EP0029712B1 - Procédé en plusieurs étapes consécutives pour l'amélioration du charbon - Google Patents

Procédé en plusieurs étapes consécutives pour l'amélioration du charbon Download PDF

Info

Publication number
EP0029712B1
EP0029712B1 EP19800304161 EP80304161A EP0029712B1 EP 0029712 B1 EP0029712 B1 EP 0029712B1 EP 19800304161 EP19800304161 EP 19800304161 EP 80304161 A EP80304161 A EP 80304161A EP 0029712 B1 EP0029712 B1 EP 0029712B1
Authority
EP
European Patent Office
Prior art keywords
coal
oil
water
agglomerates
liberated
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
Application number
EP19800304161
Other languages
German (de)
English (en)
Other versions
EP0029712A3 (en
EP0029712A2 (fr
Inventor
Edward C. Capes
William L. Thayer
Richard D. Coleman
Leonard Messer
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Canadian Patents and Development Ltd
Original Assignee
Canadian Patents and Development Ltd
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by Canadian Patents and Development Ltd filed Critical Canadian Patents and Development Ltd
Publication of EP0029712A2 publication Critical patent/EP0029712A2/fr
Publication of EP0029712A3 publication Critical patent/EP0029712A3/en
Application granted granted Critical
Publication of EP0029712B1 publication Critical patent/EP0029712B1/fr
Expired legal-status Critical Current

Links

Images

Classifications

    • C—CHEMISTRY; METALLURGY
    • C21—METALLURGY OF IRON
    • C21B—MANUFACTURE OF IRON OR STEEL
    • C21B5/00—Making pig-iron in the blast furnace
    • C21B5/001—Injecting additional fuel or reducing agents
    • C21B5/003—Injection of pulverulent coal
    • C21B5/004—Injection of slurries
    • 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
    • C10L1/00—Liquid carbonaceous fuels
    • C10L1/32—Liquid carbonaceous fuels consisting of coal-oil suspensions or aqueous emulsions or oil emulsions
    • C10L1/322—Coal-oil suspensions

