AU592472B2 - Creación de Inventos y Patentes con Inteligencia Artificial

AU592472B2 – Process for producing coal fillers
– Google Patents

AU592472B2 – Process for producing coal fillers
– Google Patents
Process for producing coal fillers

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Publication number
AU592472B2

AU592472B2
AU79651/87A
AU7965187A
AU592472B2
AU 592472 B2
AU592472 B2
AU 592472B2
AU 79651/87 A
AU79651/87 A
AU 79651/87A
AU 7965187 A
AU7965187 A
AU 7965187A
AU 592472 B2
AU592472 B2
AU 592472B2
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AU
Australia
Prior art keywords
slurry
oil
solids
coal
weight
Prior art date
1986-09-18
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.)

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Application number
AU79651/87A
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AU7965187A
(en

Inventor
Masayuki Nakai
Katsumi Tomura
Kenji Uesugi
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Idemitsu Kosan Co Ltd

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Idemitsu Kosan Co Ltd
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1986-09-18
Filing date
1987-09-17
Publication date
1990-01-11

1987-09-17
Application filed by Idemitsu Kosan Co Ltd
filed
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Idemitsu Kosan Co Ltd

1988-04-07
Publication of AU7965187A
publication
Critical
patent/AU7965187A/en

1990-01-11
Application granted
granted
Critical

1990-01-11
Publication of AU592472B2
publication
Critical
patent/AU592472B2/en

2007-09-17
Anticipated expiration
legal-status
Critical

Status
Ceased
legal-status
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Classifications

C—CHEMISTRY; METALLURGY

C09—DYES; PAINTS; POLISHES; NATURAL RESINS; ADHESIVES; COMPOSITIONS NOT OTHERWISE PROVIDED FOR; APPLICATIONS OF MATERIALS NOT OTHERWISE PROVIDED FOR

C09C—TREATMENT OF INORGANIC MATERIALS, OTHER THAN FIBROUS FILLERS, TO ENHANCE THEIR PIGMENTING OR FILLING PROPERTIES ; PREPARATION OF CARBON BLACK ; PREPARATION OF INORGANIC MATERIALS WHICH ARE NO SINGLE CHEMICAL COMPOUNDS AND WHICH ARE MAINLY USED AS PIGMENTS OR FILLERS

C09C1/00—Treatment of specific inorganic materials other than fibrous fillers; Preparation of carbon black

C09C1/44—Carbon

C09C1/48—Carbon black

C—CHEMISTRY; METALLURGY

C09—DYES; PAINTS; POLISHES; NATURAL RESINS; ADHESIVES; COMPOSITIONS NOT OTHERWISE PROVIDED FOR; APPLICATIONS OF MATERIALS NOT OTHERWISE PROVIDED FOR

C09C1/00—Treatment of specific inorganic materials other than fibrous fillers; Preparation of carbon black

C09C1/44—Carbon

C09C1/48—Carbon black

C09C1/56—Treatment of carbon black ; Purification

C09C1/58—Agglomerating, pelleting, or the like by wet methods

C—CHEMISTRY; METALLURGY

C09—DYES; PAINTS; POLISHES; NATURAL RESINS; ADHESIVES; COMPOSITIONS NOT OTHERWISE PROVIDED FOR; APPLICATIONS OF MATERIALS NOT OTHERWISE PROVIDED FOR

C09C1/00—Treatment of specific inorganic materials other than fibrous fillers; Preparation of carbon black

