CA1150172A - Process for the upgrading of low-grade solid fuel - Google Patents
Process for the upgrading of low-grade solid fuelInfo
- Publication number
- CA1150172A CA1150172A CA000359082A CA359082A CA1150172A CA 1150172 A CA1150172 A CA 1150172A CA 000359082 A CA000359082 A CA 000359082A CA 359082 A CA359082 A CA 359082A CA 1150172 A CA1150172 A CA 1150172A
- Authority
- CA
- Canada
- Prior art keywords
- fuel
- water
- heating
- acid
- tar
- 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
- C10F—DRYING OR WORKING-UP OF PEAT
- C10F5/00—Drying or de-watering peat
-
- 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
Landscapes
- Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Organic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Combustion & Propulsion (AREA)
- Solid Fuels And Fuel-Associated Substances (AREA)
- Catalysts (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
ABSTRACT
A process for the upgrading of low-grade solid fuel by heating at a temperature above 300°C in the presence of water, in which before or during the heating above 300°C
acid is added to the fuel.
A process for the upgrading of low-grade solid fuel by heating at a temperature above 300°C in the presence of water, in which before or during the heating above 300°C
acid is added to the fuel.
Description
PROGESS FOR THE UPGRADI~G OF LOW-GRADE
SOLID FUEL
The invention relates to a process for the upgrading of low-grade solid f`uel by heating at a temperature above 300 C
in the presence of water. In this specification the term low-grade solid fuel is meant to denote carbon-containing material of which the carbon originates from photo-synthesis and which can be available in various degrees of coalification (such as biomass, vegetable material, ref~se, manure, peat and brown coal)j the term low-grade solid fuel is meant to denote also a material, mentioned above, which has already undergone a pretreatment. For the sake of brevity, such materials will in this specification be denoted by the term "~uel".
As a rule, this fuel contains much water. The water is partly physically absorbed, partly bound in gel structures and partly chemically bound. The fuel also contains many oxygen-containing groups. The calorific value of the fuel can be considerably increased by removing as much wa-ter as possible, by means of a dewatering process, and oxygen-containing groups, by means of a decarboxylation process.
This removal can very conveniently be carried out by heating above 300 C in the presence of water. A considerable amount of the water present in the fuel is thus removed and a high degree of` decarbox~ylation is effected. The result is a fuel with a greatly increased value, with a low water content and a high calorific value. The heating may take place in the presence of liauid and/or vaporous water, but the presence o~ water is of importance for the decarbox~lation.
In the untreated state ~uel ma~ already contain tar, which can be separated from it by extraction; heating the fuel above 300C may in certain cases increase the amount 7~
of tar separated from the upgraded solid fuel.
It has now been found that the amount of tar formed in the above heating can be considerably increased by reducing the pH of the water present in the fuel.
According to the invention, in the process for the up-grading of low-grade solid fuel by heating to a temperature above 300 C in the presence of water, acid is added to the fuel before or during heating.
In addition to a high-grade fuel a considerable amount of tar can be obtained in this way. Thus, more than 10~w of the low-grade fuel can be converted into tar. At least part of the tar formed is suitably separatea from the upgraded fuel and/or is advantageousl~ used for pelletizing or briquetting the upgraded solid fuel.
The tar obtained typically has a highly aliphatic character and a low content of polyaromatic constituents.
The nature of the acid added is not ver~ important. It may be an inorganic acid such as hydrochloric acid or sulphuric acid. Organic acids such as lignosulphonic acid may also be used, very suitable are formic acid and acetic acid. Aroma-tic alcohols, for instance phenol, may also be used.
The desired effect of the heating is achieved at a temper-ature above 300C. Depending on the fuel to be treated, it may be useful to choose a temperature well above 300 C.
The heating ma~ be carried out at a pressure lower than 85 atm. The water which is liberated from the fuel will then evaporate.
