CA1182062A - Process for producing solid, liquid and gaseous fuels from organic material - Google Patents
Process for producing solid, liquid and gaseous fuels from organic materialInfo
- Publication number
- CA1182062A CA1182062A CA000390057A CA390057A CA1182062A CA 1182062 A CA1182062 A CA 1182062A CA 000390057 A CA000390057 A CA 000390057A CA 390057 A CA390057 A CA 390057A CA 1182062 A CA1182062 A CA 1182062A
- Authority
- CA
- Canada
- Prior art keywords
- process according
- conversion
- conversion temperature
- starting material
- gases
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired
Links
Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B53/00—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
- C10G1/02—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal by distillation
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L9/00—Treating solid fuels to improve their combustion
- C10L9/08—Treating solid fuels to improve their combustion by heat treatments, e.g. calcining
Abstract
Abstract A process for producing solid, liquid and gaseous fuels comprising the use of an organic starting material selected from a bio-mass of microbial, vegetable or animal origin and sediments or garbage containing organic material heating said organic material under the exclusion of air slowly to a conversion temperature of 200 to 600 °C, conducting the gases and vapors escaping during the heating through suitable gas and liquid separators, maintaining the conversion temperature until the development of gases and vapors has substantially ceased, and isolating the solid conversion residues and the separated gases and
Description
32~i2 BACKGROUND OF THE INVENTION
FIELD OF THE INVENTION
The invention relates to a process for producing solid, gaseous and liquid fuels from organic starting material.
DESCRIPTION OF THE PRIOR ART
1~ Nowadays soLid and liquid fuels are mainly obtained f.rom fossil energy sources, such as coal and petroleum.
A:Lso the synthetic processes for obtaining hydro-carbons, for instance the coal hydrogenation according to P:ier and Bergius or the so-called Fischer-Tropsch process, start out from these ~ossil fuels, especially .Erom coal.
It is believed nowadays that coal origlnated mainly from vegetable material with a high content Of cellulose and that petroleum originatfed from a P,i~ mass of bacteriae. Bacteriae consist~ up to 60 to 80 %
of proteins and lipids. During the formation of petroleum)the he-terofunctional groups oriyinally ~h~
present in the natural material, especially the nitrogen, sulfur, and oxygen hetero-functional groups must have been eliminated from these substances. This must have happenedunder conditionsun~er which no carbon-carbon bonds were cleaved and no oxidative or reductive processes were nècessary. It was not possible up to now to copy this~ believed "natural" course of reaction. In particular no process has been found being capable to convert organi.c material, especially organic material oE vegetable or animal origin at normal pressure and
FIELD OF THE INVENTION
The invention relates to a process for producing solid, gaseous and liquid fuels from organic starting material.
DESCRIPTION OF THE PRIOR ART
1~ Nowadays soLid and liquid fuels are mainly obtained f.rom fossil energy sources, such as coal and petroleum.
A:Lso the synthetic processes for obtaining hydro-carbons, for instance the coal hydrogenation according to P:ier and Bergius or the so-called Fischer-Tropsch process, start out from these ~ossil fuels, especially .Erom coal.
It is believed nowadays that coal origlnated mainly from vegetable material with a high content Of cellulose and that petroleum originatfed from a P,i~ mass of bacteriae. Bacteriae consist~ up to 60 to 80 %
of proteins and lipids. During the formation of petroleum)the he-terofunctional groups oriyinally ~h~
present in the natural material, especially the nitrogen, sulfur, and oxygen hetero-functional groups must have been eliminated from these substances. This must have happenedunder conditionsun~er which no carbon-carbon bonds were cleaved and no oxidative or reductive processes were nècessary. It was not possible up to now to copy this~ believed "natural" course of reaction. In particular no process has been found being capable to convert organi.c material, especially organic material oE vegetable or animal origin at normal pressure and
2~
without using reductive or oxidative processes into solid or liquid fuels.
OBJECTS OF THE INVENTION
It is an obj~ct of the invention to provide a process for producing solid, liquid and gaseous fuels which does not require the use of fossil energy sources but allows the conversion of bio-mass of microbial, vegetable or animal origin and of sediments or garbage containing organic material at normal pressure and without using reduction and oxidation processes.