C09C1/44—Carbon

C—CHEMISTRY; METALLURGY

C01—INORGANIC CHEMISTRY

C01P—INDEXING SCHEME RELATING TO STRUCTURAL AND PHYSICAL ASPECTS OF SOLID INORGANIC COMPOUNDS

C01P2004/00—Particle morphology

C01P2004/60—Particles characterised by their size

C01P2004/61—Micrometer sized, i.e. from 1-100 micrometer

C—CHEMISTRY; METALLURGY

C01—INORGANIC CHEMISTRY

C01P—INDEXING SCHEME RELATING TO STRUCTURAL AND PHYSICAL ASPECTS OF SOLID INORGANIC COMPOUNDS

C01P2006/00—Physical properties of inorganic compounds

C01P2006/32—Thermal properties

C01P2006/37—Stability against thermal decomposition

Description

S5R9L2A472 ALIA COMMONWEALTH OF AU PATENT ACT 1952 COMPLETE SPECIFICATION
(ORIGINAL)
FOR OFFICE USE CLASS INT. CLASS_ Application Number: Lodged: Complete Specification Lodged: Accepted: Published: Priority: Related Art-: This document contains the amendments made uinder Section 49 and is correct for printing.j NAME OF APPLICANT: IDEMITSU KOSAN CO. LTD.
ADDRESS OF APPLICANT: 1-1, Marunouchi 3-chome, Chiyoda-Ku, Tokyo 100, Japan.
NAME(S) OF INVENTOR(S) Masayuki NAKAI Kenji UESUGI Katsuxni TOMURA ADDRESS FOR SERVICE: DAVIES COLLISON, Patent Attorneys 1 Little Collins Street, Melbourne, 3000.
A
COMPLETE SPECIFICATION FOR THE IVENTION ENTITLED: «PROCESS FOR PRODUCING ViLLtt Fll COAL HJR The following statement is a full description of this invention, ~0 inldn h etmto f efrigi nw ou _1
IA
1 PROCESS FOR PRODUCING COAL FILLERS TECHNICAL FIELD Field of the Invention The present invention relates to a novel process for producing coal fillers. More particularly, the present invention relates to an economical process for producing coal fillers that excel in reinforcing rubbers and plastics and can be suitably used in rubber industries, tire industries, plastic industries, etc.
BACKGROUND ART Carbon blacks has been widely used as reinforcing agents for tires or rubbers, black pigments for printing inks or paints, coloring materials for resins, mater als for dry batteries, conductive materials, etc. in various fields. Especially, those for reinforcing tires or rubbers preponderate in demands, and carbon blacks of various qualities are used as materials for the reinforcing agents.
Carbon blacks are uua!ly produced by incomplete combustion or thermal decomposition of hydrocarbonaceous Sgases or oils originated from petroleum or coal, such as natural gas, petroleum gas, crude naphthalene, creosote 1 oil, pitch oil, or the like. Known processes for the above-mentioned production are furnace method for producing furnace blacks, channel process for producing channel blacks, thermal process for producing thermal blacks, and the like.
However, these methods in which hydrocarbonaceous gases or hydrocarbonaceous oils are used as raw material have defects that the raw material situations are unstable and high cost is inevitable owing to the complicated producing processes.
On the other hand, in order to solve the defects, there was proposed a method of producing coal carbon blacks for rubber-reinforcing agents wherein a solid coal itself is thermally decomposed instead of creosote oil or crude naphthalene obtained by carbonization of coal (Japanese Patent Publication No. 16,107/1963). However, the carbon blacks for coal fillers obtained by the method have a disadvantage in their use as a reinforcing agent for rubbers since they have a large ash content which decreases 20 the modulus of rubbers and elongates vulcanization of rubbers.
The object of the present invention is to provide an economical process for producing coal fillersh*vairg excellent rubber-reinforcing properties.
:r 3 1 DISCLOSURE OF INVENTION As the result of our researches to attain the object, we found that the object can be easily attained by a novel method of producing coal fillers wherein a slurry of ultrafinely pulverized product obtained by subjecting a coal to specified treatment is treated by means of a specified deliming/agglomeration treatment, i.e. a specified oil-agglomeration technique suitable for agglomeration of ultrafine-particles, and we eventually came to complete the present invention.
According to the present invention, there is provided a process for producing coal fillers which comprises the steps of: carbonization step, which comprises carbonizing crushed coal particles having a particle size of not more than 10 mm and an ash content of not more than 10 by weight by thermal decomposition at a temperature of 500 to 2,000 C and cooling the carbonized solids; ultrafine pulverization step, which comprises preparing a slurry of the carbonized solids having a solids content of 10 to 50 by weight by adding a dispersion medium to the carbonized solids; and ultrafinely pulverizing the carbonized solids dispersed in the slurry to reduce the average particle size to not more than 5 u i i: 1 agglomeration step, which comprises adjusting the solids content of the slurry to 1 to 20 by weight by further adding water to the slurry of the ultrafinely pulverized solids; adding an oil having a boiling point of not more than 150 *C to the resulting slurry in a ratio of to 300 parts by weight of the oil per 100 parts by weight of dry solids; agitating the resulting mixture to agglomerate the carbonaceous matters with oil; and separating and recovering the agglomerates; and drying step, which comprises drying the recovered agglomerates by heating them at 50 to 300 *C to evaporate the water and oil retained in the agglomerates; and cooling the dried agglomerates.
The coals which may be used in the ste., to be ce r Vo. ve carbonized by thermal decompositionhave an ash content of not more than 10 by weight, preferably not more than 7 by weight, more preferably 3 by weight. The illustrative examples of coals to be used as the raw material include anthracite, bituminous coal, sub-bituminous coal, brown coal, lignite, peat eF-meA, and the like. The preferred are those having an ash content of not more than 10 by weight or those from which coals having an ash content of not more than 10 by weight can be easily separated by gravity separation or the like. Furthermore, from the
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1 viewpoint of facility of pulverization treatment following to the carbonization, non-caking coals or semi-caking coals are preferable, and non-caking coals are particularly preferable. These coals may either be used individually or in combination of two or more of them.
In the process according to the present invention, in order to reduce the ash content of the end products, it is desirable to use a coal having a lower ash content that is selected from the above described coals or, at need, separated from a coal by gravity separation or the like.
The separation of coals having an ash content of not more than 10 by weight can be carried out by separating coals having a low specific gravity of not higher than about 1.3, i.e. coals having a low ash content, by means of a gravity separation such as flotation, heavy fluid separation, etc.
In the process of the present invention, the above described coals are carbonized by thermal decomposition to remove volatile constituents including those originated by the decomposition, and the coals to be used are those previously crushed coarsely to a particle size of not more than 10 mm, in order to equalize the ‘jrAC7L effects of the carbonization. The preferable particle size cannot be uniformly limited since it varies depending upon 6 1 the type of the carbonization furnace, carbonization temperature, the content of volatile constituents or ash constituents in the coal, etc., and any size will do so long as the volatile constituents can be rapidly and uniformly removed. As the method of crushing, any conventional method can be employed.
Also, the crushing may be conducted before the gravity separation described above.
The carbonization of coals by thermal decomposition is conducted by heating the crushed coal particles, under the condition of no air additions, usually at 500 to 2,000 C preferably 550 to 1,800 °C more preferably at 600 to 1,500 C, usually for 2 to 3 hours.
