TABLE 1


		Boiling
Carbon Chain Length	Class	Point Range (° C.)

C₅-C₁₀	Gasoline	37-175
C₁₀-C₁₅	Kerosene/Jet Fuel	175-275
C₁₂-C₂₀	Diesel	190-330
C₁₄-C₂₂	Fuel Oil	230-360
C₂₀-C₃₀	Lubricating Oil	>350
C₂₂-C₄₀	Petroleum Jelly	40-60 (m. pt.)
C₂₅-C₅₀	Paraffin Wax	50-65 (m. pt.)
C₅₀+ poly cyclics	Tar/bitumen	>400

It is known in the prior art that aqueous glycerol solutions are insoluble in hydrocarbons. See, e.g., Merck Index Entry 4493 ISBN # 0911910-1-2-3 (1996). Further, U.S. Pat. No. 4,478,612 teaches the use of glycerol as a water-binding astringent in supercritical carbon dioxide.[0009]

The term “dendritic process” is intended herein to refer to a process comprising a simultaneous set of multi-stepped reactions, and the separation and isolation of purified streams of targeted variable products from raw material constituents in a single stage reaction vessel. Examples of such are found in, e.g., Canadian Patent No. 2,249,110; C. R. Strauss,[0010]Aust. J. Chem.52: 83-96 (1999); and J. Haggin,Chemical and Engineering News74 (23): 38 (1999), the complete disclosures of which are hereby incorporated herein by reference.

An ideal dendritic process is described by Paul A Wender,[0011]ACS Chemical&Engineering News,Jan. 8, 2001, page 27, the complete disclosure of which is hereby incorporated herein by reference. The ideal dendritic process has: 1) the capability to use readily available, low cost, mixed raw materials from diverse sources; 2) a short cycle time; 3) a net positive energy balance; 4) no requirement for an organic solvent; 5) robust process variables and: a) is multi-stepped in one reaction vessel; b) leaves no environmental footprint; and c) generates controllable purified separated products in 100% yields, while involving as few personnel and as little equipment as possible.

SUMMARY OF THE INVENTION

The present invention pertains to a process for the catalytic reduction of heavy oils, kerogens, plastics, bio-masses, sludges and organic wastes to light hydrocarbon liquids, carbon dioxide and amines, all in a single reaction vessel. Disclosed herein are multiple examples of an improved dendritic process for the reaction of variegate raw materials, and the separation and isolation of the products formed thereby. The invention takes advantage of the reduction in the number of profligate process steps, the cycle time for the reactions, and the capacity to separate the products using a dendritic process. The invention thus directly addresses the need in the art for an improved dendritic process, which is suitable for application in the processing and recycling or disposal of waste from numerous and variable sources, such as, for example, agricultural, industrial and municipal waste products, and including, but not limited to, various wastes that are toxic or potentially hazardous to human or animal health or the environment.[0012]

In one embodiment, a mixture of synthetic polymers comprising nylon 6, nylon 6,6, nylon 6,10 and nylon 6,12 is subjected to a high temperature in the presence of SCW, thereby producing a mixture of ω-amino caproic acid, 1,6-diamino hexane, hexan-1,6-dioic acid, decan-1,10-dioic acid, and dodecan-1,12-dioic acid. Decarboxlyation of the amino acid and the diacids generate fractionally distillable carbon dioxide, plus pentyl amine, 1,6-diamino hexane, butane, octane, and decane. The amines serve as catalysts for these reactions. Other known catalysts, such as acids, bases and iron oxides embedded in an alumina-silica matrix, optionally are added to the reaction vessel for improved performance. Hence, in one reaction vessel, water is consumed and a mixture of four nylon polymers generates two amines, three hydrocarbons and carbon dioxide.[0013]

In another embodiment, polyethylene is subjected to a high temperature in the presence of water and iron oxide embedded in an alumina-silica matrix or a basic catalyst, such as sulfide. Reductive thermolytic cleavage of carbon-carbon bonds and oxidation of the sulfide to sulfate ion yields C[0014]₂₂to C₄₀waxes or fractionally distillable C₁₀to C₂₂hydrocarbons, respectively. Hence, in one reaction vessel, water is consumed and a mixture of hydrocarbons is formed.