When the heating is carried out at a temperature belo~
the critical temperature of water (374C)~ evaporation of the water can be prevented by heating at a pressure which is higher than the water vapour pressure at the temperature chosen. The water liberated from the fuel will then remain in the li~uid state and can be separated as such fro~ the upgraded fuel.
.: , ~LS~Z
During the heating part of` the tar fo~ed can be entrained by steam or liquid water and be reco~ered from it. The tar present in the upgraded fuel after heating may be separated fro~ it by various known methods, f~r instance by extraction with solvents such as toluene, by supercritical extraction, or by azeotropic distillation with steam.
It is preferred to add so much acid to the fuel that the p~ of the water present in it becomes 6 or lower.
Further reduction of the pH to values varying from 3.5 to 5 may in many cases lead to an additional rise in tar yield.
- It may be advantageous to impregnate the fuel with the acid before heating. This enables the acid to reduce the pH
of the water present in th~fuel. The reactions leading to a higher tar yield can thus start earlier. By subjecting the fuel to the heat treatment without an excess of acid the acid consu~ption can be considerably reduced and the risk of cor-rosion of the equipment used will be smaller.
After the addition of the acid it may be use~ul not to start the heating until after some time, so that the diffusion of the acid in the fuel, especially when the latter consists of fairly large lumps, becomes more complete, whilst reactions between the fuel and the acid are already under wa~. This leads to a further decrease of the amount of acid re~uired.
In case the heating at a temperature above 300C is carried out at a pressure below 85 atm. (Nhich means that no liquid water is present during the heating), the acid should be added before the heating. It is in this case preferred to subject the fuel to a pretreatment aiming at the removal o~ the greater part of the water before the heating above 300C; the acid is then added before or during the pretreatment of the fuel at a temperature between 150 and 300C and a pressure which is higher than the water vapour pressure at the temperature used, and the pretreated fuel is separated from expelled water before being heated to above 300C.
' ` '` ~
7æ
Such a process has the great advantage that prior to the heating above 30Q C a considerable part of the water present in the fuel is removed at a relatively low pressure without evaporating the water, whilst during the heating abo~e 300C
a very high degree of decarboxylation, upgrading and tar formation takes place at a much higher temperature without the necessity of increasing the pressure. The evaporation o~ the small amount o~ water still present when heating above 300 C is no real drawback.
The invention will no~ be explained with reference to ~our Examples.
EXAMPLE I
An Australian brown coal with a water content of 60.o%w and an ash content of 1.0%w was suspended in water (6 parts of water to 10 parts of brown coal) to which technically pure glacial acetic acid had been added until a pH of 3.5 was ob-tained (14 parts of gl&cial acetic acid to 1000 parts of brown coal), and subsequently heated in an autoclave to 340C (heat-ing rate 8C/min.).
The autoclave was then opened and water (pH 4.0) and coal were separated by means of a sieve; a hard black coal with a water content of 15%w was obtained.
This hard black coal was then extracted with toluene, whereupon an amount o~ tar went into solution corresponding to 6.8%w of the original brown coal.
For comparison, the original brown coal was extracted with toluene, which yielded an amou~t of tar equal to 1.2~w Of the brown coal.
For further comparison, the above upgrading of the brown coal was repeated with omission of the glacial acetic acid;
the ultimate tar yield was 2.4~ow of the original brown coal and the pH o~ the water after completion of the upgrading was 7.5.
:' ~ . .
- , :,,: i -:, , ; ~ :' .
, ; . ~
-The above example, together with the comparative tests, shows that there are circumstances under which acidification ;
of a brown coal - before subjectlng it to heating above 300C -has an effect on the tar ~ield.
EXAMPLE II
Cow manure was suspended in water to which so much glacial acetic acid had been added that the pH was 4.5, and the suspension was heated in an autocl&ve to 325 C, a~ter which a coal was sieved off~ In this upgrading process per 100 pbw ash-free and water-~ree material present in the cow manure~ 40 pbw ash-free and water-free coal were obtained from which 25 pbw tar could be recovered by extraction.
