CA2026828A1 - Process of feeding coal slurry filtration sludge - Google Patents
Process of feeding coal slurry filtration sludgeInfo
- Publication number
- CA2026828A1 CA2026828A1 CA 2026828 CA2026828A CA2026828A1 CA 2026828 A1 CA2026828 A1 CA 2026828A1 CA 2026828 CA2026828 CA 2026828 CA 2026828 A CA2026828 A CA 2026828A CA 2026828 A1 CA2026828 A1 CA 2026828A1
- Authority
- CA
- Canada
- Prior art keywords
- sorbent
- coal slurry
- slurry filtration
- filtration sludge
- process according
- 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.)
- Abandoned
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 OR C10K; LIQUIFIED PETROLEUM GAS; USE OF ADDITIVES TO FUELS OR FIRES; FIRE-LIGHTERS
- C10L9/00—Treating solid fuels to improve their combustion
- C10L9/10—Treating solid fuels to improve their combustion by using additives
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Combustion & Propulsion (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Organic Chemistry (AREA)
- Fluidized-Bed Combustion And Resonant Combustion (AREA)
- Treating Waste Gases (AREA)
Abstract
In a process of feeding coal slurry filtration sludge to be combusted in a fluidized bed reactor, coal slurry filtration sludge is mixed with a fine-grained sorbent for 50x and/or a fine-grained sorbent for moisture in such a manner that 20 to 40% by weight of the coal slurry filtration sludge to be fed and contained in the mixture have a particle size of 5 to 30 mm and the resulting freely flowing product is fed to the fluidized bed. The coal slurry filtration sludge is preferably mixed with limestone as a sorbent for 50xand/or with ash from the fluidized bed as a sorbent for moisture, each of which sorbents has a particle size From 50 to 300 .mu.m. The process can be used to special advantage to feed coal slurry filtration sludge to the combustion chamber of a circulating fluidized bed.
Description
. _ g ~etallgesellschaft AG October 5, 19~9 Reuterweg 14 6000 Frankfurt-on-~aln 1 Ca~e No. B90109 ProceYs of Feedlng Coal Slurry Filtratlon Sludge DESCRIPTION
This invention relaties to a process of feeding cosl slurry filtrstlon sludge to be combusted ln a fluldlzed bed reactor snd the use of thst process to feed coal slurry filtration sludge to a circulating fluidized bed. Coal slurry filtration sludge means a coal filter sludge which is obtained by a filtrstion of coal slurry.
Coal for power plants 1~ upgraded by processes by which the pyrlte content and the ash content of sald feed -~
cosl sre decressed. The waste products thus obtslned comprise high-pyrite talllngs and partlcularly comprlse an ultrsfine coal slurry flltratlon sludge. the valuable content of which will not be uaed if that sludqe 19 dumped. Oe~ides, problems are lnvolved ln the dumping of coal slurry flltration sludge.
Low-grade fuels csn be combusted in a fluldized bed, ~artlcularly in a clrculatlng fluidized bed, provlded that the fuel can be lntroduced ln a proper form lnto the combustlon chamber ln whlch the fluldized bed is malntalned.
~ feedlng of coal slurry flltration sludge will give rlse to conslderable dlfflculty becsuse such sludge become~ avallable as thixotrop~c and stlcky clods, whlch have an area of about 0.25 m2 and a thlckness of about 30 mm and can be handled only with difficulty.
i ~; " ~ ~ ;' ' . i ' ` I; . . i ~ , ~2~,2~
In an attempt to facilitate the handlino it has already been proposed to transform the filtration sludge to a pumpable pulp by an addition of water and to feed the result-., ing pulp to the comoustor, e.g., to the combustion chamber ofa ~luidized bed reactor.
~ ut that procedure involves the great disadvantage that a considerable part of the heating value oF the fuel is consumed in the evaporation and superheating of the water which has been added. Owlng to the high rate at which energy iB re-quired to evaporate the water, the rate at which coal slurry filtration sludge is required for a de~ired usable heat output of the fuel-firing plant will be much higher than would other-wise be necessary.
It i9 an ob~ect of the invention to provide a process which is free of the known disadvantages, particularly of those mentioned hereinbefore, and permits a simple, econo-mical and ssFe feeding of coal slurry Filtration ~ludge to a fluidlzed bed reactor.