DETAILRD DESCRIPTION OF T~E INVENTION
According to the present invention there is provided a process for producing solid, liquid and gaseous fuels comprising the use of an organic starting material selected from the group consisting of bio-mass of microbial, vegetable and anlmal origin, heating said organic material ~mder the exclusion o~ a:Lr slowly to a conversion temperature of 220 to 380 C, conclucting the gases and vapors escaping during the heating through suitable gas and liquid ~e~arators, Tnalntaining the conversion temperature until the development oE
~nfl~fl mld va~ors hns 3ubstantlal:Ly ceasecl, and lsolatinp, the 301:Ld conversion re~Ldues and the seyarated gases and liquids.
Preferably carbohydrates, lipids, proteins, humic acids; vegetable material, bacteriae and algae; fresh sludge, sewage sludge and fermentations sludge erom waste water purifying plants; the organic components of private or industrial garbage; and peat and brown coal are used for the present process of conversion.
It is preferred to admix a conversion catalyst with the organic starting mater:Lal be~ore heating. As catalysts an aluminum oxide, an aluminum salt, phosphoric acid, phosphates, borates, silica gel, silicates, aluminum silicate or an oxide of a transition metal or a mixture of these catalysts, respectively, can be employed. An oxide from the group consisting of Ti, V, Cr, Mn, Fe, Co, Ni, Cu or Zn or a mixture of these oxides, respectively, or a mixture of at 21~%
least one of these oxides together ~ith at least one of the compounds mentioned above is used. Especially preferred are aluminum oxide, montmorillonite, mixed catalysts of aluminum oxide/copper oxide, aluminum oxide/vanadium pentoxide and aluminum oxide/nickel oxide.
The conversion temperature is preferably about 250 to about 350 C, and further preferred about 280 ~o about 330 C. A temperature of about 300 C is the most preferred.
It :Ls preferred to heat the organic starting material at a rate of about 5 to about 30 C per minute under the exclusion of air up to the conversion temperature. More preferred is a heating rate of about 10 to about 20 C per minute.
The amount of catalyst is in general 0.01 to 10 % by weight, preferably 0.1 to 6 % by we:Lght, based on the weight of the used organic starting material.
In case the startlng material consists mainly of cellulose and carbo-hydrates (for lnstance materlal of vegetable origin) coal is the main product ob~alncd. In case ~he startlng material consists mainly oE proteins and lipids (~or Ln~ance bio--mass on the basls of mlcro-organisms) then the product oE
converslon conslsts mainly of oils and hydrocarbons.
~L~8~Q~
According to the process of the invention almost 70 to 90 ~ of the carbon originally being present in the used material is converted into coal and oil. The other carbon escapes as a aaseous mixture of CO2, Co, CH4 and lower hydrocarbons. The heat of combustion of the oils thus obtained is between 7 C00 and 10 000 kcal/kg depending on the starting material, reaction condition and catalyst. The heat of combustion of the coal formed a~ounts to ~bout 3 000 and 8 000 kcaltkg depending on the amount of the inorganic residues present in the coal. The oils obtained are free of inorganic residues and relatively pure in sulfur (0.05 to l.0 % by weight S). In this respect they can be compcared with the best petroleum having a sulfur content of 0.3 to 6 % by weight.
The process of the invention is preferably suited for ~ worklng up and converting sewage sludge and fermenta-tion ~3 s~udcJei~ obtalned ~ro~l the biological was-te water purle~lng plc~nts. Thi6 sludye is first mechanically drained (dewatered) in filter presses or centrifuges up to a water content of about 40 to 60 ~ by weight.
This water content is additionally reduced by either drying in the air or by heating so that a dr~, solid bulk ma-terial of powdery or granular type is obtained.
This material is used for the process of the invention.
One heats slowl~ under -the exclusion of air whereby wa-ter is first evaporated which condenses and is ~ollec-ted. The elimination of the heterofunctional groups starts at about 180 to 200 C. This elimination increases strongly at about 250 C and ceases slowly above 320 C. During this process carbon dioxide, carbon monoxide, ammonia, hydrochloric acid, hydrogen sulfide and lower hydrocarbons from methane to hexane are ormed. Ammonia, hydrogen chloride, hydrogen sulfide anc1 a ~rt of the carbon dioxide condense together with ~8~ 6~
water to give harmless ammonium salts and are removed as such from the vapor-phase. Therefore the escaping gases are free of basic substances and contain CO2, CO, CH4 and lower hydrocarbons as principal components.