When this test was repeated with omission of the glacial acetic acid (the pH of the cow-manure suspension in water was in this case 7.5), 34 pbw ash-free and water-free coal were obtained per 100 pbw ash-free and water-free ma-terial present in the COW manure, from which 11 pbw tar could be recovered by extraction.
By extraction of the cow manure itself o~ly 4 pbw tar were obtained per 100 pbw ash-free and water-free material present in the cow manure.
This example shows that the process according to the in-vention increases the tar yield in the upgrading of cow manure.
EXAMPLE III
2500 g of the Australian brown coal used in Example I, containing 1500 g water, 9~5 g organic material and 25 g ash, were subjected, in an aqueous suspension after acidification to a pH o~ 3.5, to a pretre~tment a-t 240C. ~his pretreatment was carried o~t in an autoclave at a pressure higher than the water-vapour pressure at 240 C. Thus, after separation of the liquid water, 1300 g partly coalified product was obtained, containing 300 g water, 975 g organic material and 25 g ash.
This product was subjected at atmospheric pressure to a further treatment at 340C, in which hea-ting was effected .
7~
directly by superheated steam. Thus, 645 g water free coal were obtained, containing 25 g ash and 140 g tar. The tar had been entrained by the steam and was reco~ered from it by condensation.
So, in this case the tar yield was 5.6%w of the original brown coal.
EXAMPLE IV
1000 g of the Australian brown coal used in Example I, containing 600 g water, 390 g organic material and 10 g ash, were subjected~ in an aqueous suspension after acidification to a pH of 3.0, to a pretreatment by heating it to 250C
(heating rate 10C/minute). This pretreatment was carried out in an autocla~e at a pressure higher than the water-vapour pressure at 250C and was continued during 30 minutes.
Thus, after separation of the liquid water, 520 g partly 15 coalified product ~re obtained, containing 120 g water, 390 g organic material and 10 g ash.
This product was subjected at a pressure of 50 bar to a fu~ther heating to 340C, in which heating was effected directly by superheated steam (heating rate ôC/minute, followed by cooling im~ediately after the temperature of 340C had been reached). Thus, 258 g water-free coal were obtained, containing 10 g ash and 56 g tar.
Without separation of the tar the product was pressed to briquettes with a diameter of 11.5 mm. The crushing strength of the briquettes formed was 29.9 ~ewton.
For comparison reasons the two-stage process was repeated using identical conditions with the exception of the pH which was kept 8 in this case. The crushing strength of the briquettes formed was now only 6.1 ~ewton.
By briquetting of the Australian brown coal itself (without applying a heat treatment at all) briquettes were ob-t&ined with a crushing strength of only 4.0 ~ewton. By briquetting of the first-stage product of the two-stage heat treatment the crushing strength of the briquettes formed was 6.o ~ewton and 7.5 ~ewton respectively when a pH = 8 and a pX = 3 was applied.
.
- .
: . .
- , ~ .. :
~ . .
: . ' '.' : '
SOLID FUEL
The invention relates to a process for the upgrading of low-grade solid f`uel by heating at a temperature above 300 C
in the presence of water. In this specification the term low-grade solid fuel is meant to denote carbon-containing material of which the carbon originates from photo-synthesis and which can be available in various degrees of coalification (such as biomass, vegetable material, ref~se, manure, peat and brown coal)j the term low-grade solid fuel is meant to denote also a material, mentioned above, which has already undergone a pretreatment. For the sake of brevity, such materials will in this specification be denoted by the term "~uel".
As a rule, this fuel contains much water. The water is partly physically absorbed, partly bound in gel structures and partly chemically bound. The fuel also contains many oxygen-containing groups. The calorific value of the fuel can be considerably increased by removing as much wa-ter as possible, by means of a dewatering process, and oxygen-containing groups, by means of a decarboxylation process.
This removal can very conveniently be carried out by heating above 300 C in the presence of water. A considerable amount of the water present in the fuel is thus removed and a high degree of` decarbox~ylation is effected. The result is a fuel with a greatly increased value, with a low water content and a high calorific value. The heating may take place in the presence of liauid and/or vaporous water, but the presence o~ water is of importance for the decarbox~lation.