In a process of the kind which is described first herelnbefore that obJect is accomplished in accordance with the inventlon ln that coal slurry flltration sludge ls mixed with a fine-grained sorbent for 50x and/or a fine-grained sor-bent for moisture in such a manner that ZO to 40X by weight of the coal slurry filtration sludge to be fed and contained in the mixture have a particle size of 5 to 30 mm and the re-sulting freely flowing product is fed to the fluidized bed reactor.
202~?,~
The mixing o~ coal slurry filtratlon sludge with a sorbent for 50x and/or a sorbent for moisture may be effec-ted in two separately operated mixers. For instance, 60 to aO%
by weight oF the coal slurry filtration sludge may be pre-mixed in a ~ixing plant which is provided with cutter blades ao that a substantially homogeneous mixture will be produced.
In that case the clods of coal slurry filtration sludge will be cru~hed and substantially uni~ormly di~tributed by the cutter blades, which revolve at about 1500 to 3000 r.p.m. The remaining 40 to Z0% by welght of the coal slurry filtratlon sludge are then incorporated in such a manner that sludge par-ticles of 5 to 30 mm are obtained. That operatlon must also be performed by mixers which can di~integrate coar~e lumps or clods of the coal 31urry filtration sludge. In both mixlng stages each particle whlch has been formed by the disintegra-tion of the clod of coal slurry filtration sludge must be covered by the sorbent for S0 and/or the sorbent for moisture so that 8 recombinatlon of lndividual particles to form larger agglomerate~ of fllter ~ludge w111 be avoided. A proper tlmlng of the tleatments wlll ensure that a substantislly ho-mogeneous mlxtl~re wlll be obtalned ln the flrst stage and the required disintegratlon lnto particle~ of 5 to 30 mm will be obtained in the second stage.
It wlll be particularly desirable to perform the mixing and dlsintegrating in one mixing plant. Such plant may conslst, e.g., of a horizontal cyllndrical mixer compri~ing ~:r":~
` 2~2~2~
.`
plowshares or blades rotating about a horlzontal axls and an additional inserted-tooth cutter (chopper) mounted on a separate drive shaft. The horizontal shaft should rotate at about 120 to 200 r.p.m. and the drive shaft ~or the inserted-tooth cutter at about 1500 to 3000 r.p.m. Just as in the second stage of the two-stage treatment, care must be taken to avoid an excessive disintegration or even a homogeneous mixing of the entire coal slurry filtration Yludge. A mixing for about one mlnute may be quite sufficient.
Limestone, calcium hydroxide and/or calcium oxide are particularly desirable sorbents fDr S0x. ~fecause lime-eftone will release carbon dioxide and be transformed to cal-cium oxide at the combustion temperatures employed, a pre-ferred feature of the inventlon resides in that the coal slurry filtration sludge is mixed with limestone as a sorbent for S0x.
The sorbent for moisture may be of any desired kind, provided that it has the required sorbent property. For Instance, wood meal or powderized coal may be employed. In a partlcularly desirable embodiment of the invention, coal lurry filtration sludge i9 mixed with ash from the fluidized bed. An advsntage resides, e.g., in that unreacted limestone or unreacted calcium oxide contained in the ash from the fluidized bed may be uaed as a sorbent for SDX.
If ash which comes from the fluidized bed and contains calcium oxide i9 used as a sorbent for moi~ture and/or as a sorbent for S0x, water contained in the coal slurry fil-tration sludge will be bound not only physically but also by a chemical reaction.
f'G7f ' :
The selection of the kind and optionally of the proportions of the components which are required for the production of a freely flowing product and consists of a sorbent for Sx and/or a sorbent for moisture will particularly depend on the sulfur content of the coal contained in the coal slurry filtration sludge. Virtually only a sorbent for moisture may be mixed with a coal which contains virtually no sulfur. The share of the sorbent for Sx will generally be increased with the sulfur content.
The content of the sorbent for SO should generally be so high that the sulfur content of the coal can be bound. In the determination of the rate at which the sorbent for Sx will be required the content of unreacted lime, for instance, which is contained in the ash from the fluidized bedj should be taken into account.
In processing coal slurry filtration sludge with a relatively high sulfur content it is also possible to omit an addition of sorbent for sulfur oxide and to admix only a sorbent for moisture, in particular sulfur containing powderized coal (coal dust). In that case the sulfur oxide content of the off gas is used e.g. for the production of sulfuric acid.