About 5 litcr of gas having a calorific value of 18 600 kJ/m3 are obtained from 1 kg of sewage sludge.
Since no C-C bonds are cleaved by the low temperature conversion of the invention - which is in contrast to ~ pyrolysis - it is understandable that only a small amount of gas is obtained. This gas serves as a protective gas during the conversion process and l~ prevents thereby the access of air.
The higher h~drocarbons and oils obtained during the conversion escape from the reaction vessel as gases or vapors, respectively. They are liquefied together and reined laterorl. With respect to the petroleum the o:il of conversion thus ob~ained has the advantage that lt does not contain any bitumen and tar which can hard:ly be ut:Llized. The oll of conversion can be ~as:llv proce~sed further for instance by Crack--processes 26 for obtaining gasoline since the oil of conversion can be evaporated quantitatively. Furthermore analytical investigationsof the oil of conversion obtained according to the process of the invention have shown that branchless h~drocarbons and fatty acids can make up to 50 % by weight. The fraction of the fatty acids can be easily removed from the oil. It represents a valuable industrial starting material the price of 'e f~o/e~
which is momentarily higher than that ~ ~x_-_u~
The same holds true for the branchless hydrocarbons.
If desired the fatty acids can also be converted into hydrocarbons in a manner known per se.
32~6~2 Since t,he carbon compounds present in the sewage sludge are converted mainly into oil during the conversion the residue obtained at the end of the converstion process is relatively poor in carbon. However, it is possible to burn i-t directly if the common precautions with respect to the heavy metals eventually being present, especially mercury and cadmium, are taken.
The sul~ur andrlitrogen con-tent of the coal residue is relatively low. It is therefore possible to hyclrogena-te the coal or to use it for the production of water gas.
The process of the invention is preferably performed in 16 a continuous manner by continuously transporting the dry starting material, for instance the dried sewage slu~ye, beiny present as powder or as a granu:Lated material,through a heated reaction tube with the aid of for instance a screw conveyor.
~0 In ~enercll, the conversion process is finished a~ter 2 to 3 hours.
In case sewage sludge is used for the conversion it is in most cases superfluous to add a catalyst material since the inorganic components present in the sewage sludge contain in most cases a sufficient amount of sllicates, aluminum compounds and transition metals.
The industrial cor~version of this material is therefore facilitated substantially.
The following examples are given in illustration of, but not in limitation of/the present invention.
~8;;~
Example 1 100 g of albumin are heated under the exclusion of air to 230 C for 3 hours to give 30 g of an oil and 42 g of a solid, carbon~like product.
Oil: C 70.5 %; H 12.1 ~; heat of combustion 7 500 kcal/kg Coal residue C 79 %; heat of combustion 8 2Q0 kcal/kg.
Example 2 ~' ~ 100 g of dried L~r~ sludge (C 44 %; H 6.66 %; N 8~39 %;
20 ~ residue) are heated under the exclusion oE air up to 320 C or 2.5 hours. 35 g of an oil and 41 g of a ~oltd, carborl-like produc-t are obtained.
Oil: C 66.1 %; H 8.4 %; N 7.5 %; S 0.32 %. Heat of combust:lon 7 100 kca:L/kg.
Carbon residue: 35.39 % C; 1.7 % H; 5,76 ~ N.
R~sldlle~ ~9.85 ~; heat of combustion 3 100 kcal/kg.
_xarn~_e 3 26 100 g of a dried sewage sludge are admixed with 5 g of Al2O3 and 0.1 g CuO and heated ~ 3 hours up to 300 C
uncler the exclusion of air. 42 g of an oil and 39 g of a so:lid product containing carhon are obtained.
Oil: C 75.9 ~; H 10.'2 ~; N 2.08 %; S 0.05 %;
Heat of combustion: 8 900 kcal/kg.
Carbon-like residue: C 40.1 ~; H 1.8 %; N 4.8 %; S 1.26 %;
Residue 42.5 ~; heat of combustion 3 600 kcal/kg.