Although the carbonization by thermal decomposition may be conducted in vacuum or In the atmosphere of an inert gas such as nitrogen, etc. or an inert industrial waste gas, a method in that the carbonization is conducted, under the condition that air is shut out, in a gas mixture of hydrogen, methane, carbon monoxide, carbon dioxide, etc.
which are generated from coal by thermal decomposition may be suitably employed.
The furnace to be used for the carbonization by thermal decomposition may be either of continuous system or batch system with the proviso that It is of closed system.
Although any conventional heating method such as electric I7 heating method, gas-combustion heating methods, and the like may be employed, the preferable heating method is a gas-combustion method because the combustible gases, i.e.
methane, other gaseous hydrocarbons, hydrogen, carbon monoxide, etc., which are recovered from the volatile components being generated in the carbonization process, can be advantageously used as fuels for heating the furnace.
If the temperature of carbonization is less than 500″C, residual volatile components may remain in the carbonized solids, and this may result in the obtained coal fillers not being suitable as reinforcing agents for rubbers. The residual volatile constituents may deteriorate rubber-reinforcing properties. Further, at 1 15 the time of vulcanization of rubbers, the residual ‘volatile constituents may hinder the vulcanization reaction and may be volatilized, causing an insufficient 0vulcanization of the rubbers. On the contrary, if the *o temperature is more than 2,000°C, graphitization of the 20 coals may occur, resulting in the production of undesirable coal fillers having poor rubber-reinforcing properties.
After the conclusion of the carbonization, the *s ‘resulting solids (hereinafter we will sometimes call them t S’ 25 char) are usually cooled as they are, i.e. under air exclusion conditions A A I1 A 891030.7
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8 1 In the step the solids (chars), which are the carbonized products obtained by the above described carbonization by thermal decomposition, are then ultrafinely pulverized usually to an average particle size of not more than 5 u m, preferably not more than 1 u m.
If the average particle size is more than 5 u m, the rubber-reinforcing properties (tensile strength, abrasion resistance, flexural strength, heat build-up, etc.) ape~decreased The illustrative examples of machines to be used for the ultrafine pulverization include ball mill and the like.
The ultrafine pulverization is conducted on the slurry of the chars dispersed in a dispersion medium. In order to increase the pulverizing efficiency, it is desirable to coarsely pulverize the chars, previously, to a particle size of about 200 meshAor below, at need. In addition to water, various kinds of dispersion medium may be used. The solids content of the slurry is 10 to 50 by weight. In order to increase the pulverization efficiency, it is desirable to increase the solids content of the slurry to about 30 to 50 by weight by adding a proper dispersing agent or the like. The pulverization efficiency can be further increased by adding a proper antifoaming agent to restrain the generation of air bubbles.
1 9 1 Any dispersion medium and antifoaming agent conventionally used for carbon-water slurries may be used.
Some illustrative examples of the dispersion medium include polystyrene sulfonic acid, polycarboxylic acid, lignosulfonic acid, etc. Some illustrative examples of the dispersing agents include methanol, ethanol, acetone, etc.
The slurries of the ultrafinely pulverized chars can be obtained by the above described methods. At need, the slurries of the ultrafinely pulverized chars may be subjected to separation/classification treatment to remove alien substances or coarse particles which will decrease the rubber-reinforcing properties.
That is, the coarse particles included in the ultrafinely pulverized particles or in the slurries thereof are classified and separated to be removed along with the alien substances. The coarse particles to be removed are usually those having a particle size of not less than 5 u m, preferably not less than 2 u m. If the particles having a. particle size of more than 5 1 m is remained, the rubberreinforcing properties of resulting coal fillers are decreased. The iron contents, which are contained in the starting coal or got mixed as a result of abrasion of apparatuses or grinding-media, can be efficiently removed S2./ by the use of a magnet. If the iron contents remains, they 1 sometimes pollute the surfaces of rolls or metal molds when the resulting coal fillers are kneaded with rubbers.
Usual methods, such as centrifugal separation method, wet-cyclone method, etc., may be employed for the separation/classification treatment.
When a wet separation/classification is I conducted, it is desirable to adjust the solids content of the slurries to 1 to 20 by weight, preferably about 5 to by weight, by dispersing the slurries in a dispersion medium such as water or by diluting them with a diluting agent, in order to increase the separation efficiency.
The separation/classification efficiency can be further increased by adding a dispersing agent, especially a dispersing agent that can homogeneously disperse particles having a particularly high cohesive strength, into the slurries. As such dispersing agents, the above described dispersing agents may be used.
In the step the slurry of the ultrafinely pulverized solids treated by the above described separation/classification is then subjected to deliming/agglomeration treatment. In this step, the ash constituents contained in the ultrafinely pulverized solids are separated and removed because the ash constituents decrease the rubber-reinforcing properties, and, at the same time, the ultrafinely pulverized solids are
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11 1 agglomerated to form agglomerates having a proper strength, so that they can tolerate the treatment to a product article and can easily and homogeneously disperse in rubbers when they are blended and kneaded with rubbers.
One of the most important characteristics of the process of the present invention is that an oilagglomeration method using an oil having a low boiling point is employed to carry out the deliming and agglomeration simultaneously.
The deliming and agglomeration by means of oilagglomeration is a method of agglomerating only carbonaceous matters to separate them from ash constituents, taking advantage of the antipodal properties thereof, i.e. the hydrophilic property of the ash constituents and the lipophilic property of the carbonaceous matters. In this method, the ash constituents are dispersed into water and only the carbonaceous matters are aggregated and agglomerated, by adding an oil having a Slow boiling point into the water slurry of the ultrafinely 1 20 pulverized solids and then agitating the mixture. The aggregated and agglomerated carbonaceous matters are then separated and recovered from the slurry by means of a screen, net, or the like to be fed to the next step. This S method permits the production of agglomerates free from binder oils or the like, because &he water and oil retained 1 12 1 in the agglomerates are removed by evaporation and, thus, the strength of the agglomerates is provided only by the adhesive force of the ultrafinely pulverized solids without the aid of a binder.
In the conventional oil-agglomeration methods for coal, a heavy oil or the like is used in order to increase the strength of agglomerates, and the residue of these oils in the agglomerates decreased the rubber-reinforcing properties. The oil-agglomeration method according to the present invention is free from such a problem.
The solids content of the ultrafinely pulverized solids-water slurry to be used in the oil-agglomeration of the present invention is 1 to 20 X by weight, preferably to 10 by weight.
Although the oil-agglomeration may be usually conducted at a temperature of 0 to 60 OC it can be suitably conducted at room temperature.
The treating time is usually about 1 to minutes and the preferred and enough time is about 5 to 20 minutes.
