CA2348947A1

CA2348947A1 - A process for the catalytic reduction of heavy oils, kerogens, plastics, bio-masses, sludges and organic waste to light hydrocarbon liquids, carbon dioxide and amines

Info

Publication number: CA2348947A1
Application number: CA002348947A
Authority: CA
Inventors: Venanzio Di Tullio; Paul Herrbach
Original assignee: Individual
Current assignee: Individual
Priority date: 2001-03-19
Filing date: 2001-06-01
Publication date: 2002-09-19
Also published as: WO2002074881A1; US20020173682A1

Abstract

A dendritic process encompassing 1) the con-commitant hydrolysis of esters and amides, 2) the decarboxylation of the free carboxylic acids, and 3) the reductive scission of carbon-carbon carbon-nitrogen and carbon-sulfur bonds in long chain molecules is described. The process has the further encompassing simultaneous capability to confine / concentrate contaminant metals to specific separated fractions and to reduce the overall sulfur contents therein and when triglycerides are present to help desiccate the hydrocarbon fraction.

Description

x17 Specifications / Background of the Invention The ideal dendritic process, as described by Paul A Wender [ACS Chemical &
Engineering News page 27 01 08 2001] 1) has the capability to use readily available, diverse sources, low cost, mixed raw material, 2) has a short cycle time, 3) has a net positive energy balance, 4) requires no solvent, 5) has 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.
By dendritic is meant a simultaneous / all at once set of multi-stepped reactions, separations and isolation of purified streams of targeted variable products from raw material constituents in a single stage reaction vessel. An example is found in Canadian Patent 2249110. Others are described by C.R. Strauss in the Australian J.
Chemistry 52 83-96 (1999) and J. Haggin in Chemical and Engineering News 74 23 38 (1999).
The major constituents of 1) biosynthetic plant/animal tissue and 2) geo/ man made polymers are carbohydrates, lignin, waxes, lipids, proteins, kerogen, mineral oils and plastics.
The three states of matter are solids, liquids and gases. Depending on pressure and temperature the three phases can exist singly or in equilibrium with other phases. Water has, what is known as, three "co-existence curves". They consist of a solid /
gas equilibrium called the sublimation curve, a liquid / gas equilibrium called the vapour pressure curve, and a solid / liquid equilibrium called the melting curve.
There also exists a triple point where all three phases exist in equilibrium. The point on the vapour-liquid curve where the liquid and vapour become identical is called the critical point. The temperature at this point is called the "critical temperature" (T_c water = 374°C) and the pressure is called the "critical pressure"~(P_c water = 218 atmospheres). O.
Maass and E.W.R Steacie. An Introduction to the Principles of Physical Chemistry pages 80-83 John Wiley and Sons Inc. 1939 ; http://www.kobelco.co.jp/p 108/
14/sfe01.htm No gas can be liquefied above its T_c. As water is heated under pressure, it slowly begins to loose its H-bonding characteristics, act more and more like a lower dielectric constant solvent and become less dense. Above its T_c / P_c super critical water (SCW) has a dielectric constant of less than 5 and a density of 0.2 gm / ml.
Hence, SCW
as a supercritical fluid simultaneously acts both as a liquid and a gas with the solvent power of an organic liquid such as benzene.