In a preferred embodiment of the process in accordance with the invention, in which ash from the fluidized bed is used as a sorbent for moisture and/or limestone is used as a sorbent for S0x, and assuming that the coal slurry filtration sludge has the usual moisture content of about 30 to 40% by weight the amount of coal slurry filtration sludge in the final mixture will be between limits which are determined by the ranges from 70 to 50% by weight if only ash from the fluidized bed is admixed and by the range from 30 to 50% by weight if only limestone i8 admixed. The above-mentioned statement relating to the amount of coal slurry filtration sludge in the mixture means: -i . ' , j /
This invention relaties to a process of feeding cosl slurry filtrstlon sludge to be combusted ln a fluldlzed bed reactor snd the use of thst process to feed coal slurry filtration sludge to a circulating fluidized bed. Coal slurry filtration sludge means a coal filter sludge which is obtained by a filtrstion of coal slurry.
Coal for power plants 1~ upgraded by processes by which the pyrlte content and the ash content of sald feed -~
cosl sre decressed. The waste products thus obtslned comprise high-pyrite talllngs and partlcularly comprlse an ultrsfine coal slurry flltratlon sludge. the valuable content of which will not be uaed if that sludqe 19 dumped. Oe~ides, problems are lnvolved ln the dumping of coal slurry flltration sludge.
Low-grade fuels csn be combusted in a fluldized bed, ~artlcularly in a clrculatlng fluidized bed, provlded that the fuel can be lntroduced ln a proper form lnto the combustlon chamber ln whlch the fluldized bed is malntalned.
~ feedlng of coal slurry flltration sludge will give rlse to conslderable dlfflculty becsuse such sludge become~ avallable as thixotrop~c and stlcky clods, whlch have an area of about 0.25 m2 and a thlckness of about 30 mm and can be handled only with difficulty.
i ~; " ~ ~ ;' ' . i ' ` I; . . i ~ , ~2~,2~
In an attempt to facilitate the handlino it has already been proposed to transform the filtration sludge to a pumpable pulp by an addition of water and to feed the result-., ing pulp to the comoustor, e.g., to the combustion chamber ofa ~luidized bed reactor.
~ ut that procedure involves the great disadvantage that a considerable part of the heating value oF the fuel is consumed in the evaporation and superheating of the water which has been added. Owlng to the high rate at which energy iB re-quired to evaporate the water, the rate at which coal slurry filtration sludge is required for a de~ired usable heat output of the fuel-firing plant will be much higher than would other-wise be necessary.
It i9 an ob~ect of the invention to provide a process which is free of the known disadvantages, particularly of those mentioned hereinbefore, and permits a simple, econo-mical and ssFe feeding of coal slurry Filtration ~ludge to a fluidlzed bed reactor.
In a process of the kind which is described first herelnbefore that obJect is accomplished in accordance with the inventlon ln that coal slurry flltration sludge ls mixed with a fine-grained sorbent for 50x and/or a fine-grained sor-bent for moisture in such a manner that ZO to 40X by weight of the coal slurry filtration sludge to be fed and contained in the mixture have a particle size of 5 to 30 mm and the re-sulting freely flowing product is fed to the fluidized bed reactor.
202~?,~
The mixing o~ coal slurry filtratlon sludge with a sorbent for 50x and/or a sorbent for moisture may be effec-ted in two separately operated mixers. For instance, 60 to aO%
by weight oF the coal slurry filtration sludge may be pre-mixed in a ~ixing plant which is provided with cutter blades ao that a substantially homogeneous mixture will be produced.
In that case the clods of coal slurry filtration sludge will be cru~hed and substantially uni~ormly di~tributed by the cutter blades, which revolve at about 1500 to 3000 r.p.m. The remaining 40 to Z0% by welght of the coal slurry filtratlon sludge are then incorporated in such a manner that sludge par-ticles of 5 to 30 mm are obtained. That operatlon must also be performed by mixers which can di~integrate coar~e lumps or clods of the coal 31urry filtration sludge. In both mixlng stages each particle whlch has been formed by the disintegra-tion of the clod of coal slurry filtration sludge must be covered by the sorbent for S0 and/or the sorbent for moisture so that 8 recombinatlon of lndividual particles to form larger agglomerate~ of fllter ~ludge w111 be avoided. A proper tlmlng of the tleatments wlll ensure that a substantislly ho-mogeneous mlxtl~re wlll be obtalned ln the flrst stage and the required disintegratlon lnto particle~ of 5 to 30 mm will be obtained in the second stage.