The oil to be added for the deliming and agglomeration by oil-agglomeration may be any one of paraffin oils, aromatic oils, and naphthene oils having not more than 8 carbon atoms and a boiling point of not more than 150 C The preferred are those able to be readily :i «1q i
I
10 r r, removed by evaporation In the following drying step, i.e.
those having a boiling point of not more than 120 C for example, low molecular weight hydrocarbon oils, such as, aromatic oils such as toluene, benzene, xylene, etc., and aliphatic oils ?uch as hexane, heptane, octane, etc. and freons such as trlchlorotrifluoroethane, etc.
These may be pure ones or mixtures thereof, or may be containing a small amount of water. Further, process oils or the like for rubbers may also be used in combination.
ItL It I
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I’ i
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-I t The ratio of the above described oils to the ultraflnely pulverized solids-water slurry, which cannot be uniformly limited since it varies depending upon the kind of the oil and the solids content of the slurry is 30 to 300 parts by weight, preferably 75 to 150 parts by weight, of the oils per 100 parts by Weight of dried ultraf’nely pulverized solids.
If the amount of the oils is less than 30 parts by weight, the aggregation and agglomeration may not occur and the ash constituents may not be removed. On the other hand, if it exceeds 300 parts by weight, the particle size of the agglomerates may be enlarged too much.
Thus, the ash content of the carbonaceous matters separated and recovered by deliming and agglomeration is typically reduced to not more than 5 by weight, preferably not more than 2 by weight.
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~a- *.o~e 0 0 00 OP I 0-10e 0 0 00 00 4 0 0000 0 004 00 0 00 0 *40 If the ash content is more than 5 by weight, when the coal fillers (end products) are used as a reinforcing agent for rubber, a decrease in durability of the rubber such as increased internal exothermic, abrasion, flex cracking, compression set, etc. and/or decreased mechanical properties, tensile strength and ultimate elongation.
Ash constituents, as described above, may severely deteriorate various properties, dynamic properties and static properties, and elongate the time of vulcanization, which is an important element in the productivity of vulcanized rubbers, thereby causing a decrease in operation efficiency.
The particle size of the agglomerates can be 15 controlled by controlling the amount of oil to be added, and, for the convenience of handling the end products, the secondary particle size (particle size of the agglomerates) is preferably about 0.5 to 3 mm.
The aggravation of work environments can be 20 prevented by employing the oil-agglomeration method for ultrafine particles because, in this method, the ultrafine particles, which scatter readily and are hard to handle, can be agglomerated in a state of slurry thereof.
The end products, which are produced by drying the agglomerates, will typically exhibit a sufficient particle strength for practical use even in the case where an oil having a low boiling point is used. Also, the particle strength of the end products may be further increased by conducting the oil-agglomeration using a dissolved mixture of a binder material and the above described oil and then drying to evaporate the oil alone.
Any usual compounding ingredient may be used as the binder, so long as it does not injure the rubberreinforcing properties. The preferred are higher fatty acids of 12 to 24 carbon atoms such as stearic acid, palmitic acid, myristic acid, arachic acid, etc.
i4 i; :ii j 0000 00 0 4 0 0 41 0044 0 0 0140 t I- I~iL-_ In order to further increase the rubberreinforcing properties by improving the conformability to rubbers of the coal fillers, an oil in which a surface modifier for ultraflnely pulverized particles is dissolved may be used for the oil-agglomeration. The surface modifier is uniformly coated on the surface of the coal fillers by drying the agglomerates to evaporate the oil alone.
Effective surface modifiers are process oils, activators, vulcanization accelerators, etc., which are a 0 S. kind of compounding ingredients for rubbers. Heretofore, surface modifiers have been added at the time of blending with rubbers. The complexity of the rubber blending step can be reduced by adding the surface modifiers at the time r 4 t f I I. S 16 16 4A 1 of production of fillers.
In the step the recovered agglomerates of the carbonaceous matters, i.e. wet coal fillers, are dried to evaporate water retained in the agglomerates, the oils having a low boiling point, etc., which are used in the above oil-agglomeration, and are cooled to obtain the objective end product, a coal filler.
The drying can be conducted by various usually drying methods. For example, it is conducted in an atmosphere of an inert gas such as gaseous nitrogen, at to 300 ‘C preferably 100 to 200 *C more preferably 110 to 150 C The drying and cooling may be conducted either in continuous system or batch system. Any conventional drier and cooler may be used. Preferred are those of rotary kiln system or fluidized bed system for the purpose of preventing the powdering of the agglomerates by cracking.
The process of the present inventionpermit, a sharp reduction in the quantity of heat necessary for the drying in comparison with a method where a slurry of ultrafinely pulverized solids is directly dried, because the drying in this process is conducted after the agglomeration and the separation of water.
yrr That is, thus recovered undry coal fillersAretain 0.3 to 1 kg of water and 0.3 to 2 kg of the oil per 1 kg of (mtyll 0 arra dry solids, and the energy required for drying them4″i only oe one third to one thirtieth of that required for directly drying the slurry, and thus a sharp reduction in energy and time for drying can be attained.
The following table shows agcomparison of energies required for the two types of drying method.
TABLE
Drying after oil-agglomeration Direct drying of 5 slurry 19 kg/kg-solids Water content per 1 kg of dry solids Toluene content per 1 kg of dry solids 0.5 kg/kg-solids 0.7 kg/kg-solids Energy required for evaporating water and toluene (150°C 428 kcal/kg-solids 12,460 kcal/kg-solids ti ~1 jl Amount of kerosene required for evaporation (converted from energy) (8,300 kcal/1) 0.051 1/kg-solids 1.50 1/kg-solids 18 1 The oils evaporated with a drying apparatus can be recycled after they are condensed by cooling and recovered by separating water.
The coal fillers thus produced due to their extremely excellent and well-balanced rubber-reinforcing properties and cheapness in price are useful as a rubberreinforcling agent in fields of rubber industries, tire industries, and the like. That is, the blending of the coal fillers prepared by the process of the present invention into rubbersei==tr e:n: effective in increasing various properties of the rubbers, such as heat build-up, flexural strength, abrasion resistance, tensile strength, tear strength, ultimate elongation, and the like, i= cn iderabMly incra. and in shortening the vulcanization time.
BEST MODE FOR CARRYING OUT THE INVENTION COMPARATIVE EXAMPLE 1 Cerrejon coal (sub-bituminous coal) was carbonized by heating at 750 0 C for 3 hours in a box furnace of batch system, and the obtained carbonized solids were then cooled to room temperature. To the resulting solids was added water to prepare a slurry having a solids content of 30 by weight. The slurry was agitated in a 19 1 ball mill of grinding-media system to ultrafinely pulverized the solids to submicron particle size.
The resulting slurry of ultrafinely pulverized solids was diluted with water to a solids content of 10 by weight. After iron contents were removed from the diluted slurry using a magnet, coarse particles were separated from the slurry by means of a wet cyclone.
The resulting slurry of ultrafine particles without coarse particles was heated at 120 °C for 24 hours to evaporate water, and the obtained dry product was subjected to Rubber Compounding Tests.