2~
~xample 4 100 g of a dried mass of bacteriae (streptomyces species) are heated with 5 g of anhydrous montmorillonite under the exclusion of air up to 350 C for 2 hours to give 47 g of an oil and 34 g of a solid residue containing~
carbon.
Oil: C 62 %; H 12.5 %, N 3.2 ~; S 0.3 ~; Heat of combustion 7 800 kcal/kg.
Residue containing carbon: C 52 %; H 1.5 %; N 3.2 %;
S 0.5 %; Residue 30.7 %; heat of combustion 5 100 kcal/kg.
Example 5 100 g of a dried sewage sludge are mlxed with 1 g of Al2O3 and 0.01 g of V2O5 and heated under the exclusion of air up to 400 C for 3 hours t:o give 33 g of an oil and S9 g of a residue.
, O:Ll: C 75.2 '~; H 11.2 %; N 5.06 ~;; S 0.15 %.
Ldue conkaininy carbon: C 37.2 %; H 1.6 ~, residue ~7.2 ~.
215 Instead of V2O5 also 0.1 g of NiO can be added.
Example 6 100 g of sewage sludge are mixed with 1 g of Al2O3 and heated for 2 hours up to 280 C to give 29 g of an oil and 51 g of a solid product con-taining carbon.
Oil: C 70.2 %; H 10.1 %; N 6.1 %; S 0.4 %; heat of combustion 6 950 kcal/kg Residue containing carbon: C 38.9 %; H 3.3 %; N 6.4 %;
S 1.4 %;
Residue: 42.1 %.
Example_ 100 g of cellulose are heated under the exclusion of air up to 250 C for 3 hours to give 5 g of an oil and 50 g of a residue containing carbon.
Residue containing carbon: C 80.5 ~; H 2.4 %; heat of combustion 7 100 kcl/kg.
Example 8 100 g of starch are heated wîth 5 g of A12O3 under the exclusion of air up to 210 C for 3 hours to yield 16 52 g of a xesidue containing carbon and 4 g of an oil.
Residue containing carbon: C 78.8 ~; H 3.2 %; heat of combustion 7 000 kcal/kg.
~0 Example 9 __ 100 g o~ humic acld from brown~coal are mixed with 1 g o~ ~l2O3 and 0.1 g of CuO and heated under the exclusion of air up to 390 C. Yield 10 g of an oil and 51 g of a residue containing carbon.
Oil C 78.9; H 11.4 %, N 1.5 %; S 0.1 %; heat of com-bustion 9 200 kcal/kg.
Residue containing carbon- C 80.1 %; H 3.2 ~; N 1.5 %;
S 0.3 %; heat of combustion 7 100 kcal/kg.
Example 10 100 g of private garbage finely y~verized are mixed with 1 g A12O3 and 0.1 g of CuO and heated under the exclusion of air up to 360 C for 4 hours to yield 20 g of an oil and 51 g of a residue containing carbon.
206;~
Oil: C 7~.2 %; H 11~3 %; N 1.0 %; S 0.3 %.
Residue containing carbon: C 43.4 %; H 3.75 %; N 1.5 %;
5 S 0.7 9~;
Residue 37 . 0 % .
1 1 1 /Hch
without using reductive or oxidative processes into solid or liquid fuels.
OBJECTS OF THE INVENTION
It is an obj~ct of the invention to provide a process for producing solid, liquid and gaseous fuels which does not require the use of fossil energy sources but allows the conversion of bio-mass of microbial, vegetable or animal origin and of sediments or garbage containing organic material at normal pressure and without using reduction and oxidation processes.
DETAILRD DESCRIPTION OF T~E INVENTION
According to the present invention there is provided a process for producing solid, liquid and gaseous fuels comprising the use of an organic starting material selected from the group consisting of bio-mass of microbial, vegetable and anlmal origin, heating said organic material ~mder the exclusion o~ a:Lr slowly to a conversion temperature of 220 to 380 C, conclucting the gases and vapors escaping during the heating through suitable gas and liquid ~e~arators, Tnalntaining the conversion temperature until the development oE
~nfl~fl mld va~ors hns 3ubstantlal:Ly ceasecl, and lsolatinp, the 301:Ld conversion re~Ldues and the seyarated gases and liquids.