In an yet another embodiment, a mixture of variegate source triglycerides and lipids (preferably with some protein “contaminant”) of animal and/or vegetable origin is subjected to a high temperature in the presence of water, with or without a catalyst. Hydrolysis of the proteins produces a mixture of amino acids; hydrolysis of the triglycerides and lipids produces a mixture of C[0015]₄to C₂₄carboxylic acids, plus glycerol. Decarboxlyation of the amino acids and the carboxylic acids generate fractionally distillable carbon dioxide, amines, and C₃to C₂₃hydrocarbons. The amines serve as catalysts for these reactions. Other known catalysts, such as acids, bases and iron oxides embedded in an alumina-silica matrix, optionally are added to the reaction vessel for improved performance. Also optionally, glycerol is added as a desiccant for the generated hydrocarbons and absorbent for the amines. Thus, the dry hydrocarbon phase optionally is separated before fractional distillation is carried out. Hence, in one reaction vessel, water is consumed and a mixture of triglycerides, lipids, and protein is converted to amines, desiccated hydrocarbons, glycerol and carbon dioxide.

In still another embodiment, animal excrement and vegetable wastes that have a fair proportion of triglycerides, lipids and protein, is subjected to a high temperature in the presence of water, with or without a catalyst. Hydrolysis of the proteins produces a mixture of amino acids; hydrolysis of the triglycerides and lipids produces a mixture of C[0016]₄to C₂₄carboxylic acids, plus glycerol. Decarboxlyation of the amino acids and the carboxylic acids generate fractionally distillable carbon dioxide, amines, and C₃to C₂₃hydrocarbons, with little, if any, methane gas. The amines serve as catalysts for these reactions. Other known catalysts, such as acids, bases and iron oxides embedded in an alumina-silica matrix, optionally are added to the reaction vessel for improved performance. A higher proportion of protein generates a higher ratio of amines to hydrocarbons. Capture and isolation of the putrid smelling amines provides an odor-free process and nitrogen reduced residue. Solid insoluble coke residue (cellulose derived) and mineral salts also are obtained. Hence, in one reaction vessel, water is consumed and human, swine, or bovine excrement and plant matter are converted to carbon dioxide, amines, hydrocarbons, glycerol, and nitrogen-depleted carbonaceous compost. This odor and pathogen-free residue is suitable for use as a low-grade fuel or compost.

In an additional embodiment, Lake Asphalt Tar Sand that has a fair proportion of carboxylic acids is subjected to a high temperature in the presence of super-critical water. Inherent clay catalyst causes decarboxylation of the acids and reductive cleavage of high molecular weight hydrocarbons, generating fractionally distillable C[0017]₁₂, plus other hydrocarbons. Solid insoluble residue (mineral salts), and very heavy organo-sulfur contaminated tars also are obtained. Hence, in one reaction vessel, water is consumed and tar sand is converted to carbon dioxide, hydrocarbons, and residual tar-contaminated clay.

In yet an additional embodiment, heavy oils that have a fair proportion of carboxylic acids are subjected to a high temperature in the presence of SCW, with an iron oxide catalyst or amino acid catalyst, causing decarboxylation of the acids and reductive cleavage of high molecular weight hydrocarbons. Fractionally distillable C[0018]₁₃to C₃₀hydrocarbons is generated. Optionally, the use of ash residue from Lake Asphalt Tar Sand as catalyst in the reductive generation of lighter oils from heavy crude causes the separation of metal contaminants and organo-sulfur compounds from the lighter fractions. Solid insoluble residue (mineral salts) containing very heavy tars and organo-sulfur compounds also are obtained. Hence, in one reaction vessel, water is consumed and heavy oil is converted to carbon dioxide, hydrocarbons, and residual tar contaminated clay (in the case of alumina-silica-iron oxide catalyst) or organo-sulfur tar contaminant residual V—Ni—Fe metals (in the case of amino acid catalyst).