It wlll be particularly desirable to perform the mixing and dlsintegrating in one mixing plant. Such plant may conslst, e.g., of a horizontal cyllndrical mixer compri~ing ~:r":~
` 2~2~2~
.`
plowshares or blades rotating about a horlzontal axls and an additional inserted-tooth cutter (chopper) mounted on a separate drive shaft. The horizontal shaft should rotate at about 120 to 200 r.p.m. and the drive shaft ~or the inserted-tooth cutter at about 1500 to 3000 r.p.m. Just as in the second stage of the two-stage treatment, care must be taken to avoid an excessive disintegration or even a homogeneous mixing of the entire coal slurry filtration Yludge. A mixing for about one mlnute may be quite sufficient.
Limestone, calcium hydroxide and/or calcium oxide are particularly desirable sorbents fDr S0x. ~fecause lime-eftone will release carbon dioxide and be transformed to cal-cium oxide at the combustion temperatures employed, a pre-ferred feature of the inventlon resides in that the coal slurry filtration sludge is mixed with limestone as a sorbent for S0x.
The sorbent for moisture may be of any desired kind, provided that it has the required sorbent property. For Instance, wood meal or powderized coal may be employed. In a partlcularly desirable embodiment of the invention, coal lurry filtration sludge i9 mixed with ash from the fluidized bed. An advsntage resides, e.g., in that unreacted limestone or unreacted calcium oxide contained in the ash from the fluidized bed may be uaed as a sorbent for SDX.
If ash which comes from the fluidized bed and contains calcium oxide i9 used as a sorbent for moi~ture and/or as a sorbent for S0x, water contained in the coal slurry fil-tration sludge will be bound not only physically but also by a chemical reaction.
f'G7f ' :
The selection of the kind and optionally of the proportions of the components which are required for the production of a freely flowing product and consists of a sorbent for Sx and/or a sorbent for moisture will particularly depend on the sulfur content of the coal contained in the coal slurry filtration sludge. Virtually only a sorbent for moisture may be mixed with a coal which contains virtually no sulfur. The share of the sorbent for Sx will generally be increased with the sulfur content.
The content of the sorbent for SO should generally be so high that the sulfur content of the coal can be bound. In the determination of the rate at which the sorbent for Sx will be required the content of unreacted lime, for instance, which is contained in the ash from the fluidized bedj should be taken into account.
In processing coal slurry filtration sludge with a relatively high sulfur content it is also possible to omit an addition of sorbent for sulfur oxide and to admix only a sorbent for moisture, in particular sulfur containing powderized coal (coal dust). In that case the sulfur oxide content of the off gas is used e.g. for the production of sulfuric acid.
In a preferred embodiment of the process in accordance with the invention, in which ash from the fluidized bed is used as a sorbent for moisture and/or limestone is used as a sorbent for S0x, and assuming that the coal slurry filtration sludge has the usual moisture content of about 30 to 40% by weight the amount of coal slurry filtration sludge in the final mixture will be between limits which are determined by the ranges from 70 to 50% by weight if only ash from the fluidized bed is admixed and by the range from 30 to 50% by weight if only limestone i8 admixed. The above-mentioned statement relating to the amount of coal slurry filtration sludge in the mixture means: -i . ' , j /
2 ~ 2 ~
:.
1. If only ash from the ~luidized bed is admixed to produ~e the freely flowing product, the proportion of ash from the fluidized bed will amount to 30 to 50% by weight and the pro-portion o~ coal slurry filtrstion aludge will amount to 70 to 50% by welght.
Z. If only limestone is admixed, the proportion of limestone will amount to 50 to 70% by ~eight and the proportion of coal slurry filter ~ludge will amount to 50 to 30% by weight.
:.
1. If only ash from the ~luidized bed is admixed to produ~e the freely flowing product, the proportion of ash from the fluidized bed will amount to 30 to 50% by weight and the pro-portion o~ coal slurry filtrstion aludge will amount to 70 to 50% by welght.
Z. If only limestone is admixed, the proportion of limestone will amount to 50 to 70% by ~eight and the proportion of coal slurry filter ~ludge will amount to 50 to 30% by weight.