Definitions

  • This invention relates to an in-line method for the upgrading of coal and the formation of a coal-in-oil combustible fuel therefrom.
  • the coal fines may contain significant proportions of hydrophilic (or oleo- phobic) impurity or ash-forming particles composed of silica, alumina, pyrite, etc. to which the functional groups of the light hydrocarbon oil bridging liquid are incapable of attaching themselves so that when the coal particle agglomerates are formed, these particles remain suspended in the water and are thus effectively separated from the coal particles.
  • hydrophilic or oleo- phobic impurity or ash-forming particles composed of silica, alumina, pyrite, etc.
  • Controlled moisture content could also be useful when the coal-in-oil suspension is subjected to vibratory energy such as, for example, in burners which use vibratory energy to increase the combustion efficiency in combustion chambers.
  • French patent application No. 2 323 754 describes a process for preparing a liquid fuel comprising a suspension of coal particles in a hydrocarbon oil by treating an aqueous suspension of coal particles in a first agglomeration device, separating the agglomerates, disintegrating the agglomerates and re-agglomerating them in a second agglomeration device, separating these agglomerates and taking them up in a hydrocarbon fuel.
  • the agglomeration step is repeated in order to obtain the required degree of deashing.
  • the largest coal particles are separated ground and recirculated.
  • a method for the continuous beneficiation of coal and the continuous formation of a coal-in-oil combustible fuel therefrom in which coal is comminuted in water to produce a coal-in-water slurry, the coal-in-water slurry is mixed with an agglomerating liquid to agglomerate the coal particles, and the agglomerates are separated out and mixed with oil to form a coal-in-oil combustible fuel, characterized in that the method comprises the following steps:
  • Figure 1 there is shown a method for continuous beneficiation of coal and the continuous formation of a coal-in-oil combustible fuel therefrom, comprising:
  • a dry pulverizer 28 is used for the initial stage of grinding since this will generally pulverize coal faster and in a smaller equipment volume than with wet methods, although wet grinding may be used throughout, if desired.
  • the coat is ground down to a required particle size sufficient to effect separation or dissociation of coal particles and impurities.
  • Coal to be pulverized is fed from a storage hopper 30 to the dry pulverizer 28 which is swept with air from a supply 32.
  • the swept air, with entrained pulverized coal is fed from the pulverizer 28 to a wet scrubber 34.
  • Water containing the pulverized coal is fed from the wet scrubber 34 to the wet mill 1 while air, which has been scrubbed free from the pulverized coal in the wet scrubber 34, is exhausted therefrom at 36.
  • coal-in-water slurry 2 from the wet mill 1 is stirred in three mixing devices 4 to 6 arranged in cascade.
  • One mixing device could be used provided that the residence time for the coal of the coal-in-water slurry 2 therein to be micro-agglomerated is tolerable. With the embodiment shown in Figure 1, a residence time of four minutes was required and so the three mixing devices 4 to 6 were provided.
  • the first mixing device 4 is a high shear mixing device and may be a conventional turbine mixer.
  • the first mixing device 4 is used to disperse the light oil agglomerating liquid 8 in the coal-in-water slurry 2 and give an initial mixing.
  • the second and third mixing devices 5 and 6 respectively are relatively lower blade speed, intermediate intensity mixing devices as compared with the mixing device 4 and are for producing the micro-agglomerates. It should be noted that in different embodiments of the present invention, only one lower intermediate- intensity mixing device is necessary and in other embodiments different mixing devices may be used, such as, for example, one or more emulsifying units with or without one or more lower, intermediate intensity mixing devices.
  • the light oil agglomerating liquid additive 8 is fed to the first mixing device 4 from a storage tank 38.
  • micro-agglomerated, impurity-liberated coal is separated from the dissociated components comprising primarily a large amount of inorganic impurities and some water on the screen 10, which in this embodiment is a stationary, inclined screen down which the separated, micro-agglom- .erated, impurity-liberated coal rolls and emerges as micro-agglomerates 12 while the dissociated inorganic impurities and water, designated 40, drain through the screen and are conveyed to a settling pond 42.
  • a vibrating screen separator or wet cyclone separator could be used at this stage if the micro-agglomerates possess sufficient strength not to break up in such apparatus.
  • the embodiment shown in Figure 1 is arranged to recycle most of the water from delivery 40 to the settling tank 42, together with make-up water 44 which is fed thereto.
  • the water 46 from the settling tank provides feed to the wet scrubber 34, wet mill 1 and the first mixing device 4.
  • the micro-agglomerates 12 then pass to the mixing device 14 which is also a relatively lower blade speed, intermediate intensity mixing device as compared with the mixing device 4.
  • the relatively larger agglomerates are separated from the dissociated water and inorganic impurities on the vibrating screen 18 because the relatively larger agglomerates have sufficient strength not to break up on the vibrating screen 18, which is an efficient separator for the purpose.
