CA1139532A - Process for the agglomeration of solids - Google Patents
Process for the agglomeration of solidsInfo
- Publication number
- CA1139532A CA1139532A CA000331049A CA331049A CA1139532A CA 1139532 A CA1139532 A CA 1139532A CA 000331049 A CA000331049 A CA 000331049A CA 331049 A CA331049 A CA 331049A CA 1139532 A CA1139532 A CA 1139532A
- Authority
- CA
- Canada
- Prior art keywords
- zone
- binder
- agglomerates
- hydrocarbon binder
- agglomeration
- 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
- 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
- C10L5/00—Solid fuels
- C10L5/02—Solid fuels such as briquettes consisting mainly of carbonaceous materials of mineral or non-mineral origin
- C10L5/06—Methods of shaping, e.g. pelletizing or briquetting
-
- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B1/00—Preliminary treatment of ores or scrap
- C22B1/14—Agglomerating; Briquetting; Binding; Granulating
- C22B1/24—Binding; Briquetting ; Granulating
- C22B1/242—Binding; Briquetting ; Granulating with binders
- C22B1/244—Binding; Briquetting ; Granulating with binders organic
Landscapes
- Chemical & Material Sciences (AREA)
- Life Sciences & Earth Sciences (AREA)
- Environmental & Geological Engineering (AREA)
- General Life Sciences & Earth Sciences (AREA)
- Geochemistry & Mineralogy (AREA)
- Geology (AREA)
- Engineering & Computer Science (AREA)
- Organic Chemistry (AREA)
- Materials Engineering (AREA)
- Mechanical Engineering (AREA)
- Metallurgy (AREA)
- Manufacturing & Machinery (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Solid Fuels And Fuel-Associated Substances (AREA)
- Glanulating (AREA)
- Separation Of Suspended Particles By Flocculating Agents (AREA)
Abstract
ABSTRACT
Process for the agglomeration of solids.
A two-stage agglomeration process for coal fines in the form of a pumpable slurry. The slurry is selectively agglomerated in the first stage by the addition of a hydrocarbon binder and the bulk of the water separated from the resulting agglomerates.
Improved agglomerates are obtained in the second stage where those from the first stage are resubmitted to turbulent motion in hot water, which is drained from the agglomerates and recirculated thus reducing energy requirements.
Process for the agglomeration of solids.
A two-stage agglomeration process for coal fines in the form of a pumpable slurry. The slurry is selectively agglomerated in the first stage by the addition of a hydrocarbon binder and the bulk of the water separated from the resulting agglomerates.
Improved agglomerates are obtained in the second stage where those from the first stage are resubmitted to turbulent motion in hot water, which is drained from the agglomerates and recirculated thus reducing energy requirements.
Description
P.t PROCESS FOR THE AGGLOME~ATION OF SOLIDS
This invention relates to a process for the agglo-meration of finely divided solids, and in particular those in the form of an aqueous suspension.
In general, agglomeration is carried out by subjecting finely divided solids to turbulence in the presence of a binder which is capable of wetting the surface of the solids. Selective aggloMeration takes place when the binder alone, or possibly in the presence of another agent, wets the surface of the solids preferentially over that of any contaminating material present.
Agglomeration is used for upgrading finely divided solids such as ores, and in particu]ar coal, and also to facilitate dewatering. Selective agglomeration is useful for the enrichment of ores and for separating coal from gangue.
Hydrocarbon binders, such as bitumen, coal tar, short residues and the like, tend to produce good agglomerates. In choosing a binder for selective agglomeration much more care has to be taken. In general the most selective binders tend to be the lighter hydrocarbons, but these do not always produce the best agglomerates.
The present invention not only seeks to provide harder agglomerates, but also to reduce the energy input necessary for their production.
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In accordance with the invention a process for the agglomeration of finely divided solids in an aqueous suspension comprises passing the suspension through a first zone where it is subjected to turbulence in the presence of a hydrocarbon binder which causes agglomerates to be formed, separating the latter from water and any unagglomerated material, passing the agglomerates to a second zone containing water at a temperature of at least 60C., where they are subjected to turbulence in the presence of a hydrocarbon binder (which need not be the same as the one employed in the first zone), and separating the resulting agglomerates from the heated liquid and recirculating the latter to the second zone.
In practice, the binder is chosen so that it does not have a viscosity in excess of 4000 mm /s at the agglomeration temperature. Where this is not possible, the binder may be emulsified as an unstable emulsion by mixing it vigorously with water at elevated temperature according to known techniques. Stabilized emulsions may also be used as mentioned below.