Preferably carbohydrates, lipids, proteins, humic acids; vegetable material, bacteriae and algae; fresh sludge, sewage sludge and fermentations sludge erom waste water purifying plants; the organic components of private or industrial garbage; and peat and brown coal are used for the present process of conversion.
It is preferred to admix a conversion catalyst with the organic starting mater:Lal be~ore heating. As catalysts an aluminum oxide, an aluminum salt, phosphoric acid, phosphates, borates, silica gel, silicates, aluminum silicate or an oxide of a transition metal or a mixture of these catalysts, respectively, can be employed. An oxide from the group consisting of Ti, V, Cr, Mn, Fe, Co, Ni, Cu or Zn or a mixture of these oxides, respectively, or a mixture of at 21~%
least one of these oxides together ~ith at least one of the compounds mentioned above is used. Especially preferred are aluminum oxide, montmorillonite, mixed catalysts of aluminum oxide/copper oxide, aluminum oxide/vanadium pentoxide and aluminum oxide/nickel oxide.
The conversion temperature is preferably about 250 to about 350 C, and further preferred about 280 ~o about 330 C. A temperature of about 300 C is the most preferred.
It :Ls preferred to heat the organic starting material at a rate of about 5 to about 30 C per minute under the exclusion of air up to the conversion temperature. More preferred is a heating rate of about 10 to about 20 C per minute.
The amount of catalyst is in general 0.01 to 10 % by weight, preferably 0.1 to 6 % by we:Lght, based on the weight of the used organic starting material.
In case the startlng material consists mainly of cellulose and carbo-hydrates (for lnstance materlal of vegetable origin) coal is the main product ob~alncd. In case ~he startlng material consists mainly oE proteins and lipids (~or Ln~ance bio--mass on the basls of mlcro-organisms) then the product oE
converslon conslsts mainly of oils and hydrocarbons.
~L~8~Q~
According to the process of the invention almost 70 to 90 ~ of the carbon originally being present in the used material is converted into coal and oil. The other carbon escapes as a aaseous mixture of CO2, Co, CH4 and lower hydrocarbons. The heat of combustion of the oils thus obtained is between 7 C00 and 10 000 kcal/kg depending on the starting material, reaction condition and catalyst. The heat of combustion of the coal formed a~ounts to ~bout 3 000 and 8 000 kcaltkg depending on the amount of the inorganic residues present in the coal. The oils obtained are free of inorganic residues and relatively pure in sulfur (0.05 to l.0 % by weight S). In this respect they can be compcared with the best petroleum having a sulfur content of 0.3 to 6 % by weight.
The process of the invention is preferably suited for ~ worklng up and converting sewage sludge and fermenta-tion ~3 s~udcJei~ obtalned ~ro~l the biological was-te water purle~lng plc~nts. Thi6 sludye is first mechanically drained (dewatered) in filter presses or centrifuges up to a water content of about 40 to 60 ~ by weight.
This water content is additionally reduced by either drying in the air or by heating so that a dr~, solid bulk ma-terial of powdery or granular type is obtained.
This material is used for the process of the invention.
One heats slowl~ under -the exclusion of air whereby wa-ter is first evaporated which condenses and is ~ollec-ted. The elimination of the heterofunctional groups starts at about 180 to 200 C. This elimination increases strongly at about 250 C and ceases slowly above 320 C. During this process carbon dioxide, carbon monoxide, ammonia, hydrochloric acid, hydrogen sulfide and lower hydrocarbons from methane to hexane are ormed. Ammonia, hydrogen chloride, hydrogen sulfide anc1 a ~rt of the carbon dioxide condense together with ~8~ 6~
water to give harmless ammonium salts and are removed as such from the vapor-phase. Therefore the escaping gases are free of basic substances and contain CO2, CO, CH4 and lower hydrocarbons as principal components.
About 5 litcr of gas having a calorific value of 18 600 kJ/m3 are obtained from 1 kg of sewage sludge.
Since no C-C bonds are cleaved by the low temperature conversion of the invention - which is in contrast to ~ pyrolysis - it is understandable that only a small amount of gas is obtained. This gas serves as a protective gas during the conversion process and l~ prevents thereby the access of air.
