PROCESS FOR PREPARATION OF HYDROCARBON FUEL FROM WASTE RUBBER

Abstract

The present disclosure provides a process for preparing a hydrocarbon fuel from waste rubber. The process involves admixing, in a reaction vessel, at least one fluid medium with the waste rubber to obtain a slurry; wherein the concentration of the waste rubber in the slurry ranges from 45% to 70%. A reactor is charged with the slurry and a predetermined amount of at least one catalyst composition to obtain a mixture, followed by introduction of hydrogen to the reactor to attain a predetermined pressure and heating the mixture at a predetermined temperature, to attain an autogenously generated pressure, and for a predetermined time period to obtain a reaction mass comprising the hydrocarbon fuel. This reaction mass comprising the hydrocarbon fuel is then cooled to obtain a cooled reaction mass. The hydrocarbon fuel is then separated from the cooled reaction mass.

Claims

1. A process for preparing hydrocarbon fuel from rubber; said process comprising the following steps: a. admixing, in a reaction vessel, at least one fluid medium with said waste rubber to obtain a slurry; wherein the concentration of said waste rubber in said slurry ranges from 45% to 70%; b. charging a reactor with said slurry and a predetermined amount of at least one catalyst composition to obtain a mixture; c. introducing hydrogen to said reactor to attain a predetermined pressure followed by heating said mixture for a predetermined time period, at a predetermined temperature to attain an autogenously generated pressure to obtain a reaction mass comprising the hydrocarbon fuel; d. cooling said reaction mass to obtain a cooled reaction mass; and e. separating said hydrocarbon fuel from said cooled reaction mass.

2. The process as claimed in claim 1, wherein said fluid medium is water.

3. The process as claimed in claim 1, wherein said at least one catalyst composition comprises: i. at least one support; ii. at least one promoter component impregnated on said at least one support; iii. optionally at least one stabilizing agent; wherein said at least one stabilizing agent is selected from the group consisting of hexamethyleneimine (HMI), ammonia solution, piperidine, pyrrolidine, morpholine, piperazine hydrate, 2-methyl cyclohexyl amine, and cyclohexylamine; and iv. an active component comprising at least two active metals uniformly dispersed on said at least one support.

4. The process as claimed in claim 3, wherein said at least one support is selected from the group consisting of alumina, silica, zirconia, alumina-silica, zeolite, mesoporous silica, and mesoporous zeolites.

5. The process as claimed in claim 3, wherein said promoter component comprises at least one metal selected from the group consisting of Group III metals, Group IV metals, Group V metals, Group VI metals, Group VII metals, and Group VIII metals.

6. The process as claimed in claim 3, wherein said promoter component is at least one selected from the group consisting of cobalt, nickel, niobium, tantalum, gallium, yttrium, boron, phosphorous, ytterbium, dysprosium, promethium, and samarium.

7. The process as claimed in claim 3, wherein said active metal is at least one selected from the group consisting of Group VIB metals, Group VIIB metals, Group VIII metals, and noble metals.

8. The process as claimed in claim 3, wherein said active metal is at least one selected from the group consisting of Nickel (Ni), Molybdenum (Mo), Cobalt (Co), Platinum (Pt), Palladium (Pd), Ruthenium (Ru), and Rhodium (Rh).

9. The process as claimed in claim 3, wherein the amount of said at least one promoter component is in the range from 0.01 to 2 wt % of the catalyst composition.

10. The process as claimed in claim 3, wherein the amount of said active metal is in the range from 0.1 to 12 wt % of the catalyst composition.

11. The process as claimed in claim 3, wherein said support is in at least one form selected from the group consisting of spheres, extrudates, powder, and pellets.

12. The process as claimed in claim 1, wherein said cooled reaction mass comprises gaseous products and solid products in the range of 4 to 22%.

13. The process as claimed in claim 1, wherein said predetermined pressure is in the range of 1-50 bar and said autogenously generated pressure is in the range of 70 to 300 bar.

14. The process as claimed in claim 1, wherein said predetermined temperature is in the range of 350 to 450° C. and said predetermined time is in the range of 5 to 60 minutes.

15. The process as claimed in claim 1, wherein the amount of said catalyst composition with respect to said waste rubber ranges from 1 to 20 wt %.

Description

DETAILED DESCRIPTION

[0019] Interest in alternative and renewable biological sources of fuels has increased in recent years because of the growing shortage of fossil fuels and the rising environmental pollution, which are the two urgent problems the world is facing today. Increased market prices for energy and fuels are driven by a number of factors including depletion of easily accessible petroleum and natural gas deposits, growth of emerging economies, political instabilities, and mounting environmental concerns. Hence, there exists a need for processes for producing alternative sources of energy (fuels) and simultaneously reducing the environmental pollution.