In still an additional embodiment, heavy oils supplemented with waste fats and lipids (as a processing aid in the pipeline transport of crude) are subjected to a high temperature in the presence of SCW. Hydrolysis of the esters, decarboxylation of the acids and reductive cleavage of high molecular weight hydrocarbons thus generates fractionally distillable desiccated lighter hydrocarbons, physically separable water-loaded glycerol, and filterable solids. The solid insoluble residue contains mineral salts and very heavy tars. Hence, in one reaction vessel, water is consumed and lipid-supplemented heavy oil is converted to carbon dioxide, hydrocarbons, and residual organo-sulfur tar contaminant metals.[0019]

In a further embodiment, Albert shale from Stoney Creek, New Brunswick is subjected to a high temperature in the presence of SCW. Reductive thermolytic cleavage of carbon-carbon bonds yields C[0020]₁₂to C₂₆hydrocarbons, as determined by GC/MS.

In yet a further embodiment, extracted lignin or black liquor from the Kraft (sulfide plus carbonate) and Soda-AQ (carbonate) process are subjected to super-critical temperatures. Hydrolysis of the esters, decarboxylation of the acids and reductive cleavage of high molecular weight hydrocarbons generates fractionally distillable hydrocarbons and physically separable precipitated carbonaceous solids. The separated aqueous fraction from the Kraft process contains a mixture of carbonate and sulfate ion, but no substantial sulfide ion. Hence, in one reaction vessel, water is consumed and pulp black liquor is converted to carbon dioxide, hydrocarbons, carbonaceous fuel and green liquor, without resorting to an energy intensive five stage evaporation in order to concentrate the black liquor. This makes the environmentally more friendly Soda-AQ process more financially competitive than the Kraft-Sulfide process, since the Soda-AQ carbonate need not be raised to 1200° C. in order to convert sulfate to sulfide.[0021]

BRIEF DESCRIPTION OF THE DRAWING

FIG. 1 shows a flow chart depicting generally the process of the present invention.[0022]

FIG. 2 shows a view of apparatus suitable for practicing the process of the present invention.[0023]

DETAILED DESCRIPTION OF THE INVENTION

The present invention pertains to a process for the catalytic reduction of heavy oils, kerogens, plastics, bio-masses, sludges and organic wastes to light hydrocarbon liquids, carbon dioxide and amines, all in a single reaction vessel. More particularly, disclosed herein are multiple examples of an improved dendritic process for the reaction of variegate raw materials, and the separation and isolation of the products formed thereby. The invention takes advantage of the reduction in the number of profligate process steps, the cycle time for the reactions, and the capacity to separate the products using a dendritic process. The invention thus directly addresses the need in the art for an improved dendritic process, which is suitable for application in the processing and recycling or disposal of waste from numerous and variable sources, such as, for example, agricultural, industrial and municipal waste products, and including, but not limited to, various wastes that are toxic or potentially hazardous to human or animal health or the environment.[0024]

In accordance with the present invention, a pressurized aqueous system is used for the transformation of higher molecular weight organic compounds into lower molecular weight hydrocarbons of reduced viscosity. The invention provides two general methods for reducing the viscosity of organic raw materials. The first is by converting 200-300° C.-sensitive esters, thioesters, amides, and amino acids to “one carbon shorter” hydrocarbons and/or amines. The second is by thermolytic cracking of the more labile carbon-carbon and carbon-sulfur bonds at 400-500° C. Separating the lower viscosity constituents from each other is accomplished by distillation. The combined inorganic phase and metals-tars-organo-sulfur contaminants separation is achieved by centrifugation.[0025]

The process of the invention optionally is conducted in batch or continuous fashion, with recycling of unconsumed starting materials, if required or desired. The reaction is conducted in a single reactor zone. The materials of construction employed preferably are inert to the starting materials, intermediate reaction materials, and the final products for the reaction process. The fabrication of the equipment should, of course, be able to withstand the reaction temperatures and pressures.[0026]