The higher h~drocarbons and oils obtained during the conversion escape from the reaction vessel as gases or vapors, respectively. They are liquefied together and reined laterorl. With respect to the petroleum the o:il of conversion thus ob~ained has the advantage that lt does not contain any bitumen and tar which can hard:ly be ut:Llized. The oll of conversion can be ~as:llv proce~sed further for instance by Crack--processes 26 for obtaining gasoline since the oil of conversion can be evaporated quantitatively. Furthermore analytical investigationsof the oil of conversion obtained according to the process of the invention have shown that branchless h~drocarbons and fatty acids can make up to 50 % by weight. The fraction of the fatty acids can be easily removed from the oil. It represents a valuable industrial starting material the price of 'e f~o/e~
which is momentarily higher than that ~ ~x_-_u~
The same holds true for the branchless hydrocarbons.
If desired the fatty acids can also be converted into hydrocarbons in a manner known per se.
32~6~2 Since t,he carbon compounds present in the sewage sludge are converted mainly into oil during the conversion the residue obtained at the end of the converstion process is relatively poor in carbon. However, it is possible to burn i-t directly if the common precautions with respect to the heavy metals eventually being present, especially mercury and cadmium, are taken.
The sul~ur andrlitrogen con-tent of the coal residue is relatively low. It is therefore possible to hyclrogena-te the coal or to use it for the production of water gas.
The process of the invention is preferably performed in 16 a continuous manner by continuously transporting the dry starting material, for instance the dried sewage slu~ye, beiny present as powder or as a granu:Lated material,through a heated reaction tube with the aid of for instance a screw conveyor.
~0 In ~enercll, the conversion process is finished a~ter 2 to 3 hours.
In case sewage sludge is used for the conversion it is in most cases superfluous to add a catalyst material since the inorganic components present in the sewage sludge contain in most cases a sufficient amount of sllicates, aluminum compounds and transition metals.
The industrial cor~version of this material is therefore facilitated substantially.
The following examples are given in illustration of, but not in limitation of/the present invention.
~8;;~
Example 1 100 g of albumin are heated under the exclusion of air to 230 C for 3 hours to give 30 g of an oil and 42 g of a solid, carbon~like product.
Oil: C 70.5 %; H 12.1 ~; heat of combustion 7 500 kcal/kg Coal residue C 79 %; heat of combustion 8 2Q0 kcal/kg.
Example 2 ~' ~ 100 g of dried L~r~ sludge (C 44 %; H 6.66 %; N 8~39 %;
20 ~ residue) are heated under the exclusion oE air up to 320 C or 2.5 hours. 35 g of an oil and 41 g of a ~oltd, carborl-like produc-t are obtained.
Oil: C 66.1 %; H 8.4 %; N 7.5 %; S 0.32 %. Heat of combust:lon 7 100 kca:L/kg.
Carbon residue: 35.39 % C; 1.7 % H; 5,76 ~ N.
R~sldlle~ ~9.85 ~; heat of combustion 3 100 kcal/kg.
_xarn~_e 3 26 100 g of a dried sewage sludge are admixed with 5 g of Al2O3 and 0.1 g CuO and heated ~ 3 hours up to 300 C
uncler the exclusion of air. 42 g of an oil and 39 g of a so:lid product containing carhon are obtained.
Oil: C 75.9 ~; H 10.'2 ~; N 2.08 %; S 0.05 %;
Heat of combustion: 8 900 kcal/kg.
Carbon-like residue: C 40.1 ~; H 1.8 %; N 4.8 %; S 1.26 %;
Residue 42.5 ~; heat of combustion 3 600 kcal/kg.
2~
~xample 4 100 g of a dried mass of bacteriae (streptomyces species) are heated with 5 g of anhydrous montmorillonite under the exclusion of air up to 350 C for 2 hours to give 47 g of an oil and 34 g of a solid residue containing~
carbon.
Oil: C 62 %; H 12.5 %, N 3.2 ~; S 0.3 ~; Heat of combustion 7 800 kcal/kg.
Residue containing carbon: C 52 %; H 1.5 %; N 3.2 %;
S 0.5 %; Residue 30.7 %; heat of combustion 5 100 kcal/kg.