3, ~ 7 Classic organic reactions such as hydrolysis, bond cleavage and bond formation can occur in the sub-critical zone as described by Wideman L.G. et al USPat 4515713;
Lesutis H.P. et al Chem. Commun. 1999, 2063, and at or above the super critical temperature of water. B. Kuhlmann, E.M.Arnett, M. Siskin J. Org. Chem 1994, 59, 3098-3101 C.R.Strauss Aust. J. Chem. 1000,52, 83-96.
Ester, thioester and amide hydrolysis is usually accompanied by decarboxylation in SCW. The following patents respectively teach the use of acid, basic and neutral catalysts in such reactions: Zeiler, A.C. USPat. 5344975, Theriot, K.J. et al.
USPat.
5329054, and Sealock, L.J. et al. USPat. 5630854.
Carbon - carbon and carbon - sulfur bond rupture followed by hydrogenation of the terminal ionic or free radical end is thermal hydrocracking [Gray M.R. et al.
Energy and Fuels 6(4) 478-485 1992] and / or hydro-desulfurization [Whitehurst D.D. et al. Adv. Catal.
42 345 (1998)). Patel, K.M. et al. USPat 4743357 teach the conversion of heavy hydrocarbons into light hydrocarbons by water and an effective amount of selected catalyst material such as iron (II andlor III) oxides, sulfides or sulfates in the absence of externally added hydrogen; at a temperature greater than 340° and less than 480°C. Pyrolysis without hydrogenation generates coke. Examples of coking are found in the thermal generation of methane gas, distillates and coke when pyrolyzing coal and wood. An excellent reference is found at http://www.newcastle.edu.au.
Amino acids under oxidative reaction conditions are known to denitrify. The products of the Akabori (J. Chem. Soc. Japan 52, 606 (1931), van Slyke (J. Chem. Soc. 99, 792 (1911) and Strecker (Annelen 123, 363 (1862) reactions are aldehydes, ammonia and carbon dioxide. We detected ammonia, carbon dioxide, phenethyl amine and a tar when subjecting phenyl alanine to SCW conditions at 430°C.
The array of products generated when subjecting reactants to SCW conditions, is separated by capture of gases, condensation of liquids in a distillation tower and crystallization / precipitation of solids. Examples of capture of gases are precipitation of carbon dioxide by lime, formation of amine salts by acids and condensation of low boiling hydrocarbons by cryogenic means.
An example of a distillation tower partitioning is the separation of gases and liquids of differing boiling points from each other. The accompanying table presents an example of hydrocarbon boiling ranges for a distillation tower.