The invention is suitable as a method for converting organic materials into lower molecular weight hydrocarbons. In a preferred embodiment, this is accomplished by injecting an organic raw material in the form of an aqueous mixture, preferably about 10-50% by weight, through a thin tube (e.g., {fraction (1/16)} inch). In the preferred embodiment, the amount of water present must be sufficient to provide hydrogen as needed to promote the formation of reduced hydrocarbons. A stirrer in the starting materials reservoir agitates the aqueous mixture of organic raw materials, water and catalyst. A pump that can generate a pressure of 200-250 atmospheres feeds the raw material to the reactor. The pressurized raw material is pre-heated to a minimum temperature of about 250° C., preferably by means of a heat exchanger, before entry into the reactor. The reactor mass is maintained at a temperature of about 400-525° C., preferably about 430-500° C., for example, as predetermined by TGA/MS analysis of the reaction raw material and a pressure that is commensurate with the temperature. A heater (preferably electric) heats the autoclave with the capability to maintain the temperature of the twenty-foot length, sixteenth-inch diameter reactor-tube at approximately 500° C. The system is provided with a cooling coil as it exits the autoclave area. Recovered energy is used to pre-heat fresh raw material as it enters the autoclave reaction chamber. Gas and liquid samples are taken after completion of the reaction and cool down.[0027]

Referring now to FIG. 2, apparatus suitable for practicing the process of the present invention is shown. Feeding hopper[0028]1 feeds into holding reservoir2.High pressure pump3 pumps the raw material into the apparatus, with pressure being monitored by pressure gauge4. Primary heat exchanger5 preheats the raw materials. Power control7 and power supply8 allow for adjustment of the amount of power delivered to heating coil6, with temperature meter/controller9 controlling the temperature. Secondary heat exchanger10 provides additional heating, as necessary. Back pressure11 regulates back pressure in the system, and gas/liquid separator allows for removal of gasses or liquids from the system, as necessary. Temperature meter13 and pressure gauge14 monitor temperature and pressure in the system. Gas collection valve15 allows for the collection of gasses, as necessary, and liquid collection valve15 allows for the collection of liquids, as necessary. Heat transfer media pump17 pumps heat transfer media through the system.

The process of our invention teaches that:[0029]

a reaction vessel may contain diverse raw materials in variable proportions, and that the product of one of the reactions may be a catalyst or drying agent for the system as a whole,[0030]

the reactions may be independent or multi-stepped, occurring in concert or cascade fashion,[0031]

the cycle time for the reactions is temperature/pressure dependent and can be controlled in a minimal 3-10 minutes by temperature/pressure regulation in the reaction vessel,[0032]

the temperature at which the reaction vessel is maintained preferably is determined by TGA/MS analysis of the starting materials,[0033]

the reaction products generated during TGA/MS analysis give an indication of the heat levels and time period required for individual reactions,[0034]

the TGA temperature ranges and slopes give a robustness measure of the process variables,[0035]

the array of products formed is isolated by entrapment of the gases, condensation of the liquids in an attached distillation tower, and physical collection of the dry residual solids,[0036]

entrapment of carbon dioxide and amines may be by physical or chemical means, such as physical absorption/adsorption/de-sorption, condensation, crystallization and chemical precipitation,[0037]

entrapment of the amines causes odor abatement,[0038]

through efficient reaction energy recovery and production of a high calorific value product, a net positive energy balance is attained,[0039]

by supplementing very heavy crude with waste animal and/or vegetable oils, a much reduced viscosity and more easily pipelineable mixture is formed,[0040]

lipid-supplemented heavy crude constitutes “diverse raw materials in variable proportions” as described in the first point made above,[0041]

depending on the aqueous content of the raw material, extra water may or may not be required as solvent, and[0042]

no waste products, and hence no environmental footprint, need be left.[0043]

Although several specific examples are described in detail below, one skilled in the art will appreciate from the present disclosure that the following examples are merely guides, which are susceptible to substantial modification, and that the invention can process a wide variety of input materials, including mixtures thereof, for numerous different applications. In the various embodiments of the invention described below, the following proportions of components preferably are used.[0044]

Dendritic Reaction Process[0045]

The term “solid entrapment” is intended to refer to bubbling a gas fraction of the reaction mixture first through a lime solution (precipitates calcium carbonate) and then through an acid solution (generates amine salts).[0046]

Glycerol is a strong water astringent. Water laden glycerol is hydrocarbon insoluble and forms a separate phase. Distillation of the hydrocarbon phase shows no trace of water present.[0047]