The process has the advantage that due to the elevated temperature in the second zone pellets are formed which are hard at ambient temperature, which can be much more easily handled, and thus have a higher market value.
~ he temperature of the water will advantageously be between 60C and 85C so that the vessel does not have to be pressurized, but should it be desirable, due to, for example, the type o~ bitumen to be used, to operate at a higher temperature, then it is of course possible to pressurize the vessel so that the water remains in the liquid phase.
By using a separate charge of water in the second zone, and by recirculating it a large proportlon of its heat energy is conserved. Furthermore, a very considerable saving is achieved by not having to heat up the whole of the water phase in which the solids are suspended on entry into the first zone.
It also permits the optional use of a relatively more volatile binder in the first zone, which can improve the selectivity of the agglomeration process.
Such a more volatile binder can be partially or wholly recovered in the second zone where it tends to be evaporated off due to the higher temperature obtaining ,: ~
there.
The binder may be a bitumen, coal tar or short residueJ whose so~tening point (R&B) is between 30C
and~120C, but as softer binders (those having a softening~ point between 30c and 60C) are more effective for selective agglomeration, these tend to be preferred if a single binder is to be used.
Normally, 6 to 12 %w binder (based on the solids :
material to be separated) will be sufficient.
If the binder is introduced without taking any ~ .
. . .
.
` ~ -.
~o~
precautions it may not be evenly distributed over the whole of the volume of the zone in which lt is introduced or the distribution may be too slow. It is therefore advantageous to do so in the form of an emulsion which dilutes itself rapidly in the obtaining turbulent conditions. Where an emulsifying agent is present it can promote more rapid agglome-ration of the solids, perhaps due to the emulsifying agent improving the wetting properties of the binder on the solids or the compaction of the particles.
Often emulsifiers used for bitumsn emu]sions comprise essentially alkaline soaps of higher fatty acids but these may only be moderately .suitable for this purpose. Better results can sometimes be obtained with a special emulsion prepared with approximately 3%
by weight (based on the proportion of bitumen) of alkaline naphthenate. ~here more rapid agglomeration takes place this evidently can result in : ~ :
additional energy and cost savings.
Where some of the binder is to be added only in the second zone, it may be introduoed in powdered form such as powdered bitumen whose softening point (R&B) is below the temperature obtaining in the second zone.
The invention is particularly suitable for :
upgrading and dewatering coal slurries either after pipeline transport or of normal run-of-mine fines. In , ~ ~
: ~ :
~ ~ .
~ : "
-.
:
such slurries the fines usual]y have a maximum dimension of up to, say, 1 to 2 mm and as such are difficult to handle; they must also remain relat;vely wet to prevent dusting. ~fter treatment in accordance with the invention they are in the form of relatively hard pellets having a diameter of tlp to 20 mm - the larger the pellets desired, the longer they must be submitted to the turbulence, and thus the more expensive they are. The pellets will also have a reduced ~ater content which is acceptable to customers wishing to use them in conventional coal-burning applications.
In addition, where the solids enter the agglomeration process with contaminating matter, the resulting pellets will normally contain a signifi-cantly lower proportion of the contaminating material due to the selectivity of the first agglomeration step. If still more selectivity is required, an intermediate grinding step may be introduced after the first zone, in which the loose agglomerates are regroùnd. They are then passed to an intermediate , zone or even the above-mentioned second zone for more selective reagglomeration to remove a proportion of the impurities.
The invention will be further described by way of example with reference to the accompanying drawing, which is a flow scheme of an agglomeration ;
: ::
~ ~ ' ; . :
', ' :
process in accordance with the invention for a coal slurry comprising an aqueous suspension of coal fines and some gangue.
The slurry with a proportioned h~drocarbon binder enters a first zone or vessel lO by lines 12 and 13 and is subjected to turbulence by means of a stirrer 14 driven by a motor 16. Loose agglomerates so formed, together with some unagglomerated material and a corresponding quantity of water, leave the ~irst vessel by a line 18 and are separated by means of a moving screen 20. The water and unagglo~erated matter are removed through a line 21 and may be recirculated to the first vessel 10 after settling and decanting the excess water and gangue (this step is not shown the flow scheme).
