid waste and a particle size of 0.1 mm to One 10mm catalyst is cracked, the ratio of the catalyst to the solid waste is 0.01:1 to 0.05:1, and is used as a feed at a temperature of 200 to 475 ° C to obtain a gaseous hydrocarbon stream and a coke residue. a catalytic thermal cracking product; (ii) a condenser (120) for receiving the gaseous hydrocarbon stream and cooling the gaseous hydrocarbon stream to obtain a liquid hydrocarbon oil containing smaller molecules and a non-condensable gaseous state An at least partially condensed stream of hydrocarbons; and (iii) an sump (142) operatively in communication with the condenser (120) to receive the condensed stream from the condenser (120), Wherein the thermal cracking reactor (110) has an operable top sidewall (103) and a horizontally disposed operable bottom sidewall (105), the thermal cracking reactor (110) being included in the operable top sidewall (103) a feed port (104) at one end and a gas outlet (116) at an opposite end; on the operable bottom side wall (103) a residue outlet (118); and a stirrer device (106) for pushing down the feed port along an operable longitudinal axis of the thermal cracking reactor (110) The feed to the reactor (110) is such that gasification of the hydrocarbons in the solid waste can be accomplished. The system of claim 1, wherein the oil reservoir (142) includes a washing unit operatively coupled to the oil reservoir (142) for receiving the non-condensable gaseous hydrocarbon For purification. The system of claim 2, wherein the oil reservoir (142) includes a combustion chamber (134) for receiving the purified non-condensable gaseous hydrocarbon for combustion. The system of claim 2, wherein the washing unit is a sodium hydroxide washing unit (143). The system of claim 2, wherein the washing unit is a calcium hydroxide washing unit (144). The system of claim 2, wherein the washing unit is a water washing unit (145). The system of claim 2, wherein the combustion chamber (134) is in operative communication with the scrubbing unit (145) for receiving the purified non-condensable gaseous hydrocarbon for combustion. A method for converting a plastic/rubber solid waste into a hydrocarbon fuel, the method comprising the steps of: (i) pulverizing the solid waste material having a particle size of less than 20 mm, and feeding the same catalyst to a heat placed horizontally In the cleavage reactor (110), wherein the cleavage reactor (110) is provided with an operable top side wall (103) and an operable bottom side wall (105) on the operable bottom side wall (103) a residue outlet (118) having a feed port (104) at one end of the operable top side wall (103) and a gas outlet (116) at an opposite end of the operable top side wall (103) And a stirrer device (106) located at a central position between an operable longitudinal axis of the reactor (110) and the side walls (103, 105); (ii) causing the solid waste in the reactor to be Cracking at a temperature of 200 to 475 ° C to obtain a catalytic thermal cracking product comprising a gaseous hydrocarbon stream and a coke residue; (iii) receiving the gaseous hydrocarbon stream in a condenser (120), a residue outlet (118) exiting the coke residue of step (ii); (iv) cooling in the condenser (120) The gaseous hydrocarbon stream to obtain an at least partially condensed stream comprising a smaller molecular liquid hydrocarbon oil and a non-condensable gaseous hydrocarbon; (v) collecting the condensed stream in an oil reservoir, and The non-condensable gaseous hydrocarbon is delivered to a scrubbing unit to purify the non-condensable gaseous hydrocarbon; and (vi) the purified non-condensable gaseous hydrocarbon is passed to a combustion chamber (134) for combustion. The method according to claim 8, wherein the catalyst is selected from the group consisting of aluminum ruthenate, bismuth ruthenate, strontium ruthenate, calcium citrate, iron citrate, magnesium ruthenate, manganese ruthenate, potassium citrate, Sodium citrate, zirconium silicate, copper citrate, tin citrate, iron citrate, lead citrate, tungsten citrate, bismuth ruthenate, lithium niobate, aluminum, bismuth, copper, iron, lead, magnesium, manganese, Nickel, tin, tungsten, zinc, aluminum oxide, cerium oxide, copper oxide, iron oxide, lead oxide, magnesium oxide, manganese oxide, nickel oxide, tin oxide, tungsten oxide, zinc oxide, aluminum carbonate, tantalum carbide, calcium carbide, Natural and synthetic zeolites, alumina, bleaching earth, bauxite, metal borate, metal boride, ZSM-5 catalyst, FCC Y-type catalyst, NiMo/ γ -alumina, NiW loaded with amorphous yttrium aluminum, cobalt Activated carbon (Co-AC), DHC-8 (industrial bismuth aluminum catalyst), HZSM-5 catalyst, activated red mud, calcined kaolin, Eckalite-1, Silton CPT-30, Silton MT 100, Mizukasieves Y-420, Re Y A group consisting of zeolite, acid alumina, Na Y zeolite and HY zeolite. According to the method of claim 9, wherein the catalyst particle size is from 0.1 mm to 10 mm, the ratio of the catalyst to the solid waste is from 0.01:1 to 0.05:1, and the catalyst contains at least one metal citrate. a mixture of at least one metal oxide, at least one zeolite-type compound, and at least one additive.