'I ~~7 Carbon Chain LengthClass Boiling Point Range°
C

C_5-C _l0 Gasoline 37 - 175 C_l0-C _l5Kerosene/Jet 175-275 Fuel C_l2-C _20Diesel 190-330 C_l4-C _22Fuel Oil 230-360 C_20-C _{30Lubricating} >350 Oil C_22-C _40Petroleum Jelly40-60 (m. pt.) C_25-C _50Paraffin Wax 50-65(m.pt.) C₅₀+poly Tar/bitumen 4 0 cyclics ~ ~_-_-Aqueous glycerol solutions are known to be insoluble in hydrocarbons. [The Merck Index Entry 4493 ISBN # 0911970-1-2-3 (1996)). Diaz Z and Miller JH [USPat 4478612]
teach the use of glycerol as a water-binding astringent in supercritical carbon dioxide.
SUMMARY DESCRIPTION OF THE INVENTION
One Step Dendritic Process This invention relates to the reaction of variegate raw materials and the separation and isolation of the products. The invention takes advantage of the reduction in the number of profligate process steps, the cycle time far the reaction and the capacity to separate the products using a dendritic process.
An example follows. A mixture of nylon 6, nylon 6,6, nylon 6,10 and nylon 6,12 is subjected to a high temperature in the presence of SCW. Hydrolysis of the nylons produces a mixture of c~ramino 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 + pentyl amine + 1,6-diamino hexane + butane + octane + decane. The amines are catalysts for the reactions.
Other known catalysts such as acids, bases and iron oxides embedded in an alumina-silica matrix can be added to the reaction vessel. Hence in one reaction vessel, water is consumed and a mixture of four nylons generates two amines, three hydrocarbons and carbon dioxide.
Another example follows. Polyethylene is subjected to a high temperature in the presence of water and iron oxide embedded in an alumina-silica matrix or a basic s~, 7 catalyst such as sulfide. Reductive thermolytic cleavage of carbon-carbon bonds and oxidation of the sulfide to sulfate ion gave C₂₂ to C₄₀ waxes or fractionally distillable C_l0 to C₂₂ hydrocarbons respectively. Hence in one reaction vessel, water is consumed and a mixture of hydrocarbons is formed.
Still another example follows. 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 C₄ to C₂₄ carboxylic acids plus glycerol. Decarboxlyation of the amino acids and the carboxylic acids generate fractionally distillable carbon dioxide, amines, ammonia and C₃ to C₂₃ hydrocarbons. The amines and ammonia are catalysts for the reactions. Other known catalysts such as acids, bases and iron oxides embedded in an alumina-silica matrix can also be added to the reaction vessel. Concomitant deamination and decarboxylation of the amino acid generate aldehyde, carbon dioxide and free ammonia. A further embodiment of this example is that glycerol is a desiccant for the generated hydrocarbons and absorbent for the ammonia. Thus the dry hydrocarbon phase can be 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, ammonia, desiccated hydrocarbons, glycerol and carbon dioxide.
Yet another example follows. 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 carboxylic acids plus glycerol. Decarboxlyation of the amino acids and the carboxylic acids generate fractionally distillable carbon dioxide, amines, and C₃ to C₂₃ hydrocarbons with little, if any, methane gas (Sealock Jr. L.J. et al USPat 5630854 teach the generation of methane gas only). The amines are catalysts for the reactions.
Concomitant de-amination and decarboxylation of the amino acid generate aldehyde, carbon dioxide and free ammonia. Other known catalysts such as acids, bases and iron oxides embedded in an alumina-silica matrix can also be added to the reaction vessel. A
high proportion of protein naturally generates a higher ratio of amines to hydrocarbons.
Capture and isolation of the putrid smelling amines and ammonia ensures an odour free process and nitrogen reduced residue. Solid insoluble coke residue (poly saccharide 4 / ~'7 derivation) and mineral salts are also obtained. Hence in one reaction vessel, water is consumed and human, swine, and bovine excrement is converted to carbon dioxide, amines, ammonia, hydrocarbons, glycerol, and nitrogen-depleted carbonaceous compost. This odour/pathogen free residue can be used as a low-grade fuel or compost.
A further example follows. 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 and 20%
by volume used vegetable oil. Hydrolysis of ester content and decarboxlyation of the total acids plus reductive cleavage of high molecular weight hydrocarbons followed by separation of the solids by centrifugation generated a distillable ( 160 -220° C) hydrocarbon fraction and a fraction whose boiling point was greater than 220° C.
Solid insoluble residue (mineral salts) with an organo-sulfur contaminated tar is also obtained. Hence in one reaction vessel, water is consumed and tar sand plus vegetable oil is converted to carbon dioxide, hydrocarbons, glycerol and residual tar contaminated clay.
An additional example follows. Heavy oils that have been doctored with waste lipid oil (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, decarboxlyation of the acids and reductive cleavage of high molecular weight hydrocarbons generated fractionally distillable desiccated lighter hydrocarbons, physically separable water-loaded glycerol and filterable solids. The solid insoluble residue contained mineral salts and very heavy tars. Hence in one reaction vessel, water is consumed and lipid doctored heavy oil is converted to carbon dioxide, hydrocarbons, and residual contaminant (V-Ni-Fe) metals.
A still additional example follows. Waste canola vegetable oil was subjected to a 500° C temperature in the presence of SCW. Hydrolysis of the esters, decarboxlyation of the acids and thermal cleavage of generated hydrocarbons gave fractionally distillable desiccated lighter hydrocarbons, physically separable water-loaded glycerol and a filterable residue. Hence in one reaction vessel, water is consumed and vegetable oil is converted to carbon diaxide, glycerol and hydrocarbons, A next to final example follows. Albert shale from Stoney Creek New Brunswick was subjected to a high temperature in the presence of SCW. Reductive thermolytic cleavage of carbon-carbon bonds gave C_l2 to C₂₆ hydrocarbons as determined by GC/MS.
A final example follows. Extracted lignin or black liquor from the Kraft (sulfide +
carbonate) and Soda-AQ (carbonate) process was subjected to super critical ~/~7 temperatures. Hydrolysis of the esters, decarboxlyation of the acids and reductive cleavage of high molecular weight hydrocarbons generated fractionally distillable hydrocarbons and physically separable precipitated carbonaceous solids. The separated aqueous fraction from the Kraft process contained a mixture of carbonate and sulfate ion. Trace sulfide ion was found. 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-AD 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.
DETAILED DESCRIPTION OF THE PROCESS
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 methods for reducing the viscosity of organic raw materials. The first is by converting, 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. Distillation is used to separate the lower viscosity constituents from each other. The combined inorganic phase and metal-tar contaminants separation is achieved by centrifugation.
The process of this invention can be conducted in batch or continuous fashion, with recycle of unconsumed starting materials, if required. The reaction is conducted in a single reactor zone. The materials of construction employed should be inert to the starting materials, intermediate reaction materials and the final products for the reaction process. The fabrication of the equipment should be able to withstand the reaction temperatures and pressures.
The present invention is a method for converting organic materials into lower molecular weight hydrocarbons. This is accomplished by injecting an organic raw material in the form of an aqueous mixture, preferably 10-50% by weight through a sixteenth inch tube.
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