  • a wet cyclone separator, other types of screens, etc., could also be used at this stage if desired.
  • the dissociated water and inorganic impurities designated 48 drain through the vibrating screen 18 and are conveyed to a separation tank 50 from which a portion 52 of the water is returned to the stirrer 14 while the remaining water and inorganic impurities 54 are conveyed to the settling pond 42.
  • the reason why the water portion 52 is returned to the mixing device 14 is to ensure that sufficient water is delivered, with the relatively larger agglomerates, to the vibrating screen 18 to ensure that the inorganic impurities are thoroughly washed from the relatively larger agglomerates. This substantially reduces the possibility of inorganic impurities being carried over the vibrating screen 18 with the relatively larger agglomerates.
  • the water in mixing device 14 would usually be heated to about 60°C to reduce the viscosity of the heavy fuel oil 16. Recirculation of water portion 52 avoids loss of thermal energy in discarded hot water.
  • the mixer 22, to which the relatively larger agglomerates 20 are conveyed in this embodiment is a stationary, cylindrical vessel having a mixing device rotating about a horizontal axis.
  • Other types of mixers may also be used such as, for example, a paddle type mixer.
  • the coal-in-oil combustible fuel 26 is stored in an agitated condition in a holding tank 56 from which it is withdrawn by a pump 58 at the desired rate for consumption as a combustible fuel in, for example, an electrical power generating installation (not shown).
  • the method can be matched to the desired rate of consumption of the combustible fuel so that the holding tank 56 is merely provided for storage to accommodate any fluctuations in the production of the coal-in-oil combustible fuel or the consumption thereof.
  • Minto coal A typical analysis of the Minto coal is given below which shows that this is a coal having a high ash and sulphur content.
  • the weight ratio of air to coal fed to the dry pulveriser 28 was in the range 1.5:1 to 2:1. 40 wt % coal and 60 wt % water were present in the wet mill 1.
  • the first mixing device 4 was fed with 20 wt % coal, 3 wt % No. 2 fuel oil and 77 wt % water.
  • the plant was a pilot plant designed to be capable of treating 100 Imperial gallons/min. (455 I/min.) of slurry 2, which is equivalent to about 6 tons/hour (5.44 tonnes/hour) of coal solids (including impurities) based on the 20 wt % slurry fed to the first mixing device 4.
  • the blades of the high shear mixing device 4 which were driven by a 5 HP motor at 3,220 rpm, comprised two groups of four high shear impeller blades, two of which are shown for each group and designated 60 to 63, which tapered radially outwardly towards truncated extremities.
  • the high shear impeller blades 60 and 62 were mounted in an 18 inch (0.46 m) internal diameter tank 64 having a 35 inch (0.89 m) height with an annular baffle 66 between the impeller blades 60 and 62 and four vertical baffles, two of which are shown and designated 68 and 70, equally spaced therearound to enhance their shearing effect on the coal-in-water slurry 2.
  • the four blades of each of the relatively lower blade speed, intermediate intensity mixing devices 5, and 6 and 14, which were driven by a 5 HP motor at 280 rpm comprised pitched, turbine impeller blades two of which are shown and designated 72 and 74.
  • the blades 72 and 74 were mounted in a 40 in. (1.02 m) internal diameter vessel having a 40 in. (1.02 m) overflow height with four vertical baffles, two of which are shown and designated 76 and 78, equally spaced around the blades 72 and 74 to enhance their shearing effect.
  • the dissociated inorganic impurities and water, designated 40 mainly comprised 96 wt % water and 3 wt % ash and sulphur as the main inorganic impurities together with 1 wt % unagglomerated combustible matter.
  • the relatively larger agglomerates produced by mixer 14 comprised 70 wt % coal, 20 wt % oil and 10 wt % water to which was added sufficient No. 6 fuel oil in the mixer 22 for the coal-in-oil combustible fuel 26 to comprise a coal/oil weight ratio of 40/60.
  • Preferred light oils/as agglomerating liquid are No. 2 fuel oil and diesel oil.
  • Other light oils as agglomerating liquid are, for example, light petroleum fractions, kerosene, coke oven light oil and light crude and residual and waste oils.
  • Preferred heavy fuel oils as agglomerating liquid are No. 6 fuel oil and heavy residual oils.
  • Other heavy fuel oils as agglomerating liquid are, for example, crude oils and coke oven tar.
  • the quantity of light oil agglomerating liquid additive used will depend upon the type of coal being processed and how finely the coal must be ground to produce impurity-liberated coal particles. While a greater quantity of light oil agglomerating liquid additive could be used than 20 wt % of the total weight of solids of the coal-in-water slurry the desirable thing according to the present invention is that only up to 20 wt % need be used so that the final coal-in-oil combustible fuel will contain, for example, the maximum amount of heavy oil for which an oil-fired installation was originally designed, when the coal-in-oil combustible fuel is for use in this manner.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Organic Chemistry (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Manufacturing & Machinery (AREA)
  • Materials Engineering (AREA)
  • Metallurgy (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Liquid Carbonaceous Fuels (AREA)
  • Solid Fuels And Fuel-Associated Substances (AREA)