The loose agglomerates are then passed via a line 24 to a second æone or vessel 22 containing hot water. The agglomerates are again stirred vigorously by means of a stirrer 26 driven by a motor 27. After remaining in the second vessel for the desired residence time, the enlarged and hardened agglome-rates in pellet form leave the vessel by line 2~ with a corresponding quantity of water and are passed over a screen 30. Dewatered agglomerates can then be stored in heaps, blns or hoppers.
The hot water drained from the agglomerates is passed via a line 31 to a reservoir 32 whence it is - ~ , ~ ~ ~æ
recirculated by a pump 3L~ via a heat exchanKer 36 in which it is reheated to the desired operating temperature of the second vessel 22.
; Ash is removed from the reservoir 32 by a line 40 and may conveniently by recirculated to the first vessel.
Unagglomerated particles are recirculated to the second vessel with the water.
In a typical case a dilute coa] slurry containing 9 m3 of water to 3 tonnes of hard coa]
fines having a maximum dimension of 1 mm and an ash content of 17% is introduced into a first vessel 10 together with 20~ by weight (based on the coal) of an unstabilized 50% emulsion of bitumen having a penetration 50-60 pen at 25C (softening point approx. 50C). After a mean residence time of 15 minutes the corresponding quantity o~ loose agglo-merates and water and ash are passed over the screen 20. An amount of 8.3 tonnes of water are drained together with the unagglomerated ash. The remaining 3 tonnes of coal agglomerates (now with 8.2% of ash) and 1 tonne of water enter the second vessel 22 and are mixed with 8 tonnes of water at 95C to produce a mixture at 80C. After a residence time of 20 minutes the resulting pellets of 5 to 20 mm diameter are separated from the hot water on the screen 30. They had an average water content of approximately 10% and the ash content had f`allen to 7%.
::
, , , 95~
A more effective de-ashing method could have been carried out by introducing a srnall quantity of a light hydrocarbon binder such as butane into the first vessel 10, which would necessitate sealing off from the atmosphere the solids between the first and second vessels. Any light hydrocarbon binder remaining in the agglomerates is flashed off due to the higher temperature obtaining in the second vessel and can be recovered. It can be replaced by adding a corresponding quantity of powdered bitumen in the second vessel.
Improved de-ashing of the coal can also be obtained by regrinding the coal between the first and second vessels.
:~: :
::, :: : :
::
,~
- .
.
~: .
.
This invention relates to a process for the agglo-meration of finely divided solids, and in particular those in the form of an aqueous suspension.
In general, agglomeration is carried out by subjecting finely divided solids to turbulence in the presence of a binder which is capable of wetting the surface of the solids. Selective aggloMeration takes place when the binder alone, or possibly in the presence of another agent, wets the surface of the solids preferentially over that of any contaminating material present.
Agglomeration is used for upgrading finely divided solids such as ores, and in particu]ar coal, and also to facilitate dewatering. Selective agglomeration is useful for the enrichment of ores and for separating coal from gangue.
Hydrocarbon binders, such as bitumen, coal tar, short residues and the like, tend to produce good agglomerates. In choosing a binder for selective agglomeration much more care has to be taken. In general the most selective binders tend to be the lighter hydrocarbons, but these do not always produce the best agglomerates.
The present invention not only seeks to provide harder agglomerates, but also to reduce the energy input necessary for their production.
~ . .
~,.,~
: ~t .
3~3L3~$~
In accordance with the invention a process for the agglomeration of finely divided solids in an aqueous suspension comprises passing the suspension through a first zone where it is subjected to turbulence in the presence of a hydrocarbon binder which causes agglomerates to be formed, separating the latter from water and any unagglomerated material, passing the agglomerates to a second zone containing water at a temperature of at least 60C., where they are subjected to turbulence in the presence of a hydrocarbon binder (which need not be the same as the one employed in the first zone), and separating the resulting agglomerates from the heated liquid and recirculating the latter to the second zone.
In practice, the binder is chosen so that it does not have a viscosity in excess of 4000 mm /s at the agglomeration temperature. Where this is not possible, the binder may be emulsified as an unstable emulsion by mixing it vigorously with water at elevated temperature according to known techniques. Stabilized emulsions may also be used as mentioned below.
The process has the advantage that due to the elevated temperature in the second zone pellets are formed which are hard at ambient temperature, which can be much more easily handled, and thus have a higher market value.