[0020] In accordance with an embodiment of the present disclosure, there is envisaged a process for producing hydrocarbon fuel from rubber's, which does not require the step of up-gradation of the hydrocarbon fuel. The process of the present disclosure produces a minimal amount of gaseous and solid products along with the liquid hydrocarbon fuel. The process is carried out by hydrothermal liquefaction process (HTL) in the presence of a catalyst composition and hydrogen. Initially rubber is admixed with at least one fluid medium to make a slurry. The mixing of the fluid medium and waste rubber is carried out by stirring the mixture at a speed ranging from 450 rpm to 500 rpm for a time period ranging from 5 minutes to 60 minutes. The fluid medium is typically water. The concentration of waste rubber in the slurry ranges from 45% to 70%.

[0021] In the present disclosure, the hydrothermal liquefaction of the waste rubber is carried out in a batch reactor (reaction vessel). The slurry obtained in the above step is charged in a reactor along with at least one catalyst composition to obtain a mixture. Hydrogen is introduced in the reactor to attain a predetermined pressure and the mixture is heated at a predetermined temperature to generate an autogenous pressure for a predetermined time period to obtain a reaction mass. The reaction mass comprises the hydrocarbon fuel.

[0022] The catalyst composition used in the process of the present disclosure is a heterogeneous catalyst composition comprising at least one support, an active component comprising at least two active metals uniformly dispersed on the support with or without a promoter. The amount of catalyst composition used with respect to the waste rubber in the process of the present disclosure ranges from 1 wt % to 20 wt % depending on the reaction mass.

[0023] In an embodiment, the catalyst composition of the present disclosure comprises an active component comprising at least two metals uniformly dispersed on a support, at least one promoter component on the support, in predetermined quantities.

[0024] The catalyst composition as used in this process of the present disclosure has a dual functionality. The catalyst composition degrades the waste rubber into oil components and reforms the products into liquid hydrocarbon oil, which is free from heteroatoms such as oxygen, nitrogen, sulphur and the like. In an exemplary embodiment, the catalyst composition has the ability to enhance the rate of degradation of the waste natural rubbers, synthetic rubbers, composites and mixed rubbers. The catalyst also has the functionality of hydrodeoxygenation, hydrodenitrogenation, and hydrodesulphurization. The catalyst composition as used in the process of the present disclosure can be easily recovered and reused by any one of the simple processes selected from the group consisting of, but not limited to, filtration, washing, and drying.

[0025] Typically, the support of the catalyst composition is selected from the group consisting of oxides of alumina, silica, zirconia, alumina-silica, mesoporous silica, mesoporous zeolites, zeolite, and the like. A stabilizing agent may be used in the process of making the catalyst composition. The stabilizing agent, which can be used as a solubilizing agent, may be at least one selected from the group consisting of hexamethyleneimine (HMI), ammonia solution, piperidine, pyrrolidine, morpholine, piperazine hydrate, 2-methyl cyclohexyl amine, and cyclohexylamine.

[0026] Typically, the promoters used in the catalyst composition of the present disclosure are selected from the group consisting of Group III metals, Group IV metals, Group V metals, Group VI metals, Group VII metals, and Group VIII metals of the periodic table. The promoter is first impregnated on a carrier by an equilibrium method (promoter (metal) dissolved in water or any organic liquid medium) using a rotation process in the temperature range of 30 to 60° C. The concentration of the promoter on the support/carrier varies from 0.01 to 2 wt %. The active metals in the catalyst are selected from the group consisting of Group VIB metals, Group VIIB metals, Group VIII metals, and noble metals salts and mixtures thereof. The concentration of the active metal used in the process of the present disclosure is in the range of 0.1 to 12 wt % of the catalyst composition.

[0027] The promoter component is at least one selected from the group consisting of cobalt, nickel, niobium, tantalum, gallium, yttrium, boron, phosphorous, ytterbium, dysprosium, promethium, and samarium. The active metal is at least one selected from the group consisting of Nickel (Ni), Molybdenum (Mo), Cobalt (Co), Platinum (Pt), Palladium (Pd), Ruthenium (Ru), and Rhodium (Rh).

[0028] The predetermined temperature is in the range of 350 to 450° C. and the predetermined pressure is in the range of 1 to 50 bar. The predetermined time period is in the range of 5 to 60 minutes. The autogenously generated pressure is in the range of 70 to 300 bar. In an embodiment of the present disclosure, the autogenously generated pressure depends on the reaction temperature and reactant composition such as the solvent and the waste rubber content in the slurry. The autogenously generated pressure is in the range of 70 to 300 bar.

[0029] The reaction mass obtained after the hydrothermal liquefaction process is then cooled to 30° C. Liquid hydrocarbon fuel is a major component of the cooled reaction mass along with a minimal amount of gaseous and solid products. The separation of liquid hydrocarbon fuel is carried out simply by decanting the liquid hydrocarbon fuel from the cooled reaction mass.