EXAMPLE 1Continuous Process Mode

A mixture of variegate source triglycerides and lipids (preferably with some protein “contaminant”) of animal and/or vegetable origin is subjected to a high temperature in the presence of water, with or without a catalyst. Hydrolysis of the proteins produces a mixture of amino acids; hydrolysis of the triglycerides and lipids produces a mixture of C[0048]₄to C₂₄carboxylic acids, plus glycerol. Decarboxlyation of the amino acids and the carboxylic acids generate fractionally distillable carbon dioxide, amines, and C₃to C₂₃hydrocarbons. The amines serve as catalysts for these reactions. Other known catalysts, such as acids, bases and iron oxides embedded in an alumina-silica matrix, optionally are added to the reaction vessel for improved performance. Also optionally, glycerol is added as a desiccant for the generated hydrocarbons and absorbent for the amines. Thus, the dry hydrocarbon phase optionally is separated before fractional distillation is carried out. Hence, in one reaction vessel, water is consumed and a mixture of triglycerides, lipids, and protein is converted to amines, desiccated hydrocarbons, glycerol and carbon dioxide.

In one example, trimmed pork fat, including rind and residual flesh (which is not limiting to the source of animal raw materials that can be used in the process) is pulped. To the pulped fat is added water such that a 50% by weight fat to water mixture is prepared. Pulped pig fat is pumped to the reactor at a rate of 300 ml/hour under 218 atmospheres of pressure. The pressurized pulp is pre-heated to 250° C. by means of a heat exchanger, before entry into the reactor. The reactor is maintained at a temperature of 470° C. Hydrolysis of the triglycerides and proteins with sequential decarboxylation of the freshly generated carboxylic acid functional groups occurs in the twenty-foot length, sixteenth-inch diameter reactor-tube. Generated amine provides a catalytic effect for the hydrolysis reaction and anti corrosive protection of the walls of the reactor. Energy recovered on cooling the exiting autoclave products is used to pre-heat fresh raw material as it enters the autoclave reaction chamber. Gas, liquid and solid products are refined as described above. Skin, ligament and some protein fractions of the pig fat carbonize under the reaction conditions. Physical filtration of the solids from the liquid phases provides solid compost that can be applied to the land as soil builder or burned as a fuel.[0049]

EXAMPLE 2Continuous Process Mode

Animal excrement and vegetable wastes that have a fair proportion of triglycerides, lipids and protein, is subjected to a high temperature in the presence of water, with or without a catalyst. Hydrolysis of the proteins produces a mixture of amino acids; hydrolysis of the triglycerides and lipids produces a mixture of C[0050]₄to C₂₄carboxylic acids, plus glycerol. Decarboxlyation of the amino acids and the carboxylic acids generate fractionally distillable carbon dioxide, amines, and C₃to C₂₃hydrocarbons, with little, if any, methane gas. The amines serve as catalysts for these reactions. Other known catalysts, such as acids, bases and iron oxides embedded in an alumina-silica matrix, optionally are added to the reaction vessel for improved performance. A higher proportion of protein generates a higher ratio of amines to hydrocarbons. Capture and isolation of the putrid smelling amines provides an odor-free process and nitrogen reduced residue. Solid insoluble coke residue (cellulose derived) and mineral salts also are obtained. Hence, in one reaction vessel, water is consumed and human, swine, or bovine excrement and plant matter are converted to carbon dioxide, amines, hydrocarbons, glycerol, and nitrogen-depleted carbonaceous compost. This odor and pathogen-free residue is suitable for use as a low-grade fuel or compost.