In the untreated state ~uel ma~ already contain tar, which can be separated from it by extraction; heating the fuel above 300C may in certain cases increase the amount 7~
of tar separated from the upgraded solid fuel.
It has now been found that the amount of tar formed in the above heating can be considerably increased by reducing the pH of the water present in the fuel.
According to the invention, in the process for the up-grading of low-grade solid fuel by heating to a temperature above 300 C in the presence of water, acid is added to the fuel before or during heating.
In addition to a high-grade fuel a considerable amount of tar can be obtained in this way. Thus, more than 10~w of the low-grade fuel can be converted into tar. At least part of the tar formed is suitably separatea from the upgraded fuel and/or is advantageousl~ used for pelletizing or briquetting the upgraded solid fuel.
The tar obtained typically has a highly aliphatic character and a low content of polyaromatic constituents.
The nature of the acid added is not ver~ important. It may be an inorganic acid such as hydrochloric acid or sulphuric acid. Organic acids such as lignosulphonic acid may also be used, very suitable are formic acid and acetic acid. Aroma-tic alcohols, for instance phenol, may also be used.
The desired effect of the heating is achieved at a temper-ature above 300C. Depending on the fuel to be treated, it may be useful to choose a temperature well above 300 C.
The heating ma~ be carried out at a pressure lower than 85 atm. The water which is liberated from the fuel will then evaporate.
When the heating is carried out at a temperature belo~
the critical temperature of water (374C)~ evaporation of the water can be prevented by heating at a pressure which is higher than the water vapour pressure at the temperature chosen. The water liberated from the fuel will then remain in the li~uid state and can be separated as such fro~ the upgraded fuel.
.: , ~LS~Z
During the heating part of` the tar fo~ed can be entrained by steam or liquid water and be reco~ered from it. The tar present in the upgraded fuel after heating may be separated fro~ it by various known methods, f~r instance by extraction with solvents such as toluene, by supercritical extraction, or by azeotropic distillation with steam.
It is preferred to add so much acid to the fuel that the p~ of the water present in it becomes 6 or lower.
Further reduction of the pH to values varying from 3.5 to 5 may in many cases lead to an additional rise in tar yield.
- It may be advantageous to impregnate the fuel with the acid before heating. This enables the acid to reduce the pH
of the water present in th~fuel. The reactions leading to a higher tar yield can thus start earlier. By subjecting the fuel to the heat treatment without an excess of acid the acid consu~ption can be considerably reduced and the risk of cor-rosion of the equipment used will be smaller.
After the addition of the acid it may be use~ul not to start the heating until after some time, so that the diffusion of the acid in the fuel, especially when the latter consists of fairly large lumps, becomes more complete, whilst reactions between the fuel and the acid are already under wa~. This leads to a further decrease of the amount of acid re~uired.
In case the heating at a temperature above 300C is carried out at a pressure below 85 atm. (Nhich means that no liquid water is present during the heating), the acid should be added before the heating. It is in this case preferred to subject the fuel to a pretreatment aiming at the removal o~ the greater part of the water before the heating above 300C; the acid is then added before or during the pretreatment of the fuel at a temperature between 150 and 300C and a pressure which is higher than the water vapour pressure at the temperature used, and the pretreated fuel is separated from expelled water before being heated to above 300C.
' ` '` ~
7æ
Such a process has the great advantage that prior to the heating above 30Q C a considerable part of the water present in the fuel is removed at a relatively low pressure without evaporating the water, whilst during the heating abo~e 300C
a very high degree of decarboxylation, upgrading and tar formation takes place at a much higher temperature without the necessity of increasing the pressure. The evaporation o~ the small amount o~ water still present when heating above 300 C is no real drawback.
The invention will no~ be explained with reference to ~our Examples.