3. If ash from the fluid~ed bed and limestone are admixede.g. at a weight retio of 1:1, the proportion of coal slurry fll-tration sludge will be wlthin the limits of 40 and 60%
by weight and the proportion of ash from the fluidized bed and limestone will lie between the limits of 60 and 40%
by weight.
~ ccordlng to another preferred ~eature of the proces~ in accordance wlth the invention, the sQrbent For Sx and/or the sorbent ~or moisture are u~ed at the rates required for the productlon of the freely flowing product in particle ei2es between 5D and 300 ~m, preFerably with dp50 ~1~0 ~m.
Wlth such particle sizes ~he ratio of particle surface to par-ticle volume will be favourable and particularly desirable results will be obtained as regards the capacity to sorb liquid and SOx produced by the combustion in an intermediate stage.
Where ash from the fluidized bed is used, it will be particylarly desirable desirable to separate and grind the coarse fraction of the ash from the fluidized bed. In that case the ': :' .: - -~::
~'''''''..' ~2~ 8 unreacted lime which i~ abunoant in the coarse ash f'rom the fluidized bed will be exposed for the reaction with the 50x-In addition to the ~reely flowing product producedby the process in accordance with the invention, a different carbonaceou~ material, particularly coal, may be charged to the fluidized bed reactor. That concept may be embodied in a preferred embodiment o~ the invention in which sorbent for Sx at the rate required to bind the sul~ur which i9 contalned in the addltional feedstock i~ already incorporated in the freely flowing product which i9 produced. This will not af~ect the above rule for proportioning. In that case it will not be ne-ces,3ary to ~eed separate sorbent ~or 50x to the fluidized bed reactor.
The freely flowing product which has been pro-duced by the orocess in accordance with the invention dlffers from the coal slurry flltration ~ludge in thst it can be hsnd-led, e.g., on belts, and stored ln bin~. It can be fed with the conventional mechanical feeders. The heat lossea occurring in the f'uel-f'irlng plant are lower than those which are in-volved particularly ln the evaporation o~ water when the coal slurry filtration sludge 19 fed as a pumpable pulp. As a re-sult, smaller equipment can be used to produce the same power and the rate at whlch flue gas i9 produced will be decreased by about 10 to Z0%.
If sorbent for Sx 19 used at an adequate rate, about 90 to 98X of the Sx thst 19 produced by the combustion can be bound.
2 ~ J~ ~ ~
The freely flowing product of the process in accordance with the invention can be used in combustion pro-cesses which are csrried out in a so-called orthodox fluidized bed and can be used to special advantage as a feedstock in combustion processes performed in a circulating fluidized bed.
Such combustion processes performed in a circulating fluidized bed have been described, e.g., in DE-C-Z 539 546 (and the corresponding US-A-4 165 717), DE-C-Z 6Z4 30Z (and the correspond~ng U5-A-4 111 158), EP-A-0 Z06 066 (and the corresponding US-A-4 716 556), EP-A-0 Z81 165 (and the corresponding US-A-4 817 563).
', ' ~, :. . . :.. .. : : . ~
by weight and the proportion of ash from the fluidized bed and limestone will lie between the limits of 60 and 40%
by weight.
~ ccordlng to another preferred ~eature of the proces~ in accordance wlth the invention, the sQrbent For Sx and/or the sorbent ~or moisture are u~ed at the rates required for the productlon of the freely flowing product in particle ei2es between 5D and 300 ~m, preFerably with dp50 ~1~0 ~m.
Wlth such particle sizes ~he ratio of particle surface to par-ticle volume will be favourable and particularly desirable results will be obtained as regards the capacity to sorb liquid and SOx produced by the combustion in an intermediate stage.
Where ash from the fluidized bed is used, it will be particylarly desirable desirable to separate and grind the coarse fraction of the ash from the fluidized bed. In that case the ': :' .: - -~::
~'''''''..' ~2~ 8 unreacted lime which i~ abunoant in the coarse ash f'rom the fluidized bed will be exposed for the reaction with the 50x-In addition to the ~reely flowing product producedby the process in accordance with the invention, a different carbonaceou~ material, particularly coal, may be charged to the fluidized bed reactor. That concept may be embodied in a preferred embodiment o~ the invention in which sorbent for Sx at the rate required to bind the sul~ur which i9 contalned in the addltional feedstock i~ already incorporated in the freely flowing product which i9 produced. This will not af~ect the above rule for proportioning. In that case it will not be ne-ces,3ary to ~eed separate sorbent ~or 50x to the fluidized bed reactor.