Claims (6)

1. Procédé en continue pour traiter du charbon afin de produire un combustible constitué par une suspension de charbon dans de l'huile, selon lequel du charbon est pulvérisé dans le l'eau pour former une suspension de charbon dans de l'eau (2), la suspension de charbon dans de l'eau est mélangée avec une liquide agglomérant (8) destiné à agglomérer les particules de charbon, et les agglomérats (20) sont séparés et mélangés à de l'huile pour former un combustible constitué par une suspension de charbon dans de l'huile (26), caractérisé en ce qu'il comprend les étapes suivantes:
a) pulvériser du charbon dans de l'eau pour former une suspension de charbon dans l'eau (2) comprenant des particules de charbon purifié dont la taille pour une particule de poids moyen, est au moins aussi faible que 40 µm, puis
b) mélanger la suspension de charbon dans l'eau (2) avec de l'huile légère (8) en tant que liquide agglomérant dont la masse spécifique est inférieure à 1 g/cm3 pour agglomérer les particules de charbon purifié en agglomérats (12) relativement petits et en dissocier essentiellement des impuretés inorganiques et de l'eau, l'huile légère en tant que liquide agglomérant étant ajoutée dans une quantité non supérieure à 20 % en poids du poids total des solides contenus dans la suspension de charbon dans l'eau, puis
c) séparer les agglomérats (12) relativement petits purifiés des impuretés inorganiques dissociées et de l'eau, puis
d) mélanger les agglomérats (12) relativement petits purifiés et séparés avec du mazout lourd (16) dont la masse spécifique est supérieure à 0,9 g/cm3 et supérieure à celle de l'huile légère (8), en tant que liquide agglomérant pour former des agglomérats relativement gros dont la dimension moyenne n'est pas supérieure à 3 mm, et dissocier principalement de l'eau et des impuretés inorganiques qui étaient contenues dans les agglomérats relativement petis et purifiés, et laisser une quantité résiduelle d'au moins 5 % en poids d'eau dans les agglomérats relativement gros, puis
e) séparer les agglomérats relativement, gros (20) de l'eau et des impuretés inorganiques dissociées, puis
f) mélanger les agglomérats relativement gros (20) séparés avec de l'huile lourde additionnelle (24) de complément pour former un combustible (26) constitué par une suspension de charbon dans l'huile.
2. Procédé selon la revendication 1, caractérisé en ce que le charbon est pulvérisé initialement dans un pulvérisateur à sec (28), de l'air est extrait du charbon pulvérisé sec dans un épurateur par voie humide (34), puis le charbon pulvérisé et épuré est broyé dans de l'eau pour former la suspension de charbon dans l'eau (2).
3. Procédé selon la revendication 1 ou la revendication 2, caractérisé en ce que la suspension de charbon dans l'eau (2) est remuée initialement avec l'huile légère agglomérante (8) dans un dispositif agitateur à cisaillement élevé, pour donner un mélange initial, puis dans au moins un dispositif mélanger (5, 6) du puissance intermédiaire à vitesser d'ailettes relativement plus basse.
4. Procédé selon l'une quelconque des revendications 1 à 3, dans lequel l'huile légère (8), en tant que liquide agglomérant, est choisie parmi le groupe constitué par le mazout N° 2 et la gazole.
5. Procédé selon l'une quelconque des revendications 1 à 4, dans lequel l'huile lourde
(16), en tant que liquide agglomérant, est choisie parmi le groupe constitué par le mazout N° 6 et les huiles résiduelles lourdes.
EP19800304161 1979-11-22 1980-11-20 Procédé en plusieurs étapes consécutives pour l'amélioration du charbon Expired EP0029712B1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
CA340749 1979-11-22
CA000340749A CA1117884A (fr) 1979-11-22 1979-11-22 Methode pour l'enrichissement en reseau de la houille, et preparation d'un combustible houille et huile par la mise en oeuvre de ladite methode

Publications (3)

Publication Number Publication Date
EP0029712A2 EP0029712A2 (fr) 1981-06-03
EP0029712A3 EP0029712A3 (en) 1981-11-11
EP0029712B1 true EP0029712B1 (fr) 1984-07-25

Family

ID=4115706

Family Applications (1)

Application Number Title Priority Date Filing Date
EP19800304161 Expired EP0029712B1 (fr) 1979-11-22 1980-11-20 Procédé en plusieurs étapes consécutives pour l'amélioration du charbon

Country Status (3)

Country Link
EP (1) EP0029712B1 (fr)
CA (1) CA1117884A (fr)
DE (1) DE3068727D1 (fr)

Families Citing this family (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2526680B2 (fr) * 1978-12-04 1990-03-02 American Minechem Corp Procede de transformation de matieres charbonneuses en une charge d'alimentation amelioree
CA1216551A (fr) * 1984-05-23 1987-01-13 Her Majesty The Queen In Right Of The Province Of Alberta As Represented By The Minister Of Energy And Natural Resources Agglomeration selective des fines de charbon sous-bitumineux
US4730787A (en) * 1984-06-19 1988-03-15 The University Of Toronto Innovations Foundation Method of separating solids by simultaneous comminution and agglomeration
US5096461A (en) * 1989-03-31 1992-03-17 Union Oil Company Of California Separable coal-oil slurries having controlled sedimentation properties suitable for transport by pipeline
AU5349090A (en) * 1989-03-31 1990-11-05 Union Oil Company Of California Separable coal-in-oil mixtures having controlled sedimentation properties and method for making same

Family Cites Families (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3665066A (en) * 1969-11-28 1972-05-23 Canadian Patents Dev Beneficiation of coals
AU499147B2 (en) * 1975-09-09 1979-04-05 Shell Internationale Research Maatschappij Bv Coal/hydrocarbon coil suspension