EXAMPLE I
An Australian brown coal with a water content of 60.o%w and an ash content of 1.0%w was suspended in water (6 parts of water to 10 parts of brown coal) to which technically pure glacial acetic acid had been added until a pH of 3.5 was ob-tained (14 parts of gl&cial acetic acid to 1000 parts of brown coal), and subsequently heated in an autoclave to 340C (heat-ing rate 8C/min.).
The autoclave was then opened and water (pH 4.0) and coal were separated by means of a sieve; a hard black coal with a water content of 15%w was obtained.
This hard black coal was then extracted with toluene, whereupon an amount o~ tar went into solution corresponding to 6.8%w of the original brown coal.
For comparison, the original brown coal was extracted with toluene, which yielded an amou~t of tar equal to 1.2~w Of the brown coal.
For further comparison, the above upgrading of the brown coal was repeated with omission of the glacial acetic acid;
the ultimate tar yield was 2.4~ow of the original brown coal and the pH o~ the water after completion of the upgrading was 7.5.
:' ~ . .
- , :,,: i -:, , ; ~ :' .
, ; . ~
-The above example, together with the comparative tests, shows that there are circumstances under which acidification ;
of a brown coal - before subjectlng it to heating above 300C -has an effect on the tar ~ield.
EXAMPLE II
Cow manure was suspended in water to which so much glacial acetic acid had been added that the pH was 4.5, and the suspension was heated in an autocl&ve to 325 C, a~ter which a coal was sieved off~ In this upgrading process per 100 pbw ash-free and water-~ree material present in the cow manure~ 40 pbw ash-free and water-free coal were obtained from which 25 pbw tar could be recovered by extraction.
When this test was repeated with omission of the glacial acetic acid (the pH of the cow-manure suspension in water was in this case 7.5), 34 pbw ash-free and water-free coal were obtained per 100 pbw ash-free and water-free ma-terial present in the COW manure, from which 11 pbw tar could be recovered by extraction.
By extraction of the cow manure itself o~ly 4 pbw tar were obtained per 100 pbw ash-free and water-free material present in the cow manure.
This example shows that the process according to the in-vention increases the tar yield in the upgrading of cow manure.
EXAMPLE III
2500 g of the Australian brown coal used in Example I, containing 1500 g water, 9~5 g organic material and 25 g ash, were subjected, in an aqueous suspension after acidification to a pH o~ 3.5, to a pretre~tment a-t 240C. ~his pretreatment was carried o~t in an autoclave at a pressure higher than the water-vapour pressure at 240 C. Thus, after separation of the liquid water, 1300 g partly coalified product was obtained, containing 300 g water, 975 g organic material and 25 g ash.
This product was subjected at atmospheric pressure to a further treatment at 340C, in which hea-ting was effected .
7~
directly by superheated steam. Thus, 645 g water free coal were obtained, containing 25 g ash and 140 g tar. The tar had been entrained by the steam and was reco~ered from it by condensation.
So, in this case the tar yield was 5.6%w of the original brown coal.
EXAMPLE IV
1000 g of the Australian brown coal used in Example I, containing 600 g water, 390 g organic material and 10 g ash, were subjected~ in an aqueous suspension after acidification to a pH of 3.0, to a pretreatment by heating it to 250C
(heating rate 10C/minute). This pretreatment was carried out in an autocla~e at a pressure higher than the water-vapour pressure at 250C and was continued during 30 minutes.
Thus, after separation of the liquid water, 520 g partly 15 coalified product ~re obtained, containing 120 g water, 390 g organic material and 10 g ash.
This product was subjected at a pressure of 50 bar to a fu~ther heating to 340C, in which heating was effected directly by superheated steam (heating rate ôC/minute, followed by cooling im~ediately after the temperature of 340C had been reached). Thus, 258 g water-free coal were obtained, containing 10 g ash and 56 g tar.
Without separation of the tar the product was pressed to briquettes with a diameter of 11.5 mm. The crushing strength of the briquettes formed was 29.9 ~ewton.