The freely flowing product which has been pro-duced by the orocess in accordance with the invention dlffers from the coal slurry flltration ~ludge in thst it can be hsnd-led, e.g., on belts, and stored ln bin~. It can be fed with the conventional mechanical feeders. The heat lossea occurring in the f'uel-f'irlng plant are lower than those which are in-volved particularly ln the evaporation o~ water when the coal slurry filtration sludge 19 fed as a pumpable pulp. As a re-sult, smaller equipment can be used to produce the same power and the rate at whlch flue gas i9 produced will be decreased by about 10 to Z0%.
If sorbent for Sx 19 used at an adequate rate, about 90 to 98X of the Sx thst 19 produced by the combustion can be bound.
2 ~ J~ ~ ~
The freely flowing product of the process in accordance with the invention can be used in combustion pro-cesses which are csrried out in a so-called orthodox fluidized bed and can be used to special advantage as a feedstock in combustion processes performed in a circulating fluidized bed.
Such combustion processes performed in a circulating fluidized bed have been described, e.g., in DE-C-Z 539 546 (and the corresponding US-A-4 165 717), DE-C-Z 6Z4 30Z (and the correspond~ng U5-A-4 111 158), EP-A-0 Z06 066 (and the corresponding US-A-4 716 556), EP-A-0 Z81 165 (and the corresponding US-A-4 817 563).
', ' ~, :. . . :.. .. : : . ~
Claims (18)
1. A process of feeding coal slurry filtration sludge to be combusted in a fluidized bed reactor characterized in that coal slurry filtration sludge is mixed with fine-grained sorbent for SOx or a fine-grained sorbent for moisture in such a manner that 20 to 40% by weight of the coal slurry filtration sludge to be fed and contained in the mixture have a particle size of 5 to 30 mm and the resulting freely flowing product is fed to the fluidized bed.
2. A process according to claim 1, characterized in that coal slurry filtration sludge is mixed with limestone.
3. A process according to claim 1, characterized in that coal slurry filtration sludge is mixed with ash from the fluidized bed.
4. A process according to claim 1, 2 or 3, characterized in that sorbent for SOx sorbent for moisture is or are used at the required rates and in a particle size of 50 to 300 µm.
5. A process according to claim 1, 2 or 3, characterized in that sorbent for SOx or sorbent for moisture is or are used at the required rates and in a particle size of 50 to 300 µm, with dp50 < 180 µm.
6. A process according to claim 3, characterized in that the coarse fraction of the ash from the fluidized bed is ground and is mixed with the coal slurry filtration sludge.
7. A process according to claim 1, 2, 3 or 5, characterized in that the fluid bed reactor is charged with an additional carbonaceous material, and sorbent for SOx at the rate required to bind sulfur of the carbonaceous material charged in addition is incorporated in the freely flowing product which is produced.
8. A process according to claim 1, 2, 3 or 5, used for feeding coal slurry filtration sludge to the combustion chamber of a circulating fluidizing bed.
9. A process of feeding coal slurry filtration sludge to be combusted in a fluidized bed reactor characterized in that coal slurry filtration sludge is mixed with fine-grained sorbent for SOx and a fine-grained sorbent for moisture in such a manner that 20 to 40% by weight of the coal slurry filtration sludge to be fed and contained in the mixtrue have a particle size of S to 30 mm and the resulting freely flowing product is fed to the fluidized bed.
10. A process according to claim 9, characterized in that coal slurry filtration sludge is mixed with limestone.
11. A process according to claim 9, characterized in that coal slurry filtration sludge is mixed with ash from the fluidized bed.
12. a process according to claim 9, 10 or 11, characterized in that sorbent for SOx and sorbent for moisture are used at the required rates and in a particle size of 50 to 300 µm.
13. A process acording to claim 9, 10 or 11, characterized in that sorbent for SOx and sorbent for moisture are used at the required rates and in a particle size of 50 to 300 µm, with dp50 < 180 um.
14. A process according to claim 3, characterized in that the coarse fraction of the ash from the fluidized bed is ground and is mixed with the coal slurry filtration sludge.
15. A process according to claim 9, 10, 11 or 14, characterized in that the fluid bed reactor is charged with an additional carbonaceous material, particularly with coal, and sorbent for SOx at the rate required to bind sulfur of the carbonaceous material charged in addition is incor-porated in the freely flowing product which is produced.