COMPARATIVE EXAMPLE 2 Cerrejon coal (sub-bituminous coal) was subjected to gravity separation using a heavy liquid having a specific gravity of 1.40 to separate and recover a coal having a specific gravity of not more than 1.40. The obtained coal was carbonized by heating at 750 «C for 3 hours in a box furnace of batch system, and the obtained 20 carbonized solids were cooled to room temperature. To the resulting solids was added water to prepare a slurry having a solids content of 30 by weight. The slurry was then agitated in a ball mill of grinding-media system to ultrafinely pulverize the solids to submicron particle size.
s: d i 1 I 2 1 The resulting slurry of ultrafinely pulverized particles was diluted with water to a solid content of 10 by weight. After iron contents were removed from the slurry using a magnet, coarse particles were separated by means of wet cyclone.
The resulting slurry of ultrafine particles without coarse particles was heated at 120 «C for, 24 hours to evaporate water, and the obtained dry product was subjected to Rubber Compounding Tests.
COMPARATIVE EXAMPLE 3 The procedure of Comparative Example 2 was repeated with the exception that a coal having a specific gravity of not more than 1.3 that was separated from Cerrejon coal by gravity separation using heavy liquid having a specific gravity of 1.30 was used.
EXAMPLE 1 Cerrejon coal (sub-bituminous coal) was subjected 20 to gravity separation using a heavy liquid having a specific gravity of 1.30 to separate and recover a coal having a specific gravity of not more than 1.30. The recovered coal was crushed to a particle size of not more than 10 mm, and the crushed coal was carbonized by heating at 750 °C for 3 hours in a box furnace of batch system.
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r a il m~ 21 1 The obtained carbonized solids were then cooled to room temperature. To the solids was then added water to prepare a slurry having a solids content of 30 by weight. The slurry was agitated in a ball mill of grinding-media system to ultrafinely pulverize the solids to submicron particle size.
To the slurry of ultrafinely pulverized particles was diluted with water to a solids content of 10 by weight. After iron contents were removed from the slurry using a magnet, coarse particles are separated by means of wet cyclone.
To the slurry of the ultrafine particles without coarse particles was added toluene (boiling point: 110.7 0
C
in a ratio of 1 ml of toluene per 1 g of solids. The mixture was then agitated to oil-agglomerate the ultrafine particles until the particle size is enlarged to about 1 mm. The ash constituents were then removed by recovering the agglomerated secondary particles using a screen.
The recovered agglomerates dried by heating at 120 °C for 24 hours to evaporate water and toluene, and the obtained dry product was subjected to Rubber Compounding Tests.
SEXAMPLE 2 o The procedure of Example 1 was repeated with the 22 1 exception that Cerrejon coal not subjected to gravity separation was used.
EXAMPLE 3 The procedure of Example 1 was repeated with the exception that a coal having a specific gravity of not more than 1.26 separated from Cerrejon coal by gravity separation using a heavy liquid having a specific gravity of 1.26 was used.
EXAMPLE 4 The procedure of Example 1 was repeated with the exception that a coal having a specific gravity of not more than 1.35 separated form Cerrejon coal by gravity separation using a heavy liquid having a specific gravity of 1.35.
COMPARATIVE EXAMPLE 4 Loy Yang coal (brown coal) was carbonized by heating at 650 C for 2 hours in a box furnace of batch system, and the carbonized solids were cooled to room temperature. To the resulting solids was added water to prepare a slurry having a solids content of 30 by weight.
The slurry was then agitated in a ball mill of grindingmedia system to ultrafinely pulverize the solids to 23 1 submicron particle size.
The slurry of the ultrafinely pulverized particles was diluted with water to a solids content of by weight. After iron contents were removed using a magnet, coarse particles were separated by means of wet cyclone.
The obtained slurry of ultrafine particles without coarse particles was driej by heating at 120 ‘C for 24 hours to evaporate water, and the obtained dry product was subjected to Rubber Compounding Tests.
EXAMPLE Loy Yang coal (brown coal) was crushed to a particle size of not more than 10 mm. The crushed coal was carbonized by heating at 650 0 C for 2 hours in a box furnace of batch system, and the obtained carbonized solids were cooled to room temperature. To the solids was then added water to prepare a slurry having a solids content of by weight. The slurry was agitated in a ball mill of grinding-media system to ultrafinely pulverize the solids to submicron particle size.
The slurry of the ultrafinely pulverized particles was diluted with water to a solids content of X by weight. After iron contents were removed using a magnet, coarse particles were separated by means of wet s ‘1 cyclone.
To the slurry of the ultrafine particles without coarse particles was added toluene in a ratio of 1 ml of toluene per 1 g of solids. The mixture was then agitated to oil-agglomerate the ultrafine particles until the particle size is enlarged to about 1 mm. The ash constituents were then removed by recovering the agglomerated secondary particles using a screen.
The recovered agglomerates were dried by heating at 120 0 C for 24 hours to evaporate water, and the obtained dry product was subjected to Rubber Compounding Tests.
COMPARATIVE EXAMPLE GPF carbon black produced by oil-furnace method (NITTERON #55, produced by Shin-Nittetsu Kagaku K. was subjected to Rubber Compounding Tests.
COMPARATIVE EXAMPLE 6 The procedure of Comparative Example 1 was repeated with the exception that a sl’urry was prepared by adding water to uncarbonized Cerrejon coal.
COMPARATIVE EXAMPLE 7 The procedure of Comparative Example 1 was repeated with the exception that the carbonization of Roy- 1 Young coal was conducted at 400 C.
EXAMPLE 6 The procedure of Example 5 was repeated with the exception that the carbonization of Loy Yang coal was conducted at 500 C EXAMPLE 7 The procedure of Example 5 was repeated with the exception that the carbonization of Loy Yang coal was conducted at 650 C for 3 hours.
ili SEXAMPLE 8 The procedure of Example 5 was repeated with the exception that the carbonization of Loy Yang coal was conducted at 900 «C for 3 hours.
EXAMPLE 9 The procedure of Example 5 was repeated with the exception that the carbonization of Loy Yang coal was conducted at 1,100 C for 3 hours.
EXAMPLE The procedure of Example 5 was repeated with the 2 5 exception that the carbonization of Loy Yang coal was I’7i jP conducted at 1,500 «C for 3 hours.
4 COMPARATIVE EXAMPLE 8 The procedure of Example 5 was repeated with the eyception that the carbonization of Loy Yang coal was conducted at 1,800 «C for 4 hours.
EXAMPLE 11 Loy Yang coal (brown coal) was crushed to a particle size of not more than 10 mm. The crushed coal was carbonized by heating at 650 «C for 3 hours in a box furnace of batch system, and the resulting carbonized solids were cooled to room temperature. To the solids was then added water to prepare a slurry having a solids content of 30 by weight. The slurry was agitated in a ball mill of grinding-media system to ultrafinely pulverize the solids to submicron particle size.
The obtained slurry of the ultrafinely pulverized particles was diluted with water to a solids content of 20 by weight. After iron contents were removed from the diluted slurry, coarse particles were separated by means of wet cyclone.
To the slurry of the ultrafine particles without coarse particles was added trichlorotrifluoroethane in a ratio of 1 ml of trichlorotrifluoroethane per 1 g of 27 1 solids. The mixture was then agitated to oil-agglomerate the ultrafine particles until the particle size is enlarged to about 1 mm. The ash constituents were then removed by recovering the agglomerated secondary particles using a screen.
The recovered agglomerates were dried by heating at 120 C for 24 hours to evaporate water and trichlorotriiluoroethane, and the obtained dry product was subjected to Rubber Compounding Tests.
EXAMPLE 12 The procedure of Example 7 was repeated with the exception that 0.02 by weight of polyethylene sulfonic acid and 5 by weight of ethanol were added to the slurry before the ultrafine pulverization.