For comparison reasons the two-stage process was repeated using identical conditions with the exception of the pH which was kept 8 in this case. The crushing strength of the briquettes formed was now only 6.1 ~ewton.
By briquetting of the Australian brown coal itself (without applying a heat treatment at all) briquettes were ob-t&ined with a crushing strength of only 4.0 ~ewton. By briquetting of the first-stage product of the two-stage heat treatment the crushing strength of the briquettes formed was 6.o ~ewton and 7.5 ~ewton respectively when a pH = 8 and a pX = 3 was applied.
.
- .
: . .
- , ~ .. :
~ . .
: . ' '.' : '
Claims (10)
1. A process for the upgrading of low-grade solid fuel by heating at a temperature above 300°C
in the presence of water, characterized in that before or during the heating above 300°C acid is added to the fuel.
in the presence of water, characterized in that before or during the heating above 300°C acid is added to the fuel.
2. A process according to claim 1, characterized in that so much acid is added that the pH of the water present in the fuel becomes 6 or lower.
3. A process according to claim 1, characterized in that the heating is carried out at a pressure below 85 atm. and in that the acid is added before the heating.
4. A process according to claim 2, characterized in that the heating is carried out at a pressure below 85 atm. and in that the acid is added before the heating.
5. A process according to claim 1, characterized in that the acid is added before or during a pretreat-ment of the fuel at a temperature between 150 and 300°C
and a pressure which is higher than the water-vapour pressure at the temperature used and in that the pre-treated fuel is separated from expelled water before being heated above 300°C;
and a pressure which is higher than the water-vapour pressure at the temperature used and in that the pre-treated fuel is separated from expelled water before being heated above 300°C;
6. A process according to claim 2, 3 or 4, characterized in that the acid is added before or during a pretreatment of the fuel at a temperature between 150 and 300°C and a pressure which is higher than the water-vapour pressure at the temperature used and in that the pretreated fuel is separated from expelled water before being heated above 300°C.
7. A process according to claim 1, 2 or 3, characterized in that at least part of the tar formed is separated from the upgraded fuel.
8. A process according to claim 4 or 5, characterized in that at least part of the tar formed is separated from the upgraded fuel.
9. A process as claimed in claim 1, 2 or 3, characterized in that at least part of the tar formed is used for pelletizing or briquetting of the upgraded solid fuel.
10. A process as claimed in claim 4 or 5, characterized in that at least part of the tar formed is used for pelletizing or briquetting of the upgraded solid fuel.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| NL7907116 | 1979-09-25 | ||
| NL7907116 | 1979-09-25 |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CA1150172A true CA1150172A (en) | 1983-07-19 |
Family
ID=19833905
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA000359082A Expired CA1150172A (en) | 1979-09-25 | 1980-08-27 | Process for the upgrading of low-grade solid fuel |
Country Status (20)
| Country | Link |
|---|---|
| EP (1) | EP0026011B1 (en) |
| AR (1) | AR223729A1 (en) |
| AT (1) | ATE4462T1 (en) |
| AU (1) | AU534926B2 (en) |
| BR (1) | BR8006056A (en) |
| CA (1) | CA1150172A (en) |