Example 5 100 g of a dried sewage sludge are mlxed with 1 g of Al2O3 and 0.01 g of V2O5 and heated under the exclusion of air up to 400 C for 3 hours t:o give 33 g of an oil and S9 g of a residue.
, O:Ll: C 75.2 '~; H 11.2 %; N 5.06 ~;; S 0.15 %.
Ldue conkaininy carbon: C 37.2 %; H 1.6 ~, residue ~7.2 ~.
215 Instead of V2O5 also 0.1 g of NiO can be added.
Example 6 100 g of sewage sludge are mixed with 1 g of Al2O3 and heated for 2 hours up to 280 C to give 29 g of an oil and 51 g of a solid product con-taining carbon.
Oil: C 70.2 %; H 10.1 %; N 6.1 %; S 0.4 %; heat of combustion 6 950 kcal/kg Residue containing carbon: C 38.9 %; H 3.3 %; N 6.4 %;
S 1.4 %;
Residue: 42.1 %.
Example_ 100 g of cellulose are heated under the exclusion of air up to 250 C for 3 hours to give 5 g of an oil and 50 g of a residue containing carbon.
Residue containing carbon: C 80.5 ~; H 2.4 %; heat of combustion 7 100 kcl/kg.
Example 8 100 g of starch are heated wîth 5 g of A12O3 under the exclusion of air up to 210 C for 3 hours to yield 16 52 g of a xesidue containing carbon and 4 g of an oil.
Residue containing carbon: C 78.8 ~; H 3.2 %; heat of combustion 7 000 kcal/kg.
~0 Example 9 __ 100 g o~ humic acld from brown~coal are mixed with 1 g o~ ~l2O3 and 0.1 g of CuO and heated under the exclusion of air up to 390 C. Yield 10 g of an oil and 51 g of a residue containing carbon.
Oil C 78.9; H 11.4 %, N 1.5 %; S 0.1 %; heat of com-bustion 9 200 kcal/kg.
Residue containing carbon- C 80.1 %; H 3.2 ~; N 1.5 %;
S 0.3 %; heat of combustion 7 100 kcal/kg.
Example 10 100 g of private garbage finely y~verized are mixed with 1 g A12O3 and 0.1 g of CuO and heated under the exclusion of air up to 360 C for 4 hours to yield 20 g of an oil and 51 g of a residue containing carbon.
206;~
Oil: C 7~.2 %; H 11~3 %; N 1.0 %; S 0.3 %.
Residue containing carbon: C 43.4 %; H 3.75 %; N 1.5 %;
5 S 0.7 9~;
Residue 37 . 0 % .
1 1 1 /Hch
Claims (11)
PROPERTY OR PRIVILEGE IS CLAIMED ARE DEFINED AS FOLLOWS:
1. A process for producing solid, liquid and gaseous fuels comprising the use of an organic starting material selected from the group consisting of bio-mass of microbial, vegetable and animal origin, heating said organic material under the exclusion of air slowly to a conversion temperature of 220 to 38°C, conducting the gases and vapors escaping during the heating through suitable gas and liquid separators, maintaining the conversion temperature until the development of gases and vapors has substantially ceased, and isolating the solid conversion residues and the separated gases and liquids.
2. A process according to claim 1 wherein the starting material is selected from the group consisting of carbohydrates, lipids, proteins, humic acids;
vegetable material, bacteriae and algae; fresh sludge, sewage sludge and fer-mentation sludge from waste water purifying plants; the organic components of private or industrial garbage; and peat and brown coal.
vegetable material, bacteriae and algae; fresh sludge, sewage sludge and fer-mentation sludge from waste water purifying plants; the organic components of private or industrial garbage; and peat and brown coal.
3. A process according to claim 1 wherein a conversion catalyst is admixed to the organic starting material before heating.
4. A process according to claim 3 wherein a catalyst selected from the group consisting of aluminum oxide, an aluminum salt, phosphoric acid, a phosphate, a borate, silica gel, a silicate, an aluminum silicate or an oxide of a tran-sition metal or a mixture of these catalysts, respectively, is used.