~ he temperature of the water will advantageously be between 60C and 85C so that the vessel does not have to be pressurized, but should it be desirable, due to, for example, the type o~ bitumen to be used, to operate at a higher temperature, then it is of course possible to pressurize the vessel so that the water remains in the liquid phase.
By using a separate charge of water in the second zone, and by recirculating it a large proportlon of its heat energy is conserved. Furthermore, a very considerable saving is achieved by not having to heat up the whole of the water phase in which the solids are suspended on entry into the first zone.
It also permits the optional use of a relatively more volatile binder in the first zone, which can improve the selectivity of the agglomeration process.
Such a more volatile binder can be partially or wholly recovered in the second zone where it tends to be evaporated off due to the higher temperature obtaining ,: ~
there.
The binder may be a bitumen, coal tar or short residueJ whose so~tening point (R&B) is between 30C
and~120C, but as softer binders (those having a softening~ point between 30c and 60C) are more effective for selective agglomeration, these tend to be preferred if a single binder is to be used.
Normally, 6 to 12 %w binder (based on the solids :
material to be separated) will be sufficient.
If the binder is introduced without taking any ~ .
. . .
.
` ~ -.
~o~
precautions it may not be evenly distributed over the whole of the volume of the zone in which lt is introduced or the distribution may be too slow. It is therefore advantageous to do so in the form of an emulsion which dilutes itself rapidly in the obtaining turbulent conditions. Where an emulsifying agent is present it can promote more rapid agglome-ration of the solids, perhaps due to the emulsifying agent improving the wetting properties of the binder on the solids or the compaction of the particles.
Often emulsifiers used for bitumsn emu]sions comprise essentially alkaline soaps of higher fatty acids but these may only be moderately .suitable for this purpose. Better results can sometimes be obtained with a special emulsion prepared with approximately 3%
by weight (based on the proportion of bitumen) of alkaline naphthenate. ~here more rapid agglomeration takes place this evidently can result in : ~ :
additional energy and cost savings.
Where some of the binder is to be added only in the second zone, it may be introduoed in powdered form such as powdered bitumen whose softening point (R&B) is below the temperature obtaining in the second zone.
The invention is particularly suitable for :
upgrading and dewatering coal slurries either after pipeline transport or of normal run-of-mine fines. In , ~ ~
: ~ :
~ ~ .
~ : "
-.
:
such slurries the fines usual]y have a maximum dimension of up to, say, 1 to 2 mm and as such are difficult to handle; they must also remain relat;vely wet to prevent dusting. ~fter treatment in accordance with the invention they are in the form of relatively hard pellets having a diameter of tlp to 20 mm - the larger the pellets desired, the longer they must be submitted to the turbulence, and thus the more expensive they are. The pellets will also have a reduced ~ater content which is acceptable to customers wishing to use them in conventional coal-burning applications.
In addition, where the solids enter the agglomeration process with contaminating matter, the resulting pellets will normally contain a signifi-cantly lower proportion of the contaminating material due to the selectivity of the first agglomeration step. If still more selectivity is required, an intermediate grinding step may be introduced after the first zone, in which the loose agglomerates are regroùnd. They are then passed to an intermediate , zone or even the above-mentioned second zone for more selective reagglomeration to remove a proportion of the impurities.
The invention will be further described by way of example with reference to the accompanying drawing, which is a flow scheme of an agglomeration ;
: ::
~ ~ ' ; . :
', ' :
process in accordance with the invention for a coal slurry comprising an aqueous suspension of coal fines and some gangue.
The slurry with a proportioned h~drocarbon binder enters a first zone or vessel lO by lines 12 and 13 and is subjected to turbulence by means of a stirrer 14 driven by a motor 16. Loose agglomerates so formed, together with some unagglomerated material and a corresponding quantity of water, leave the ~irst vessel by a line 18 and are separated by means of a moving screen 20. The water and unagglo~erated matter are removed through a line 21 and may be recirculated to the first vessel 10 after settling and decanting the excess water and gangue (this step is not shown the flow scheme).
The loose agglomerates are then passed via a line 24 to a second æone or vessel 22 containing hot water. The agglomerates are again stirred vigorously by means of a stirrer 26 driven by a motor 27. After remaining in the second vessel for the desired residence time, the enlarged and hardened agglome-rates in pellet form leave the vessel by line 2~ with a corresponding quantity of water and are passed over a screen 30. Dewatered agglomerates can then be stored in heaps, blns or hoppers.