EXAMPLE 13 The procedure of Example 7 was repeated with the exception that, in the oil-agglomeration step, a solution in that stearic acid, I.e. a compounding ingredient for rubber, was dissolved in toluene in a ratio of 0.02 mg of stearic acid per 1 ml of toluene was added to the slurry in a ratio of 1 ml of the solution per 1 g of the solids.
I: 9’ iii~ -1 -~rr 28 1 EXAMPLE 14 The procedure of Example 7 was repeated with the exception that in the oil-agglomeration step, a solution in that a rubber process oil (DIANA PROCESS OIL AH-58 produced by Idemitsu Kosan Co., Ltd.) was dissolved in toluene in a ratio of 0.05 ml of the process oil per 0.95 ml of toluene was added to the slurry in a ratio of 1 ml of the solution per 1 g of the solids.
The properties of the starting coals and the properties of the products in Comparative Examples 1 to 4 and Examples 1 to 5 are shown in Table 1, and those in Comparative Examples 5 to 8 and Examples 6 to 14 are shown in Table 2.
In order to strictly inquire the effect of ash content by measuring ash content and volatile matter content of the products in Table 1 and Table 2, each product was dried again at a temperature of not less than 105 OC to reduce the water content to 0 previous to the 20 tests.
The measurement of primary particle size was conducted by high speed centrifugal sedimentation method using an automatic particle size distribution analyzer (Horiba Seisaku-sho, CAPA-500).
2- In accordance with JIS K 6383 Test Method for w
N
I 29 Synthetic Rubber-SBR, formulations having the composition described below were prepared by blending thus obtained coal fillers and other ingredients with the rubbers using a 8-inch-double roll mill. Mooney viscosity of the resulting compounded rubbers was measured according to JIS K 6300 Physical Test Method for Unvulcanized Rubbers. The compounded rubbers were then vulcanized under the conditions that were preestablished using JSR Curelastometer III.
Formulation (1) (2) (3) (4) (6) (7) (8) SBR 1500 Zinc oxide No.1 Stearic acid Vulcanization accelerator DM Vulcanization accelerator TS Sulfur Activator (ACTING B) Coal filler 100 (pbw) 5 (pbw) 1 (pbw) 1.2 (pbw) 0.2 (pbw) 2 (pbw) 3 (pbw) variable The amounts of the coal filler were varied as shown in Table 3.
In Comparative Examples 1 to 4 and Examples 1 to in order to strictly compare the effects of the ash contents, the amounts of coal filler were varied so that i i i– 1 compounded rubbers having the same content of actual carbonaceous matters and having varying ash contents could be obtained. In other Comparative Examples and Examples, parts by weight of coal filler was blended.
The components used for the compounded rubbers are those produced by the following companies.
Styrene Butadiene Rubber produced by Japan Synthetic Rubber Co., Ltd.
produced by Sakai Chemical Industry Co., Ltd.
produced by Asahi Denka Kogyo K.K.
Dibenzothiazol disulfide produced by Ouchi Shinko Kagaku K.K.
Tetramethylthiuram monosulfide produced by Ouchi Shinko Kagaku K.K.
Powder sulfur #325 produced by Hosoi Kagaku Kogyo K. K.
produced by Yoshitomi Pharmaceutical Industries, Ltd.
A The properties of the vulcanized compounded r- nrey 31 1 rubbers containing the coal fillers obtained in Comparative Examples 1 to 8 and Examples 1 to 14 are shown in Table 4 and Table 1) according to JIS K 6300 2) 155 C JSR Curelastometer III, based on T max. (Black T on the market) 3) according to JIS K 6301, tension speed: 500 mm/min, measuring temperature: 25 OC test piece: Dumbbell No.3 4) according to JIS K 6301, tension speed: 500 mm/min, measuring temperature: 25 C test piece: Type-B according to JIS K 6301, JIS A hardness meter 6) Goodrich Flexometer, measuring temperature: 50C Samplitude: 0.255 inch, load: 24 lb., rotational frequency: 1800 rpm, measuring time: 25 minutes 7) according to JIS K 6301, measuring temperature: 23 C 2 mm-notch S8) according to JIS K 6301 4 32 1 9) according to JIS K 6301, measuring temperature: 70 °C measuring time: 22 hours 10) BRIDGESTONE Standard 903 part A9 Method-C based on Comparative Examples 1 and 3.
Abrasion resistance, heat build-up, and flexural strength are particularly important properties of carbon blacks among other rubber reinforcing properties.
These properties of carbon blacks varies depending upon the grade, the grade varying depending upon the particle size and the strength of structure. Generally, those excelling in the abrasion resistance are inferior in the exothermic resistance and, on the contrary, those excelling in exothermic resistance are inferior in the abrasion resistance.
The lesser the internal exothermic, flex cracking, and AKRON Abrasion loss which are shown in Table 4 and Table 5 are, the more the carbon blacks excel in the exothermic resistance, flexural strength, and abrasion resistance, respectively.
In the Examples 1 to 5 as opposed to Comparative Examples 1 to 4, the ash constituents in the coals are C -I 33
I.
1 removed by gravity separation and oil-agglomeration or by oil-agglomeration alone. As far as conventional carbon blacks are concerned, abrasion resistance and exothermic resistance are reciprocal properties, that is, the more one is excellent, the more the other is inferior. However, the comparison of the Comparative Examples 1 to 3 with the opposed Examples 1 to 3 indicates that the removal of ash constituents from coal fillers results in the reduction of all the internal exothermic, flex cracking, and AKRON 10 Abrasion and in the improvement of both the exothermic resistance and abrasion resistance, which have been the conflicting properties. It shows that the ash constituents have a bad influence to all of the abrasion resistance, exothermic resistance, and flexural strength. Further, in comparison with the coal fillers obtained in Comparative Examples 1 wherein no removal of the ash constituents was conducted, the coal fillers obtained in Examples 1 to 4 wherein the residual ash content was reduced to not more than about 5 by weight extremely improved the exothermic 20 resistance, abrasion resistance, abrasion resistance, and flexural strength.
The results of the tests in Example 4 which corresponding to Comparative Example 5 were similar to those described above.
Further, the ash constituents have bad influences ~r I-i-Y i u a-nm>.
3 i:: 1 to other rubber-reinforcing properties. This was definitely shown by the fact that the separation and removal of the ash constituents from the coal fillers reduced the vulcanizing time, and improved the tensile properties, i.e. the tensile strength, ultimate elongation, and tear strength, and increased the impact resilience percentage, and reduced compression set. Therefore, from the viewpoint of the improvement of the whole rubberreinforcing properties, the removal of the ash constituents from coal fillers is extremely advantageous.
Comparing the Comparative Example 7 in which the carbon black produced by oil-furnace method with Examples 6 to 10 in which the carbonization by thermal decomposition was cinducted at a temperature of 500 to 1,500 °C the coal lillers produced according to the present invention afford a ensile strength equal or superior to that afforded by the carbon black produced by oil-furnace method, lesser heat build-up, and larger impact resilience. It shows that the coal fillers have properties desirable for reinforcing rubbers.
The coal filler obtained in Comparative Example 6, in which carbonization by thermal decomposition was not conducted, required longer vulcanizing time in comparison with those obtained in Examples 6 to 10. Also, it is inferior in rubber-reinforcing properties as shown in its N 1-x~U. I L_ I 1 low 100 %-modulus, tensile strength, and tear strength and large flex cracking.
Similarly, in Comparative Example 7 in which the carbonization was conducted at 400 °C the vulcanizing time was longer than that of Examples 6 to 10, and afforded lesser 300 %-modulus, tensile strength, and tear strength and larger flex cracking in comparison with Examples 6 to On the other hand, in Comparative Example 8, in which the temperature of carbonization was so high as 1,800 C the 100 X-modulus, 300 %-modulus, and tensile strength were lesser and the heat build-up was larger, in comparison with those of Examples 6 to Also, good results were obtained in Example 11, in which the oil-agglomeration was conducted using a freon.