16. A process according to claim 4, characterized in that the fluid bed reactor is charged with an additional carbonaceous material, particularly with coal, and sorbent for SOx at the rate required to bind sulfur of the carbonaceous material charged in addition is incorporated in the freely flowing product which is produced.
17. A process according to claim 9, 10, 11 or 14, used for feeding coal slurry filtration sludge to the combustion chamber of a circulating fluidizing bed.
18. A process according to any of claim 4, used for feeding coal slurry filtration sludge to the combustion chamber of a circulating fluidizing bed.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| DEP3933374.4 | 1989-10-06 | ||
| DE19893933374 DE3933374A1 (en) | 1989-10-06 | 1989-10-06 | METHOD FOR CHARGING CHARCOAL FILTER SLUDGE |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CA2026828A1 true CA2026828A1 (en) | 1991-04-07 |
Family
ID=6390939
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA 2026828 Abandoned CA2026828A1 (en) | 1989-10-06 | 1990-10-03 | Process of feeding coal slurry filtration sludge |
Country Status (4)
| Country | Link |
|---|---|
| EP (1) | EP0423859A1 (en) |
| AU (1) | AU6382690A (en) |
| CA (1) | CA2026828A1 (en) |
| DE (1) | DE3933374A1 (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US8382862B2 (en) | 2009-12-22 | 2013-02-26 | Re Community Energy, Llc | Sorbent containing engineered fuel feed stock |
| US8585787B2 (en) | 2012-01-26 | 2013-11-19 | Mph Energy Llc | Mitigation of harmful combustion emissions using sorbent containing engineered fuel feed stocks |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5231797A (en) * | 1991-04-19 | 1993-08-03 | Energy International Corporation | Process for treating moisture laden coal fines |
Family Cites Families (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4230460A (en) * | 1978-10-31 | 1980-10-28 | Maust Jr Edwin E | Method for enhancing the utilization of powdered coal |
| US4635572A (en) * | 1984-03-13 | 1987-01-13 | Kasa-Technoplan Gmbh | Desulfurizing of fossile fuels |
| GB2200133B (en) * | 1987-01-30 | 1989-04-05 | Allied Colloids Ltd | Coal compositions and their production |
-
1989
- 1989-10-06 DE DE19893933374 patent/DE3933374A1/en active Granted
-
1990
- 1990-09-26 EP EP90202544A patent/EP0423859A1/en not_active Withdrawn
- 1990-10-03 CA CA 2026828 patent/CA2026828A1/en not_active Abandoned
- 1990-10-05 AU AU63826/90A patent/AU6382690A/en not_active Abandoned
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US8382862B2 (en) | 2009-12-22 | 2013-02-26 | Re Community Energy, Llc | Sorbent containing engineered fuel feed stock |
| US8617264B2 (en) | 2009-12-22 | 2013-12-31 | Mph Energy Llc | Sorbent containing engineered fuel feed stock |
| US9181508B2 (en) | 2009-12-22 | 2015-11-10 | Accordant Energy, Llc | Sorbent containing engineered fuel feed stock |
| US9752086B2 (en) | 2009-12-22 | 2017-09-05 | Accordant Energy, Llc | Sorbent containing engineered fuel feed stock |
| US10563144B2 (en) | 2009-12-22 | 2020-02-18 | Accordant Energy, Llc | Sorbent containing engineered fuel feed stock |
| US8585787B2 (en) | 2012-01-26 | 2013-11-19 | Mph Energy Llc | Mitigation of harmful combustion emissions using sorbent containing engineered fuel feed stocks |
| US9487722B2 (en) | 2012-01-26 | 2016-11-08 | Accordant Energy, Llc | Mitigation of harmful combustion emissions using sorbent containing engineered fuel feed stocks |
| US10174268B2 (en) | 2012-01-26 | 2019-01-08 | Accordant Energy, Llc | Mitigation of harmful combustion emissions using sorbent containing engineered fuel feed stocks |
Also Published As
| Publication number | Publication date |
|---|---|
| DE3933374A1 (en) | 1991-04-18 |
| DE3933374C2 (en) | 1991-07-18 |
| EP0423859A1 (en) | 1991-04-24 |
| AU6382690A (en) | 1991-04-11 |
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