The hot water drained from the agglomerates is passed via a line 31 to a reservoir 32 whence it is - ~ , ~ ~ ~æ
recirculated by a pump 3L~ via a heat exchanKer 36 in which it is reheated to the desired operating temperature of the second vessel 22.
; Ash is removed from the reservoir 32 by a line 40 and may conveniently by recirculated to the first vessel.
Unagglomerated particles are recirculated to the second vessel with the water.
In a typical case a dilute coa] slurry containing 9 m3 of water to 3 tonnes of hard coa]
fines having a maximum dimension of 1 mm and an ash content of 17% is introduced into a first vessel 10 together with 20~ by weight (based on the coal) of an unstabilized 50% emulsion of bitumen having a penetration 50-60 pen at 25C (softening point approx. 50C). After a mean residence time of 15 minutes the corresponding quantity o~ loose agglo-merates and water and ash are passed over the screen 20. An amount of 8.3 tonnes of water are drained together with the unagglomerated ash. The remaining 3 tonnes of coal agglomerates (now with 8.2% of ash) and 1 tonne of water enter the second vessel 22 and are mixed with 8 tonnes of water at 95C to produce a mixture at 80C. After a residence time of 20 minutes the resulting pellets of 5 to 20 mm diameter are separated from the hot water on the screen 30. They had an average water content of approximately 10% and the ash content had f`allen to 7%.
::
, , , 95~
A more effective de-ashing method could have been carried out by introducing a srnall quantity of a light hydrocarbon binder such as butane into the first vessel 10, which would necessitate sealing off from the atmosphere the solids between the first and second vessels. Any light hydrocarbon binder remaining in the agglomerates is flashed off due to the higher temperature obtaining in the second vessel and can be recovered. It can be replaced by adding a corresponding quantity of powdered bitumen in the second vessel.
Improved de-ashing of the coal can also be obtained by regrinding the coal between the first and second vessels.
:~: :
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::
,~
- .
.
~: .
.
Claims (12)
1. A process for the agglomeration of finely divided solids in an aqueous suspension, which process comprises the following steps:-a) passing the suspension through a first zone where it is subjected to turbulence in the presence of a hydrocarbon binder which causes loose agglomerates to be formed;
b) separating the agglomerates formed in step (a) from the water and any unagglomerated material;
c) passing the agglomerates to a second zone containing water having a temperature of at least 60°C, where they are subjected to turbulence in the presence of a hydrocarbon binder; and d) separating the resulting agglomerates from the heated liquid and recirculating the latter to the second zone.
b) separating the agglomerates formed in step (a) from the water and any unagglomerated material;
c) passing the agglomerates to a second zone containing water having a temperature of at least 60°C, where they are subjected to turbulence in the presence of a hydrocarbon binder; and d) separating the resulting agglomerates from the heated liquid and recirculating the latter to the second zone.
2. A process as claimed in claim 1, in which the binder preferentially wets the solids over any contaminating material which is present in the suspension.
3. A process as claimed in claim 1, in which the hydrocarbon binder has a softening point between 30°C and 120°C as measured by the Ring and Ball method according to ASTM-D-36-647.
4. A process as claimed in claim 3, in which the hydrocarbon binder has a softening point between 30°C and 60°C as measured by the Ring and Ball method according to ASTM-D-36-647.
5. A process as claimed in claim 3, in which the hydrocarbon binder is introduced into the first zone in the form of an emulsion.
6. A process as claimed in any one of claims 1, 2 or 3, in which the temperature of the heated liquid in the second zone is maintained between 60°C and 85°C.
7. A process as claimed in any one of claims 1, 2 or 3, in which between 6 and 12 per cent by weight (based on the weight of solids to be separated) of the hydrocarbon binder is added.
8. A process as claimed in any one of claims 1, 2 or 3, in which a light hydrocarbon binder is introduced in the first zone in order to improve the selectivity of the agglomeration of the solids over any contaminating material and that said binder is at least party removed from the agglomerates in the second zone due to the higher temperature in that zone.
9. A process as claimed in any one of claims 1, 2 or 3, in which a quantity of powdered bitumen is added in the second zone as a binder.
10. A process as claimed in claim 1, 2 or 3, in which the hydrocarbon binder used in the first zone is the same as the hydrocarbon binder used in the second zone.
11. A process as claimed in claim 1, 2 or 3, in which the hydrocarbon binder used in the first and second zones are different.