In one example, partially de-watered pig excrement including floor washings (which is not limiting to the amount or type of excrement source that can be used in the process) is prepared as a 20% by weight solids mixture. A pump feeds the conditioned excrement to the reactor at a rate of 300 ml/hour under 218 atmospheres of pressure. The pressurized excrement is pre-heated to 250° C. by means of a heat exchanger, before entry into the reactor. The reactor is maintained at a temperature of 430° C. Hydrolysis of the triglycerides and proteins with sequential decarboxylation of the freshly generated carboxylic acid functional groups occurs in the twenty-foot length, sixteenth-inch diameter reactor-tube. All pathogenic material is sterilized and becomes part of the raw material. Generated amine provides a catalytic effect for the hydrolysis reaction and anti-corrosive protection of the walls of the reactor. Energy recovered on cooling the exiting autoclave products is used to pre-heat fresh raw material as it enters the autoclave reaction chamber. Gas, liquid and solid products are refined as described in Example 1. The amine fraction is composed of, for example, ammonia from glycine; methyl amine from alanine, aspartic acid, asparagine and β-alanine; dimethyl amine from sarcosine; trimethyl amine from betaine; iso-butyl amine from valine; iso-pentyl amine from leucine; ethanol amine from serine; 1,2-propanol amine from threonine; 1,3-propanol amine from homo-serine; putrescine from lysine, arginine, and ornithine; histamine from histidine; phenethyl amine from phenyl alanine; tyramine from tyrosine; tryptamine from tryptophan; cysteamine from cysteine; pyrrolidine from proline.[0051]

Amines are odiferous compounds that are usually associated with excrement and decomposing proteins. Putrescine (1,4-diamino butane) and cadaverine (1,5-diamino pentane) aptly derive their nomenclature from the Latin—putrere or putrefaction and cadere or cadaver. Isolation and containment of the amines is one way to achieve abatement of foul odors.[0052]

EXAMPLE 3Continuous Process Mode

Heavy oils supplemented with waste fats or lipids (as a processing aid in the pipeline transport of crude) are subjected to a high temperature in the presence of SCW. Hydrolysis of the esters, decarboxylation of the acids and reductive cleavage of high molecular weight hydrocarbons thus generates fractionally distillable desiccated lighter hydrocarbons, physically separable water-loaded glycerol, and filterable solids. The solid insoluble residue contains mineral salts and very heavy tars. Hence, in one reaction vessel, water is consumed and lipid-supplemented heavy oil is converted to carbon dioxide, hydrocarbons, and residual organo-sulfur tar contaminant metals.[0053]

In one example, 10% by weight waste cooking oil (which is not limiting to the amount or type of triglycerides that can be used in the process) is added to wet crude. The pressurized mixture is pre-heated to 250° C. by means of a heat exchanger, before being pumped into the reactor at a rate of 300 ml/hour under 218 atmospheres of pressure. The reactor is maintained at a temperature of 430° C. Hydrolysis of the triglycerides and tramp proteins with sequential decarboxylation of the freshly generated carboxylic acid functional groups occurs in a twenty-foot length, sixteenth-inch diameter reactor-tube. Generated amine provides a catalytic effect on the hydrolysis reaction. Energy recovered on cooling the exiting autoclave products is used to pre-heat fresh raw material as it enters the autoclave reaction chamber. Gas, liquid and solid products are refined as described above. The distilled hydrocarbon has a boiling range fraction of 60-220° C., which is not present in the starting raw materials.[0054]

Experiments were carried out in a batch reactor. The reactor is constructed from a six-inch diameter stainless steel rod of seven-inch length. Eight half-inch diameter bolts are used to hold a cover head in place. A copper gasket is used to maintain an ultimate pressure of 250 atmospheres in the 40 ml volume well of the reactor. Six propane torches are used to heat the reactor to 430-470° C. Ice is used to cool the reactor, once the reaction temperature is reached.[0055]

EXAMPLE 4Batch Process Mode

Lake Asphalt Tar Sand that has a fair proportion of carboxylic acids is subjected to a high temperature in the presence of super-critical water. Inherent clay catalyst causes decarboxylation of the acids and reductive cleavage of high molecular weight hydrocarbons, generating fractionally distillable C[0056]₁₂, plus other hydrocarbons. Solid insoluble residue (mineral salts), and very heavy organo-sulfur contaminated tars also are obtained. Hence, in one reaction vessel, water is consumed and tar sand is converted to carbon dioxide, hydrocarbons, and residual tar-contaminated clay.