8 ~17 pump that feeds the raw material to the reactor can generate a pressure of 200-atmospheres. The pressurized raw material is preheated to minimum 250°C
by means of a heat exchanger before entry into the reactor. The reactor mass is maintained at a temperature of 400-525°C, preferably 430-500°C, as predetermined by TGA/MS analysis of the reaction raw material and a pressure that is commensurate with the temperature. An electric heater 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 preheat fresh raw material as it enters the autoclave reaction chamber. Gas and liquid samples are taken after completion of the reaction and cool down.
In preferred embodiments of the inventions the following proportions of components can be used.
Experiment 1 - Continuous Process Mode.
Trimmed pork fat including rind and residual ._=w, which is not limiting to the 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 preheated 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 and possible oxidation of the free amine occurs in the twenty-foot length, sixteenth-inch diameter reactor-tube. Generated amine and ammonia 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 preheat fresh raw material as it enters the autoclave reaction chamber.
Gas, liquid and solid products are refined as described below. The fractionally distilled (less than 220°C) product of the reaction by Gel Permeation Chromatography was mainly C_l3, C_l5, and C_l7 alkanes, and glycerol. GC/MS confirmed the presence of C_l3, C_l5, C_l7 alkanes, and carbon dioxide. A second experiment at 500°C caused thermal cracking. GC/MS showed the presence of C₇ to C_l4 alkenes plus C₇ to C_l7 alkanes.

DENDRITIC REACTION PROCESS
Raw material Carbon Dioxide --i gas or solid entrapment + Amines + Ammonia --~ gas, liquid or solid entrapment Water Hydrocarbons ~ fractional distillation Catalyst Glycerol + water --~ phase separation for + water soluble salts 3-10 minutes Q ~ Solid compost ~ filtration 430-470°C
By solid entrapment is meant bubbling the gas fraction of the reaction mixture first through an acid solution (generates ammonia and amine salts) and then through a lime solution (precipitates calcium carbonate). 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.
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.
In another preferred embodiment of the invention the following proportions of components can be used.
Experiment 2- Continuous Process Mode.
Partially de-watered pig excrement including floor washings, which is not limiting to the excrement source that can be used in the process, is prepared as a less than 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 preheated 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 (partial oxidation of the liberated amino acid is possible) occurs in the twenty-foot length, sixteenth-inch diameter reactor-tube. All pathogenic material is t n ~f ~
sterilized and becomes part of the raw material. Generated amine and ammonia 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 preheat fresh raw material as it enters the autoclave reaction chamber. Gas, liquid and solid products are refined as described in experiment 1. The amine fraction is composed of ammonia from glycine; methyl amine from alanine, aspartic acid, asparagine and ~3-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; putrecine from lysine, arginine, and ornithine; histamine from histidine; phenethyl amine from phenyl alanine;
tyramine from tyrosine; tryptamine from tryptophan; cysteamine from cysteine;
pyrollidine from proline.
Amines are odiferous compounds that are usually associated with excrement and decomposing proteins. Putrecine (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 odours. Partial oxidation of the amino acids to aldehyde and ammonia gave an aqueous solution containing 13.9g/1 N-NH₃, a Total Kjeldahl Nitrogen of 15.1g/1, trace N-NO₂, trace N-NO₃, 29.0g/1 Potassium and 1.11 g/1 Total Phosphorous. The low phosphorous content in the aqueous phase is indicative of insoluble phosphates in the residual solids. Attempted deamination of free amine using SCW was unsuccessful.
In still another preferred embodiment of the invention the following proportions of components can be used.
Experiment 3 - Continuous Process Mode.
Twenty percent by weight waste cooking oil (which is not limiting to the amount of triglycerides that can be used in the process) was added to the heavy-oil bottoms asphaltene fraction separated from Kern River crude. The viscosity reduced mixture is preheated 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 was 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 occurred in a twenty-foot length, sixteenth-inch diameter reactor-tube.