Also Published As

Publication number Publication date
CA1117884A (fr) 1982-02-09
DE3068727D1 (en) 1984-08-30
EP0029712A3 (en) 1981-11-11
EP0029712A2 (fr) 1981-06-03

Similar Documents

Publication Publication Date Title
US4284413A (en) In-line method for the beneficiation of coal and the formation of a coal-in-oil combustible fuel therefrom
CA1133700A (fr) Methode d'enrichissement de la houille, et produits derives
Papachristodoulou et al. Coal slurry fuel technology
US4332593A (en) Process for beneficiating coal
CA1168871A (fr) Procede de decendrage et de transport de la houille
WO1983004189A1 (fr) Procedes de traitement du charbon
US4030894A (en) Stabilized fuel slurry
CA1146893A (fr) Procede de desulfuration et de reduction de la teneur en cendres des charbons
JPS59133295A (ja) 粉末化固体燃料、石油残留物および水をベ−スとする液体燃料、その製造方法、およびボイラ−または工業炉中のその応用
US4564369A (en) Apparatus for the enhanced separation of impurities from coal
US1420164A (en) Process of purifying materials
EP0029712B1 (fr) Procédé en plusieurs étapes consécutives pour l'amélioration du charbon
CA1109818A (fr) Batterie de fours de cokefaction, et agglomeration des fines engendrees par le procede
EP0032811B1 (fr) Procédé d'amélioration du charbon et charbon ainsi amélioré
US4536372A (en) Apparatus for beneficiating coal
US4526585A (en) Beneficiated coal, coal mixtures and processes for the production thereof
CA1194304A (fr) Charbon enrichi, ses melanges et leur production
US4412842A (en) Coal beneficiation process
Kim et al. Effect of grinding conditions on the performance of a selective agglomeration process for physical coal cleaning
KR100881627B1 (ko) 석탄 혼합 액상연료 제조장치, 이를 이용한 석탄 혼합액상연료 제조방법 및 이에 의하여 제조된 석탄 혼합액상연료
WO1982001376A1 (fr) Combustible a dispersion et procede de fabrication de celui-ci
US4869727A (en) Production of hardened coal agglomerates
US5474582A (en) Coal-water mixtures from low rank coal and process of preparation thereof
JPS58150423A (ja) 石炭微粉の水中造粒方法
CA1194305A (fr) Melanges charbon-huile et methode d'obtention

Legal Events

Date Code Title Description
PUAI Public reference made under article 153(3) epc to a published international application that has entered the european phase

Free format text: ORIGINAL CODE: 0009012

AK Designated contracting states

Designated state(s): BE DE FR GB IT

PUAL Search report despatched

Free format text: ORIGINAL CODE: 0009013

AK Designated contracting states

Designated state(s): BE DE FR GB IT

17P Request for examination filed

Effective date: 19811124

RAP1 Party data changed (applicant data changed or rights of an application transferred)

Owner name: MESSER, LEONARD

Owner name: CANADIAN PATENTS AND DEVELOPMENT LIMITED

ITF It: translation for a ep patent filed

Owner name: SOCIETA' ITALIANA BREVETTI S.P.A.

GRAA (expected) grant

Free format text: ORIGINAL CODE: 0009210

AK Designated contracting states

Designated state(s): BE DE FR GB IT

REF Corresponds to:

Ref document number: 3068727

Country of ref document: DE

Date of ref document: 19840830

ET Fr: translation filed
PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: FR

Payment date: 19841213

Year of fee payment: 5

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: DE

Payment date: 19841218

Year of fee payment: 5

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: BE

Payment date: 19841231

Year of fee payment: 5

PLBE No opposition filed within time limit

Free format text: ORIGINAL CODE: 0009261

STAA Information on the status of an ep patent application or granted ep patent

Free format text: STATUS: NO OPPOSITION FILED WITHIN TIME LIMIT

26N No opposition filed
ITTA It: last paid annual fee
PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: GB

Effective date: 19891120

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: BE

Effective date: 19891130

BERE Be: lapsed

Owner name: MESSER LEONARD

Effective date: 19891130

Owner name: CANADIAN PATENTS AND DEVELOPMENT LTD

Effective date: 19891130

GBPC Gb: european patent ceased through non-payment of renewal fee
PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: FR

Effective date: 19900731

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: DE

Effective date: 19900801

REG Reference to a national code

Ref country code: FR

Ref legal event code: ST