In one example, to 40 grams of Trinidadian Lake Asphalt Tar Sand (70% by weight clay) is added 15 ml of water. The mixture is introduced into the reactor and the temperature of the reactor is raised to 430° C. Upon reaching 430° C., the source of heat is shut down and cooling is started. Upon reaching room temperature, the reactor is opened, and trapped carbon dioxide is allowed to escape. The oily-water residual material is extracted with methylene chloride. Distillation of the extract yields a heavy oil that boils above 200° C. The residual clay contains 3% by weight of tar.[0057]

EXAMPLE 5Batch Process Mode

Heavy oils that have a fair proportion of carboxylic acids are subjected to a high temperature in the presence of SCW, with an iron oxide catalyst or amino acid catalyst, causing decarboxylation of the acids and reductive cleavage of high molecular weight hydrocarbons. Fractionally distillable C[0058]₁₃to C₃₀hydrocarbons is generated. Optionally, the use of ash residue from Lake Asphalt Tar Sand as catalyst in the reductive generation of lighter oils from heavy crude causes the separation of metal contaminants and organo-sulfur compounds from the lighter fractions. Solid insoluble residue (mineral salts) containing very heavy tars and organo-sulfur compounds also are obtained. Hence, in one reaction vessel, water is consumed and heavy oil is converted to carbon dioxide, hydrocarbons, and residual tar contaminated clay (in the case of alumina-silica-iron oxide catalyst) or organo-sulfur tar contaminant residual V—Ni—Fe metals (in the case of amino acid catalyst).

In one example, to 20 grams of 57% aqueous butoxyethanol insoluble Athabasca heavy oil (i.e., maltene extracted asphaltene residuum) is added 15 ml of water and 100 mg aspartic acid. The mixture is introduced into the reactor and the temperature of the reactor is raised to 430° C. Upon reaching 430° C., the source of heat is shut down and cooling is started. Upon reaching room temperature, the reactor is opened, and trapped carbon dioxide and ethyl amine are allowed to escape. The oily-water residual material is partitioned using 100 ml 20% by volume butoxyethanol in water at 80° C. All of the viscosity reduced oil dissolves in the top layer (57% butoxyethanol in water) and a solid residue collects at the bottom of the 10% butoxyethanol in water layer.[0059]

EXAMPLE 6Batch Process Mode

Polyethylene is subjected to a high temperature in the presence of water and iron oxide embedded in an alumina-silica matrix or a basic catalyst, such as sulfide. Reductive thermolytic cleavage of carbon-carbon bonds and oxidation of the sulfide to sulfate ion yields C[0060]₂₂to C₄₀waxes or fractionally distillable C₁₀to C₂₂hydrocarbons, respectively. Hence, in one reaction vessel, water is consumed and a mixture of hydrocarbons is formed.

In one example, to 20 grams of low density polyethylene film is added 0.5 gm sodium sulfide in 15 ml of water. The mixture is introduced into the reactor and the temperature of the reactor is raised to 460° C. Upon reaching 460° C., the source of heat is shut off and cooling is started. Upon reaching room temperature, the reactor is opened. The oily-water residual material is partitioned from the aqueous phase using 100 ml -methylene chloride. Filtering it through a pad of basic aluminum oxide decolorizes the methylene chloride solution. The kerosene smelling light oil is tested for sulfur content. The water phase is analyzed for sulfide and sulfate content. Performing the reaction using Lake Asphalt clay residue as catalyst yields a waxy product. The melting point is 25-30° C.[0061]

In another embodiment, a mixture of synthetic polymers comprising nylon 6, nylon 6,6, nylon 6,10 and nylon 6,12 is subjected to a high temperature in the presence of SCW, thereby producing a mixture of ω-amino caproic acid, 1,6-diamino hexane, hexan-1,6-dioic acid, decan-1,10-dioic acid, and dodecan-1,12-dioic acid. Decarboxlyation of the amino acid and the diacids generate fractionally distillable carbon dioxide, plus pentyl amine, 1,6-diamino hexane, butane, octane, and decane. The amines serve as catalysts for these reactions. Other known catalysts, such as acids, bases and iron oxides embedded in an alumina-silica matrix, optionally are added to the reaction vessel for improved performance. Hence, in one reaction vessel, water is consumed and a mixture of four nylon polymers generates two amines, three hydrocarbons and carbon dioxide.[0062]

EXAMPLE 7Batch Process Mode

Albert shale from Stoney Creek, New Brunswick is subjected to a high temperature in the presence of SCW. Reductive thermolytic cleavage of carbon-carbon bonds yields C[0063]₁₂to C₂₆hydrocarbons, as determined by GC/MS.