[0030] The amount of liquid hydrocarbon fuel obtained, from the process of the present disclosure, from the waste rubber is in the range of 78 to 96% and the amount of gaseous and solid products is in the range of 4 to 22%. There is no formation of the carbon black in the reaction mass.

[0031] The present disclosure is further described in light of the following experiments which are set forth for illustration purpose only and not to be construed for limiting the scope of the disclosure. The following experiments can be scaled up to industrial/commercial scale and the results obtained can be extrapolated to industrial scale.

EXPERIMENTAL DETAILS

Experiment 1

Production of Hydrocarbon Fuel

[0032] 20 gm of waste rubber in the ground/shreded form (0.01-10 mm) was added to a reaction vessel along with 20 ml water and stirred for 15 minutes to obtain a slurry. 2.0 g of the catalyst composition was added to the reaction vessel followed by hydrogen gas till a pressure of 35 bars was attained in the reaction vessel. The reaction vessel was heated to attain a temperature of 415° C. and pressure of the reaction vessel was increased upto 250 bar. A reaction mass comprising the hydrocarbon fuel was obtained along with other gaseous and solid products.

[0033] The reaction mass was then cooled to a temperature of 30° C. and the hydrocarbon fuel was separated by decantation from the reaction mass.

[0034] The yield of liquid hydrocarbon fuel was 96%, that of gaseous product was 4% and solid product was Nil. Table 1 summarises the catalyst assisted performance of various rubbers with and without the use of catalyst.

TABLE-US-00001 TABLE 1 Catalyst assisted HTL performance. Reaction Reaction Oil Entry Type of temp time yield No. waste Catalyst (° C.) (min) (wt %) 1 PBR No catalyst 415 15 79 2 PBR CoMo/Al2O3 415 15 92 3 PBR CoMo/P/Al2O3 415 15 96 4 PBR CoMo/Nb/Al2O3 415 15 96 5 SBR No catalyst 415 15 78 6 SBR CoMo/Nb/Al2O3 415 15 96 7 NR No catalyst 415 30 79 8 NR No catalyst 415 15 79 9 NR CoMo/Nb/Al2O3 415 15 96 10 NR CoMo/Nb/Al2O3 375 30 96 11 NR CoMo/Nb/Al2O3 350 30 90 12 EPDM No catalyst 415 15 76 13 EPDM CoMo/P/Al2O3 415 15 87 14 PBR + CoMo/Nb/Al2O3 415 15 92 SBR + NR 15 PP + PBR + CoMo/Nb/Al2O3 415 15 90 SBR + NR .sup.a Initial H.sub.2 pressure 35 bar; PBR—Poly Butyl Rubber; PP—Polypropylene; NR—Natural Rubber; EPDM—Ethylene Propylene Diene Monomer; SBR—Styrene Butyl Rubber;

TECHNICAL ADVANCEMENTS

[0035] The present disclosure described herein above has several technical advantages including, but not limited to, the realization of: [0036] a simple, energy efficient, time saving, and high yielding process for the production of hydrocarbon fuel from waste rubber, [0037] a process for producing hydrocarbon fuel from waste rubber, which does not need a step of up-gradation; [0038] a process for producing liquid hydrocarbon fuel from waste rubber which does not need the use of any organic solvent; and [0039] reuse of the catalyst in the next cycle of the process for production of hydrocarbon fuel from waste rubber; without affecting the hydrocarbon fuel yield.

[0040] Throughout this specification the word “comprise”, or variations such as “comprises” or “comprising”, will be understood to imply the inclusion of a stated element, integer or step, or group of elements, integers or steps, but not the exclusion of any other element, integer or step, or group of elements, integers or steps.

[0041] The use of the expression “at least” or “at least one” suggests the use of one or more elements or ingredients or quantities, as the use may be in the embodiment of the invention to achieve one or more of the desired objects or results. While certain embodiments of the inventions have been described, these embodiments have been presented by way of example only, and are not intended to limit the scope of the inventions. Variations or modifications to the formulation of this invention, within the scope of the invention, may occur to those skilled in the art upon reviewing the disclosure herein. Such variations or modifications are well within the spirit of this invention.

[0042] The numerical values given for various physical parameters, dimensions and quantities are only approximate values and it is envisaged that the values higher than the numerical value assigned to the physical parameters, dimensions and quantities fall within the scope of the invention unless there is a statement in the specification to the contrary.

[0043] While considerable emphasis has been placed herein on the specific features of the preferred embodiment, it will be appreciated that many additional features can be added and that many changes can be made in the preferred embodiment without departing from the principles of the disclosure. These and other changes in the preferred embodiment of the disclosure will be apparent to those skilled in the art from the disclosure herein, whereby it is to be distinctly understood that the foregoing descriptive matter is to be interpreted merely as illustrative of the disclosure and not as a limitation.