/f Generated amine provided a catalytic effect on the hydrolysis reaction. Energy recovered on cooling the exiting autoclave products is used to preheat fresh raw material as it enters the autoclave reaction chamber. Gas, liquid and solid products were refined as described above. The distillable hydrocarbon, which was not present in the starting raw materials, had a boiling point range fraction of 160 - 220.degrees.C
In yet still another preferred embodiment of the invention the following proportions of components can be used.
Experiment 4 - Continuous Process Mode.
Waste canola vegetable oil was subjected to a 500°C temperature in the presence of SCW. Hydrolysis of the esters, decarboxlyation of the acids and thermal cleavage of generated hydrocarbons gave fractionally distillable desiccated lighter hydrocarbons, physically separable water-loaded glycerol and a filterable residue. The fraction, which distilled between 60 and 220°C was shown by GC/MS to contain C₄ -C_l5 alkanes and alkenes. Trace amounts of C_l0 and C_ll alkyl benzene was also detected. The non-distilled fraction above 220°C was shown by FTIR to contain free acid (1710 cm^-1) and no starting material (1736 cm.sup: 1).
Preliminary experiments were carried out in a batch reactor. The reactor was constructed from a six-inch diameter stainless steel rod of seven-inch length. Eight half-inch diameter bolts were used to hold a cover head in place. A copper gasket was used to maintain an ultimate pressure of 250 atmospheres in the 40 ml volume well of the reactor.
Six propane torches were used to heat the reactor to 430-470°C. Ice was used to cool the reactor once the reaction temperature was reached.
Experiment 5 Batch Process Mode To 40 grams of Trinidadian Lake Asphalt Tar Sand (70% by weight clay) was added 15 ml of water. The temperature of the reactor was raised to 430°C. Upon reaching 430, the source of heat was shut down and cooling was started. Upon reaching room temperature the reactor was opened. Trapped carbon dioxide escaped. The oily-water residual material was extracted with methylene chloride. The extract gave a heavy oil that boiled above 200°C. The residual clay contained 3% by weight tar. The aqueous phase contained trace amounts of sulfide (0.08 mg/I) and large amounts of sulfate (288mg/I).

Experiment 6 - Batch Process Mode To 20 grams of 57% aqueous butoxyethanol insoluble Athabasca heavy oil (i.e.
maltene extracted asphaltene residuum; Number average molecular weight by Gel Permeation Chromatography 413; Polydispersity 3.78; Molecular range --400 - 10000 ) was added 15 mls of water and 100 mg aspartic acid. The temperature of the reactor was raised to 430°C. Upon reaching 430, the source of heat was shut down and cooling was started. Upon reaching room temperature the reactor was opened. Trapped carbon dioxide and amine/ammonia escaped. The oily-water residual material was partitioned using 100m1 20% by volume butoxyethanol in water at 80°C. All of the viscosity-reduced oil dissolved in the top layer (57% butoxyethanol in water) and a solid residue collected at the bottom of the 10% butoxyethanol in water layer. The viscosity-reduced oil had a number average molecular weight of 277; Polydispersity 1.62;
Molecular range -100 -1500 and a 17.37, 2.29 and 1.53 fold decrease in iron, nickel and vanadium respectively. The mostly carbon solid residue had much higher concentrations of iron, nickel, and vanadium.
Experiment 7 Batch - Process Mode Crude light (Brut/Isthmus/Maya -35m1) oil that had a naphthenic acid portion was subjected to a high temperature in the presence of SCW with an amino acid catalyst causing decarboxlyation of the acids and reductive cleavage of higher molecular weight hydrocarbons. The starting density of the oil was 0.8923 g/ml at 20°C;
the final density was 0.8633. Solid insoluble residue contained most of the V-Ni-Fe metal.
Experiment 8 Batch - Process Mode To 20 grams of low density polyethylene film was added 0.5 gm sodium sulfide and 15 mls of water. The temperature of the reactor was raised to 460°C. Upon reaching 460, the source of heat was shut off and cooling was started. Upon reaching room temperature the reactor was opened. The oily-water residual material was partitioned from the aqueous phase using 100m1-methylene chloride. Filtering it through a pad of basic aluminum oxide decolorized the methylene chloride solution. The kerosene smelling light oil was tested for sulfur content. Analysis showed the oil contained 0.1%
sulfur. The water phase was also analyzed for sulfide and sulfate content.
Greater than 98% of the sulfide had been converted to sulfate. A repeat reaction using 7.5%
ferric oxide on alumina silicon dioxide as catalyst gave a waxy hydrocarbon product.
The melting point was 25-30°C.