In one example, to 25 grams of crushed Albert Shale (20% organic content) is added 10 ml of water. The temperature of the reactor is raised to 460° C. Upon reaching 460° C., the source of heat is shut down and cooling is started. Upon reaching room temperature, the reactor is opened. The oily-water residual material is partitioned from the aqueous phase using 100 ml methylene chloride. Oil is obtained upon evaporation of the solvent. GC/MS analysis indicates that the oil is composed of C[0064]₁₂to C₂₆saturated hydrocarbon.

EXAMPLE 8Batch Process Mode

Extracted lignin or black liquor from the Kraft (sulfide plus carbonate) and Soda-AQ (carbonate) process are subjected to super-critical temperatures. Hydrolysis of the esters, decarboxylation of the acids and reductive cleavage of high molecular weight hydrocarbons generates fractionally distillable hydrocarbons and physically separable precipitated carbonaceous solids. The separated aqueous fraction from the Kraft process contains a mixture of carbonate and sulfate ion, but no substantial sulfide ion. Hence, in one reaction vessel, water is consumed and pulp black liquor is converted to carbon dioxide, hydrocarbons, carbonaceous fuel and green liquor, without resorting to an energy intensive five stage evaporation in order to concentrate the black liquor. This makes the environmentally more friendly Soda-AQ process more financially competitive than the Kraft-Sulfide process, since the Soda-AQ carbonate need not be raised to 1200° C. in order to convert sulfate to sulfide.[0065]

In one example, 35 ml of 18% Kraft black liquor (sulfide-soda) is placed in the reactor well. The temperature of the reactor is raised to 430° C. Upon reaching 430° C., the source of heat is shut down and cooling is started. Upon reaching room temperature ,the reactor is opened. The oily-water residual material is partitioned from a solid phase using 100 ml methylene chloride. Viscous oil is obtained upon evaporation of the dried methylene chloride solvent. GC/MS analysis indicates that the oil is composed mostly of polyaromatic material. Solid powered carbonaceous material is filtered from the reaction mixture. Examination of the water shows that all of the sulfide ions are oxidized to sulfate ions, and that most of the lignin reaction products are precipitated out. Upon standing, the water white aqueous phase begins to take on a brown color, most likely due to oxidation of the water-soluble phenolics. Treatment of 18% Soda-AQ black liquor under the same conditions gives a greater yield of lower boiling point range hydrocarbon and a slightly lesser yield of carbonaceous material.[0066]

Several advantages of the invention are listed below in Table 2.[0067]

TABLE 2


1.	Simplicity of the equipment and the process	Low capital costs,
	requiring fewer personnel	maintenance fees
		and salaries
2.	One step dendritic separation of the organic,	Smaller portable
	water soluble and solid inorganic constituents	reactors withshort
		cycle times

3.	Performing the reaction and separation of	Eliminating the
	constituents in one step	costs of profligate
		process steps
4.	Can use readily available, diverse mixed-	Security against
	source raw materials	availability of raw
		materials sources
		and prices
5.	Reduction in the viscosity of the heavier oil	Increased pipeline
	fractions	flow capabilities at
		lower temperatures
6.	Up-grading the constituents by concentrating	Reduction of the oil
	metals into fewer product streams	volumes which re-
		quire de-contam-
		ination treatment
7.	Reducing odor producing organosulfur and	Eliminates catalyst
	nitrogen compound products	poisoning; Lowers
		treatment costs,
		increases social
		acceptance
8.	Increases liquid volume yield	Decreases coke
		yield
9.	Provides a drying agent when glycerol is	Eliminates emulsion
	generated	formation
10.	Reduces the energy cost to delignify cellulose	Provides an alter-
	pulps; raises the cost competitiveness of the	nate recovery
	Soda-AQ process	method for green
		liquor in paper
		making
11.	Uses wastes as a raw material source and	Eliminates wastes,
	leaves no environmental footprint	including
		pathogenic
		organisms

Accordingly, it is to be understood that the embodiments of the invention herein described are merely illustrative of the application of the principles of the invention. Reference herein to details of the illustrated embodiments is not intended to limit the scope of the claims, which themselves recite those features regarded as essential to the invention.[0068]