In Example 12, in which a dispersing agent and an antifoaming agent were added to the slurry before the ultrafine pulverization, the pulverizing efficiency was improved as shown in the reduced particle size of the obtained coal filler.
In Examples 13 and 14, in which a higher fatty acid was used as a binder in order to increase the strength of agglomerates, a tensile strength higher than that of Example 7, in which the surface treatment was not conducted, was obtained.
SAs described above, the coal fillers of the I 36 1 present invention directly produced from a coal &s mo be.
superior in static properties and dynamic properties even to the carbon blacks produced by oil-furnace method.
I TABLE 1 Properties of starting coals and resulting products Starting coal Carbonization Examples and Comparative Kind of Volatile Ash Deliming Temperature Time Examples coal matter content content wt% wt% «C hr Comparative Example 1 Cerrejon 36.2 9.1 None 750 3 Comparative Gravity separation Example 2 Cerrejon 36.2 9.1 (Specific gravity:1.40) 750 3 Comparative Gravity separation Example 3 Cerrejon 36.2 9.1 (Specific gravity:1.30) 750 3 Example i Cerrejon 36.2 9.1 Gravity separation +OA 750 3 (Specific gravity:1.30) Example 2 Cerrejon 36.2 9.1 OA 750 3 Example 3 Cerrejon 36.2 9.1 Gravity separation +OA 750 3 (Specific gravity:1.26) Example 4 Cerrejon 36.2 9.1 Gravity separation +OA 750 3 (Specific gravity:1.35) Comparative Example 4 Loy Yang 49.3 1.6 None 650 2 Example 5 Loy Yang 49.3 1.6 OA 650 2 OA: oil-agglomeration -to be continuedi: 1- I1
I
-continued- Examples and Comparative Examples Comparative Example 1 Comparative Example 2 Comparative Example 3 TABLE 1 Properties of starting coals and resulting products Properties of resulting product Primary particle size ium Secondary particle size mm Moisture Ash Volatile content content matter wt% wt% content wt% Iodine adsorption pH number mg/g 0.74 0.71 0.65 Example 1 0.69 Example 2 0.68 Example 3 0.67 Example 4 0.71 0.0 18.14 3.80 6.19 0.0 10.80 3.91 6.28 0.0 8.18 3.96 6.28 1.5 0.0 3.46 4.16 6.37 1.0 0.0 5.62 4.01 6.00 1.2 0.0 1.98 4.33 6.39 0.8 0.0 4.43 4.08 6.32 0.0 3.52 7.01 8.18 1.2 0.0 0.96 7.23 8.07 j
I
S
i ic Comparative Example 4 0.65 Example 5 0.64 39
I
TABLE 2 Properties of starting coals and resulting products Starting coal Carbonization Examples and Comparative Kind of Volatile Ash Deliming Temperature Time Examples coal matter content content wt% wt% ‘C hr Comparative Example 5 GPF Comparative Example 6 Cerrejon 36.2 9.1 None Comparative Example 7 Loy Yang 49.3 1.6 OA 400 2 Example 6 Loy Yang 49.3 1.6 OA 500 2 Example 7 Loy Yang 49.3 1.6 OA 650 3 Example 8 Loy Yang 49.3 1.6 OA 900 3 Example 9 Loy Yang 49.3 1.6 OA 1100 3 Example 10 Loy Yang 49.3 1.6 OA 1500 3 Comparative Example 8 Loy Yang 49.3 1.6 OA 1800 4 Example 11 Loy Yang 49.3 1.6 OA 650 3 Example 12 Loy Yang 49.3 1.6 OA 1500 3 Example 13 Loy Yang 49.3 1.6 OA 1800 3 Example 14 Loy Yang 49.3 1.6 OA 650 3 OA: oil-agglomeration -to be continued- -continued- TABLE 2 Properties of starting coals and resulting products Properities of resulting product Examples and Comparative Primary Secondary Moisture Ash Volatile Iodine adsorption Examples particle particle content content matter pH number size ium size m wt% wt% content wt% mg/g Comparative Example 5 Comparative Example 6 Comparative Example 7 Example 6 Example 7 Example 8 Example 9 Example 10 Comparative Example 8 Example 11 Example 12 Example 13 Example 14 0.062 0.71 0.68 0.70 0.81 0.66 0.74 0.78 0.75 0.74 0.66 0.73 0.74 0.0 0.09 0.6 6.4 0.0 8.90 36.6 1.28 1.21 1.04 1.17 0.98 0.93 0.97 0.92 0.87 1.15 1.26 18.75 14.26 12.07 7.50 2.10 1.02 0.18 9.43 12.51 14.51 16.23 41 TABLE 3 Examples and Amount of Carbonaceous matter Ash content of Comparative coal filler content of coal filler coal filler Examples (parts by weight) (parts by weight) (parts by weight) Comparative Example 1 Comparative Example 2 Comparative Example 3 Example 1 Example 2 Example 3 Example 4 Comparative Example 4 Example 5 50.0 45.9 44.6 42.4 43.4 41.8 42.8 42.4 41.3 40.93 40.93 40.93 40.93 40.93 40.93 40.93 40.93 40.93 9.07 4.96 3.65 1.47 2.44 0.83 1.85 1.49 0.34 -j, 42 Fundamental Compounding Composition SBR 1500 100 parts by weight Zinc oxide No.1 5 parts by weight Stearic acid 1 part by weight Vulcanization accelerator DM 1.2 parts by weight Vulcanization accelerator TS 0.2 parts by weight Sulfur 2 parts by weight Activator (ACTING B) 3 parts by weight Coal filler variable 1) The amounts of carbon blacks to be compounded in Comparative Examples 1 to 4 and Examples 1 to 5 were varied so that the amounts of carbonaceous matters in all examples were equalized to that of Comparative Example 1. In each other Comparative Examples and Examples, 50 parts by weight of carbon black was blended.
A
i if I Li:.
TABLE 4 Examples and 1) 2) 3) 3) 3) 3) 4) Comparative looney Vulcanizing 0l0%-Modulus 300%-Mlodulus Tensile Ultimate Tear Hardness Examples viscosity time strength elongation strength L 1+4 lOt0C (min.) (kgf/cd) (kgf/ cD (kgf/ c) CO (kgf/cm) (degree) Comparative Examle 1 68.0 32 23 128 228 420 54 63 Coparative Example 2 63.2 30 21 115 231 450 54 61 Comparative Example 3 63.8 30 21 113 225 440 52 61 Example 1 62.6 28 20 118 235 460 58 Example 2 63.2 30 20 116 230 450 54 61 Example 3 61.5 25 20 118 236 480 58 59 Example 4 62.5 28 20 120 238 470 58 Comparative Example 4 62.8 20 24 129 220 420 54 62 Example 5 60.8 17 23 125 238 450 57 61 -to be continued-
A&
1′ -continued- TABLE 4 6) 7) 8) 9) Exuaples and Impact Compression Speci fic Comparative Heat Reduction D Set P Set Flex cracking Reduction of resilience set AKRON Reduction of gravity Exmples build-up of HBU flex cracking»* abrasion AKRON loss abrasion loss AT 00) (co MX CD) (,iu/20times) (co (oZC (CC/lOO0 times) (co Comparative Exqlel1 31 0 -2.29 4.57 5.4 0 62 15.7 0.2654 0 1.1497 Comparative Exmpe 2 30 3.2 -1.72 2.58 5.1 5.6 62 .15.3 0.2547 4.0 1.1306 Comparative Exmpe 3 30 3.2 -1.86 3.12 4.9 9.3 62 15.2 0.2636 4.4 1.1243 Example 1 28 9.7 -1.72 2.78 3.7 31.5 65 14.6 0.2332 12.1 1.1153 Example 2 30 3.2 -1.80 2.96 4.6 14.8 63 15.0 0.2485 6.4 1. 12D4 &xwle 3 .27 12.9 -1.72 2.98 3.6 33.3 65 13.5 0.2316 12.7 1.1098 Example 4 28 9.7 -1.73 2.83 3.7 31.5 64 14.7 0.2346 11.6 1. 1170 Comparative Exwde 4 28 0 -1.43 0.83 4.3 0 65 12.0 0.2410 0 1.119 Example 5 24 14.3 -1.31 0.77 3.6 16.3 67 11.2 0.2220 7.9 1.1040
A
K
TABLE Examples and 1) 2) 3) 3) 3) 3) 4) Comparative Mooney Vulcanizing 100%-odulus 300%-Modulus Tensile Ultimate Tear Hardness Examples Viscosity time strength elongation strength ML 1+4 lOOc (min.) (kgf/ca (lgf/cg D (kgf/cD) (D (kgf/cm) (degree) Comarative Example 5 72.3 23 34 152 205 420 63 66 Comarative Emple 6 66.0 38 18 33 62 620 30 59 Comparative Example 7 72.4 47 30 110 116 320 33 Example 6 69.1 33 33 169 201 380 54 63 Exaple 7 67.8 23 27 160 226 410 57 64 Example 8 65.0 23 25 157 242 470 55 Example 9 62.7 19 23 146 259 450 56 Example 10 60.8 18 22 115 210 490 54 Comparative Example 8 59.6 18 18 74 181 560 52 59 Example 11 68.1 24 27 167 232 400 56 64 Example 12 70.2 22 27 179 254 380 58 63 Example 13 65.5 22 28 160 232 410 56 63 Example 14 58.7 18 23 145 242 480 56 61 -to be continued- -continued- TABLE 6) 7) 8) 9) Exuaples and Flex cracking Impact Comression AKRON~ Specific Comparative Heat D set P Set resilience set abrasion loss gravity Examples build-up AT (It) CD 00 (mm/2000 times) w w (cc/11000 times) Comarative Example 5 26 -1.44 1.58 15.0 54 15.2 0.2102 1.1724 Comarative Exmple 6 26 -1.15 3.23 cut 59 15.6 1.1983 1.09M Comarative Exmle 7 26 -1.43 0.60 cut 66 11.3 0.6060 1.1100 Exple 6 24 -1.44 1.03 13.4 65 11.7 0.2710 1.1163 Example 7 24 -2.00 2.34 6.0 60 17.6 0.2412 1.12Z79 Exmle 8 23 -2.00 2.47 3.5 60 19.9 0.2177 1.1351 Exple 9 23 -2.28 1.20 3.2 60 16.7 0.2211 1.1443 Exmpe 10 24 -2.13 0.87 3.0 60 12.3 0.2346 1.1530 Comarative Wimple 8 26 -1.25 0.73 2.8 59 12.0 0.2820 1.1673 Example 11 23 -2.16 2.18 7.5 61 18.2 0.2358 1.1368 Example 12 20 -1.43 1.75 7.3 60 16.3 0.1770 1.1293 Example 13 22 -1.90 2.44 5.6 60 16.8 0.2284 1.1245 Example 14 20 -1.82 2.62 5.0 58 18.4 0.2758 1.1206