f3/~~T
Experiment 9 - Batch Process Mode To 25 grams of crushed Albert Shale (20% organic content) from New Brunswick Canada was added 10 mls of water. The temperature of the reactor was raised to 460°C.
Upon reaching 460, the source of heat was shut down and cooling was started.
Upon reaching room temperature the reactor was opened. The oily-water residual material was partitioned from the aqueous phase using 100m1 methylene chloride. Oil was obtained upon evaporation of the solvent. GC/MS analysis indicated that the oil was composed of C_l2 to C₂₆ saturated hydrocarbon.
Experiment 10 - Batch Process Mode 35 mls of used lubricating oil (a mixture of motor oil, grease, transmission oil, gasoline, ethylene glycol, water, floor sweepings, etc.) was placed in the reactor well.
The temperature of the reactor was raised to 430°C. Upon reaching 430, the source of heat was shut down and cooling was started. Upon reaching room temperature the reactor was opened. The oily-water residual material was gravity fed through an S&S
qualitative No. 410 filter paper. Water remained in the oil-residue impregnated filter paper. The coloured oil filtrate was gravity fed through a ten centimeter long one cm diameter pad of dry Brockmann I, 150 mesh basic alumina in order to remove all colour.
ICP analysis of the water white oil showed the following metals to be less than 1 ppm:
aluminium, arsenic, barium, boron, cadmium, calcium, chromium, copper, iron, lead, magnesium, molybdenum, nickel, phosphorous, selenium, silicon, silver, sodium, tin, titanium, vanadium, and zinc.
Experiment 11 - Batch Process Mode 35 mls of 18% Kraft black liquor (sulfide-soda) was placed in the reactor well. The temperature of the reactor was raised to 430°C. Upon reaching 430, the source of heat was shut down and cooling was started. Upon reaching room temperature the reactor was opened. The oily-water residual material was partitioned from a solid phase using 100 ml methylene chloride. Viscous oil was obtained upon evaporation of the dried methylene chloride solvent. GC/MS analysis indicated that the oil was composed mostly of polyaromatic material. Solid powered carbonaceous material (Total Organic Carbon =
43.9%) was filtered from the reaction mixture. Examination of the water showed that all of the sulfide ions had been oxidized to sulfate and that most of the lignin reaction products had been precipitated out. Upon standing, the water white aqueous phase began to take on a brown colour - most likely oxidation of water-soluble phenolics.

i~l ~7 Treatment of 18% Soda-AC~ black liquor under the same conditions gave a greater yield of lower boiling point range hydrocarbon and a slightly lesser yield of carbonaceous material.
ADVANTAGE OF OUR PROCESS
1. Simplicity of the equipment and Low capital costs, maintenance the process fees requiring fewer personnel and salaries.

2. One step dendritic separation of Smaller portable reactors the organic, water with short soluble and solid inorganic constituentscycle times.

3. Performing the reaction and separationEliminating the costs of of profligate constituents in one step. process steps.

4. Can use readily available, diverse Security against availability mixed-source of raw raw material materials sources and prices.

5. Reduction in the viscosity of the Increased pipeline flow capabilities heavier oil at fractions lower temperatures.

6. Up-grading the constituents by concentratingReduction of the oil volumes which metals into fewer product streams. require de-contamination treatment.

7. Reducing odour producing organosulfurEliminates catalyst poisoning;
and Lowers nitrogen compound products treatment costs, increases social acceptance ~ ~

8. Increases liquid volume yield Decreases coke yield.

9. Provides a drying agent when glycerolEliminates emulsion formation is generated 10.Reduces the energy cost to delignifyProvides an alternate recovery cellulose pulps. Raises the cost competitivenessmethod for green liquor in of the paper Soda-AD process making 11.Uses wastes as a raw material sourceEliminates wastes including and leaves no environmental footprint pathogenic ones

Claims

1) An upgrading process for waste, low grade oil, petroleum crude, fats or greases comprising:
a) Loading feed material in the form of diverse raw materials in variable proportions with water into a pressure vessel under supercritical conditions, b) Adjusting temperature and pressure in the reaction vessel to cause water to reach supercritical conditions, c) Regulating and maintaining temperature / pressure in the reaction vessel for a minimal 3-10 minutes, d) Isolating the array of products formed by entrapment of the gases, condensation of the liquids in an attached distillation tower and physical collection of the dry residual solids, e) Entrapping carbon dioxide and amines by physical or chemical means, f) Recovering energy to produce a positive energy balance, and g) Separating the gaseous / liquid and solid inorganic / charred cellulosic products.