| CS (1) | CS222691B2 (en) |
| DE (1) | DE3064580D1 (en) |
| DK (1) | DK400980A (en) |
| ES (1) | ES8106547A1 (en) |
| FI (1) | FI802993A (en) |
| GR (1) | GR70066B (en) |
| HU (1) | HU186751B (en) |
| IE (1) | IE50128B1 (en) |
| NZ (1) | NZ195028A (en) |
| PL (1) | PL125118B1 (en) |
| RO (1) | RO78331A (en) |
| SU (1) | SU1056908A3 (en) |
| TR (1) | TR21076A (en) |
| YU (1) | YU40885B (en) |
Families Citing this family (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| AU5088885A (en) * | 1985-11-29 | 1987-06-04 | Gippsland Institute of Advanced Education, The | The production of hard compact carbonaceous material through water/acid/alkali treatment |
| JP6219185B2 (en) * | 2014-01-30 | 2017-10-25 | 株式会社神戸製鋼所 | Method for producing modified coal and modified coal |
Family Cites Families (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE508392C (en) * | 1930-09-26 | I G Farbenindustrie Akt Ges | Process for dewatering peat | |
| GB191305873A (en) * | 1913-03-10 | 1914-06-10 | Wetcarbonizing Ltd | Improvements in and relating to the Utilisation of Peat. |
| FR644440A (en) * | 1927-02-08 | 1928-10-08 | Process for the treatment of peat | |
| DE899493C (en) * | 1950-08-14 | 1953-12-14 | Josef Schmitz Dipl Chem | Method of treating peat |
| US3660054A (en) * | 1970-09-29 | 1972-05-02 | Atlantic Richfield Co | Coal upgrading |
-
1980
- 1980-08-27 EP EP80200805A patent/EP0026011B1/en not_active Expired
- 1980-08-27 DE DE8080200805T patent/DE3064580D1/en not_active Expired
- 1980-08-27 CA CA000359082A patent/CA1150172A/en not_active Expired
- 1980-08-27 AT AT80200805T patent/ATE4462T1/en not_active IP Right Cessation
- 1980-09-23 BR BR8006056A patent/BR8006056A/en unknown
- 1980-09-23 FI FI802993A patent/FI802993A/en not_active Application Discontinuation
- 1980-09-23 HU HU802320A patent/HU186751B/en unknown
- 1980-09-23 IE IE1976/80A patent/IE50128B1/en unknown
- 1980-09-23 YU YU2418/80A patent/YU40885B/en unknown
- 1980-09-23 ES ES495250A patent/ES8106547A1/en not_active Expired
- 1980-09-23 NZ NZ195028A patent/NZ195028A/en unknown
- 1980-09-23 GR GR62940A patent/GR70066B/el unknown
- 1980-09-23 CS CS806421A patent/CS222691B2/en unknown
- 1980-09-23 DK DK400980A patent/DK400980A/en not_active Application Discontinuation
- 1980-09-23 SU SU802984502A patent/SU1056908A3/en active
- 1980-09-23 PL PL1980226878A patent/PL125118B1/en unknown
- 1980-09-23 TR TR21076A patent/TR21076A/en unknown
- 1980-09-23 AR AR282620A patent/AR223729A1/en active
- 1980-09-23 AU AU62624/80A patent/AU534926B2/en not_active Ceased
- 1980-09-24 RO RO80102210A patent/RO78331A/en unknown
Also Published As
| Publication number | Publication date |
|---|---|
| ATE4462T1 (en) | 1983-09-15 |
| DK400980A (en) | 1981-03-26 |
| GR70066B (en) | 1982-07-26 |
| SU1056908A3 (en) | 1983-11-23 |
| FI802993A (en) | 1981-03-26 |
| RO78331A (en) | 1982-04-12 |
| PL226878A1 (en) | 1981-05-22 |
| YU241880A (en) | 1983-02-28 |
| ES495250A0 (en) | 1981-06-16 |
| IE801976L (en) | 1981-03-25 |
| AR223729A1 (en) | 1981-09-15 |
| CS222691B2 (en) | 1983-07-29 |
| TR21076A (en) | 1983-06-23 |
| HU186751B (en) | 1985-09-30 |
| PL125118B1 (en) | 1983-03-31 |
| YU40885B (en) | 1986-08-31 |
| IE50128B1 (en) | 1986-02-19 |
| NZ195028A (en) | 1982-08-17 |
| AU6262480A (en) | 1981-04-09 |
| DE3064580D1 (en) | 1983-09-22 |
| BR8006056A (en) | 1981-04-07 |
| EP0026011B1 (en) | 1983-08-17 |
| ES8106547A1 (en) | 1981-06-16 |
| AU534926B2 (en) | 1984-02-23 |
| EP0026011A1 (en) | 1981-04-01 |
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