5. A process according to claim 4 wherein an oxide of a transition metal selected from the group consisting of Ti, V, Cr, Mn, Fe, Co, Ni, Cu or Zn or a mixture of these oxides, respectively or a mixture of at least one of these oxides together with at least one of the compounds mentioned in claim 4 is used.
6. A process according to anyone of claim 3, 4 or 5 wherein a catalyst selected from the group consisting of A1203, montmorillonite, A1203+CuO, A1203+V205 or A1203+Ni0 is used.
7. Process according to claim 1, 2 or 3, wherein a conversion temperature of 250 to 350°C is applied.
8. Process according to claim 1, 2 or 3, wherein a conversion temperature of 280 to 330 °C is applied.
9. A process according to claim 1, 2 or 3, wherein a conversion temperature of about 300 °C is applied.
10. A process according to claim 1, 2 or 3 wherein the organic starting material is heated at a rate of 5 to 30 °C per minute up to the conversion temperature.
11. A process according to claim 1, 2 or 3, wherein the organic starting material is heated at a rate of 10 to 20 °C. per minute up to the conversion temperature.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| DE19803042964 DE3042964A1 (en) | 1980-11-14 | 1980-11-14 | METHOD FOR ELIMINATING HETEROATOMES FROM BIOLOGICAL MATERIAL AND ORGANIC SEDIMENTS FOR CONVERTING TO SOLID AND LIQUID FUELS |
| DEP3042964.2 | 1980-11-14 |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CA1182062A true CA1182062A (en) | 1985-02-05 |
Family
ID=6116767
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA000390057A Expired CA1182062A (en) | 1980-11-14 | 1981-11-13 | Process for producing solid, liquid and gaseous fuels from organic material |
Country Status (6)
| Country | Link |
|---|---|
| US (1) | US5114541A (en) |
| EP (1) | EP0052334B2 (en) |
| JP (1) | JPS57111380A (en) |
| AT (1) | ATE20759T1 (en) |
| CA (1) | CA1182062A (en) |
| DE (2) | DE3042964A1 (en) |
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| DE624843C (en) * | 1926-04-23 | 1936-01-30 | I G Farbenindustrie Akt Ges | Conversion of resins into hydrocarbons |
| US3962044A (en) * | 1972-07-05 | 1976-06-08 | The Regents Of The University Of California | Heat treating excreta and products thereof |
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| US4111800A (en) * | 1976-10-06 | 1978-09-05 | Harendza Harinxma Alfred J | Process for treating municipal solid waste and raw sewage sludge |
| JPS544903A (en) * | 1977-06-14 | 1979-01-16 | Agency Of Ind Science & Technol | Method of recovering oils from condensed water formed on thermal decomposition of municipal waste |
| US4300009A (en) * | 1978-12-28 | 1981-11-10 | Mobil Oil Corporation | Conversion of biological material to liquid fuels |
| US4298350A (en) * | 1979-09-17 | 1981-11-03 | Occidental Research Corporation | Method of embrittling waste |
-
1980
- 1980-11-14 DE DE19803042964 patent/DE3042964A1/en not_active Withdrawn
-
1981
- 1981-11-10 EP EP81109604A patent/EP0052334B2/en not_active Expired - Lifetime
- 1981-11-10 DE DE8181109604T patent/DE3174939D1/en not_active Expired
- 1981-11-10 AT AT81109604T patent/ATE20759T1/en not_active IP Right Cessation
- 1981-11-13 CA CA000390057A patent/CA1182062A/en not_active Expired
- 1981-11-13 JP JP56182970A patent/JPS57111380A/en active Granted
-
1991
- 1991-05-13 US US07/698,897 patent/US5114541A/en not_active Expired - Lifetime
Also Published As
| Publication number | Publication date |
|---|---|
| DE3174939D1 (en) | 1986-08-21 |
| US5114541A (en) | 1992-05-19 |
| EP0052334B1 (en) | 1986-07-16 |
| JPH0461037B2 (en) | 1992-09-29 |
| EP0052334A3 (en) | 1982-11-10 |
| EP0052334B2 (en) | 1994-05-11 |
| DE3042964A1 (en) | 1982-07-01 |
| ATE20759T1 (en) | 1986-08-15 |
| JPS57111380A (en) | 1982-07-10 |
| EP0052334A2 (en) | 1982-05-26 |
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