2) A process as described in claim 1 where diverse raw materials such as plastics, animal/vegetable protein, triglycerides and lipids in a) animal fats, b) animal excrement, and c) vegetable wastes, and resins in tar sands and petroleum heavy oil are chemically transformed into liquid hydrocarbon fuels,

3) A process according to claim 1 where very heavy crude is doctored with waste animal and / or vegetable oils to reduce viscosity so that a more easily pipelineable mixture is formed,

4) A process according to claim 1 where extra water may or may not be required as solvent,

5) A process as described in claim 1 where carbon dioxide and amines are recovered by physical absorption /adsorption /desorption, condensation, crystallization and chemical precipitation to reduce odour,

6) A process as described in claim 1 where amides in plastics such as nylon and animal / vegetable protein, where esters in polyester, and where animal / vegetable esters in triglycerides / lipids, and where resins in tar sands and petroleum heavy oil are hydrolyzed into acids, alcohols, amino acids, ammonia and amines,

7) A process as described in claim 6 where both free and generated acids are decarboxylated to carbon dioxide and "one carbon less" hydrocarbon,

8) A process as described in claim 6 where amino acids are oxidatively decarboxylated to ammonia, carbon dioxide and "one carbon less" aldehyde,

9) A process as described in claim 7 where decarboxylation of emulsion generating carboxylic acids causes partition of oil into separated hydrocarbon and aqueous phases,

10) A process as described in claim 1 where carbon-carbon and carbon-sulfur bonds in natural and synthetic polymers, oligomers, and natural petroleum waxes are reductively cleaved to generate lower molecular weight hydrocarbons and thiols,

11) A process as described in claim 1 where tramp metals such as vanadium, nickel and iron precipitate out because lower molecular weight hydrocarbons cannot solubilize them,

12) A process as described in claim 2 where amines, both added and generated act as catalysts in the hydrolysis of amides, esters, and thioesters,

13) A process as described in claim 12 where amines, both added and generated inhibit the corrosive nature of water at supercritical temperatures,

14) A process as described in claim 1 where iron oxide, sulfide ion and carbonate ion are catalysts,

15) A process as described in claims 1 where the reactions are simultaneously occurring independently, in concert and in cascade fashion,

16) A process as described in claims 1 where reactions occur in 3-10 minutes,

17) A process as described in claims 5 where hydrolysis and decarboxylation occur at a temperature of 200-430°C,

18) A process as described in claim 1 where carbon-carbon and carbon-sulfur scission occurs at a temperature of 430-500°C,

19) A process as described in claim 4 where super critical water reductively hydrogenates the cleaved carbon-carbon and carbon-sulfur terminal radicals without generating coke,

20) A process as described in claim 1 where super critical water with a dielectric constant of .PSI. = 2-5 is miscible with hydrocarbons,

21) A process as described in claim 1 where generated carbon dioxide is precipitated by lime water and amines are trapped as ammonium salts,

22) A process as described in claim 5 where socially unacceptable amine odours are controlled by transforming them into ammonium salts,

23) A process as described in claim 1 where animal and vegetable derived pathogens are destroyed by sterilization at super critical temperatures and pressures,

24) A process as described in claim 1 where the inorganic and poly saccharide fractions of animal/vegetable waste become nitrogen depleted carbonaceous compost,

25) A process as described in claim 2 where a mixture of petroleum and triglycerides generates glycerol that desiccates the hydrocarbon phase,

26) A process where black liquor need not be concentrated in order to separate chemically solubilized lignin from the aqueous phase,

27) A process as described in claim 26 that causes chemically solubilized wood extracted lignin to be chemically transformed into non-aqueous soluble liquid hydrocarbon and solid carbonaceous fuel.

28) A process as described in claim 26 where sulfide catalyst and Kraft sulfide ions respectively are oxidized into sulfate ion,

29) A process where heavy crude petroleum and used lubricating oils can be de-mineralized, decolourized and dried in one step, and finally

30) A process as described in claims 1 and 26 where 50-70% of the heat from the post-reaction cool down process steps is recycled to the pre-reaction raw materials.