12. A process as claimed in claim 1, 2 or 3, wherein the hydrocarbon binder in the first zone has a viscosity not in excess of 4000mm2/s at the agglomeration temperature.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| NL7807223 | 1978-07-04 | ||
| NL7807223A NL7807223A (en) | 1978-07-04 | 1978-07-04 | METHOD FOR AGGLOMERATING SOLIDS |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CA1139532A true CA1139532A (en) | 1983-01-18 |
Family
ID=19831187
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA000331049A Expired CA1139532A (en) | 1978-07-04 | 1979-07-03 | Process for the agglomeration of solids |
Country Status (10)
| Country | Link |
|---|---|
| JP (1) | JPS558897A (en) |
| AU (1) | AU4858279A (en) |
| BE (1) | BE877264A (en) |
| CA (1) | CA1139532A (en) |
| DE (1) | DE2926696A1 (en) |
| FR (1) | FR2430256A1 (en) |
| GB (1) | GB2024251B (en) |
| NL (1) | NL7807223A (en) |
| SE (1) | SE7905779L (en) |
| ZA (1) | ZA793269B (en) |
Families Citing this family (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| AT376147B (en) * | 1980-12-15 | 1984-10-10 | Gergely Gerhard | METHOD AND DEVICE FOR GRANULATING A POWDER MIXTURE |
| ZA834208B (en) * | 1982-06-22 | 1985-01-30 | British Petroleum Co Plc | Process for the production of agglomerated fuels |
| US4966608A (en) * | 1988-08-09 | 1990-10-30 | Electric Power Research Institute, Inc. | Process for removing pyritic sulfur from bituminous coals |
| JP2731484B2 (en) * | 1992-03-13 | 1998-03-25 | 出光興産株式会社 | Granulation method of coal powder |
| ES2338733B1 (en) * | 2008-01-18 | 2011-02-10 | Hera-Amasa, S.A. | PERFECTED PROCEDURE FOR RECYCLING OF ACERGE DUST. |
Family Cites Families (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| FR588120A (en) * | 1924-02-09 | 1925-04-30 | Process for the manufacture of a fuel and product obtained by this process | |
| FR682967A (en) * | 1928-10-20 | 1930-06-04 | Trent Process Corp | Process for preparing an amalgam of oil and coal |
| NL245113A (en) * | 1959-11-06 | 1964-02-10 | Shell Internationale Research Maatschappij N.V. | METHOD AND EQUIPMENT FOR THE PREPARATION OF SOLID SOOTAGE AGGREGATES FROM A WATERY SOIL SUSPENSION |
| US3856668A (en) * | 1973-05-30 | 1974-12-24 | R Shubert | Method for treatment of coal washery waters |
| NL7513673A (en) * | 1975-11-24 | 1977-05-26 | Shell Int Research | PROCEDURE FOR THE BENEFICATION OF SOLID FUEL. |
| GB1575413A (en) * | 1976-12-03 | 1980-09-24 | Shell Int Research | Method for agglomeration of coal fines |
-
1978
- 1978-07-04 NL NL7807223A patent/NL7807223A/en not_active Application Discontinuation
-
1979
- 1979-06-26 BE BE1/9435A patent/BE877264A/en unknown
- 1979-06-29 FR FR7916928A patent/FR2430256A1/en not_active Withdrawn
- 1979-07-02 ZA ZA793269A patent/ZA793269B/en unknown
- 1979-07-02 AU AU48582/79A patent/AU4858279A/en not_active Abandoned
- 1979-07-02 JP JP8276279A patent/JPS558897A/en active Pending
- 1979-07-02 SE SE7905779A patent/SE7905779L/en unknown
- 1979-07-02 GB GB7922992A patent/GB2024251B/en not_active Expired
- 1979-07-02 DE DE19792926696 patent/DE2926696A1/en not_active Withdrawn
- 1979-07-03 CA CA000331049A patent/CA1139532A/en not_active Expired
Also Published As
| Publication number | Publication date |
|---|---|
| BE877264A (en) | 1979-12-27 |
| DE2926696A1 (en) | 1980-01-17 |
| JPS558897A (en) | 1980-01-22 |
| NL7807223A (en) | 1980-01-08 |
| SE7905779L (en) | 1980-01-05 |
| ZA793269B (en) | 1980-07-30 |
| GB2024251A (en) | 1980-01-09 |
| GB2024251B (en) | 1982-07-21 |
| AU4858279A (en) | 1980-01-10 |
| FR2430256A1 (en) | 1980-02-01 |
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