Claims (9)

1. A process for producing a coal filler, which comprises the steps of: carbonization step, which comprises carbonizing crushed coal particles having a particle size of not more than 10 mm and an ash content of not more than 10 by weight by thermal decomposition at a temperature of 500 to 2,000 C and cooling the carbonized solids; ultrafine pulverization step, which comprises preparing a slurry of the carbonized solids having a solids content of 10 to 50 by weight by adding a dispersion medium to the carbonized solids; and ultrafinely pulverizing the carbonized solids dispersed in the slurry to reduce the average particle size to not more than 5 u m; agglomeration step, which comprises adjusting the solids content of the slurry to 1 to 20 by weight by further addink water to the slurry of the ultrafinely pulverized solids; adding an oil having a boiling point of not’more than 150 OC to the resulting slurry in a ratio of 30 to 300 parts by weight of the oil per 100 parts by weight of dry solids; agitating the resulting mixture to agglomerate the carbonaceous matters with oil; and separating and recovering the agglomerates; and R4 (hh 251 drying step, which comprises drying the recovered i N M i 48 agglomerates by heating them at a temperature in the range 50 to 300*C to evaporate the water and oil retained in the agglomerates; and cooling the dried agglomerates.

2. The process as claimed in claim 1, wherein in the step the carbonized solids are pulverized to not more than 200 mesh Tyler prior to the preparation of the slurry.

3. The process as claimed in claim 1 or claim 2, wherein, in the step the slurry is prepared by adding a dispersing agent and/or an antifoaming agent together with water. S» 4. The process as claimed in any preceding claim, Swherein, in the step iron contents in the slurry are removed by the means of a magnet after the preparation of the slurry. The process as claimed in any preceding claim, wherein, in the step coarse particles are classified and removed by the use of a wet classifier after the adjustment of the solids content of the slurry.

6. The process as claimed in any preceding claim, wherein the oil comprises a hydrocarbonaceous oil or 1,1,2-trichloro-l,2,2-trifluoroethane. t The process as claimed in claim 6, wherein the S’ hydrocarbonaceous oil is toluene. S8. The process as claimed in any preceding claim, wherein, in the step the oil is previously mixed with a compounding ingredient for rubber and/or a higher fatty acid of 12 to 24 carbon atoms.

9. The process as claimed in any preceding claim, k’ 1; 49 wherein the oil is previously mixed with a surface modifier for the ultrafinely pulverized particles. The process as claimed in claim 9, wherein the surface modifier is a process oil for rubber, an activator, or a vulcanization accelerator.

11. The process as claimed in any preceding claim, wherein, in the step the oil recovered in the drying step is used.

12. A process for producing a coal filler according to claim 1 and substantially as hereinbefore described with reference to the Examples.

13. A coal filler produced by the process of any preceding claim. DATED this 30th day of October 1989. 444 0 4 0

604. .4 a *i 9 *0 #00 IDEMITSU KOSAN CO., LTD. By Its Patent Attorneys DAVIES COLLISON ti I 4* Cf I

AU79651/87A
1986-09-18
1987-09-17
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