CA1083059A - Oven for thermal processing of lump solid fuel - Google Patents
Oven for thermal processing of lump solid fuelInfo
- Publication number
- CA1083059A CA1083059A CA249,289A CA249289A CA1083059A CA 1083059 A CA1083059 A CA 1083059A CA 249289 A CA249289 A CA 249289A CA 1083059 A CA1083059 A CA 1083059A
- Authority
- CA
- Canada
- Prior art keywords
- shaft
- low
- carbonization
- chambers
- shale
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired
Links
Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/02—Fixed-bed gasification of lump fuel
- C10J3/20—Apparatus; Plants
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B1/00—Retorts
- C10B1/02—Stationary retorts
- C10B1/04—Vertical retorts
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/02—Fixed-bed gasification of lump fuel
- C10J3/20—Apparatus; Plants
- C10J3/30—Fuel charging devices
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/72—Other features
- C10J3/74—Construction of shells or jackets
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/72—Other features
- C10J3/74—Construction of shells or jackets
- C10J3/76—Water jackets; Steam boiler-jackets
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0913—Carbonaceous raw material
- C10J2300/0946—Waste, e.g. MSW, tires, glass, tar sand, peat, paper, lignite, oil shale
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0953—Gasifying agents
- C10J2300/0956—Air or oxygen enriched air
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0953—Gasifying agents
- C10J2300/0973—Water
- C10J2300/0976—Water as steam
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0983—Additives
- C10J2300/0993—Inert particles, e.g. as heat exchange medium in a fluidized or moving bed, heat carriers, sand
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/16—Integration of gasification processes with another plant or parts within the plant
- C10J2300/1603—Integration of gasification processes with another plant or parts within the plant with gas treatment
- C10J2300/1609—Post-reduction, e.g. on a red-white-hot coke or coal bed
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Organic Chemistry (AREA)
- Combustion & Propulsion (AREA)
- Materials Engineering (AREA)
- Processing Of Solid Wastes (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
- Gasification And Melting Of Waste (AREA)
Abstract
OVEN FOR THERMAL PROCESSING OF LUMP SOLID FUEL
Abstract of the Disclosure An oven for thermal processing of lump solid fuel, low-energy oil shales in particular, which accommodates a low--temperature carbonization, a gasifying and a cooling shafts arranged one after another in said oven. The low-temperature carbonization shaft is provided with two vertical lattice partition walls subdividing said shaft along the oven axis into two low-temperature carbonization chambers, with a cham-ber for producing and distributing a heat carrier being for-med between said partition walls. This allows attaining a high degree of filling (60 - 70%) of the low-temperature car-bonization shaft volume with the shales and creates the pre-requisites for providing a high oven capacity in terms of shales (3000 - 4000 t per 24 hrs). Each of said low-tempera-ture carbonization chambers is provided with an individual gas offtake, and a discharging device enagles an individual control of the fuel descent rate in each of said chambers.
Charging devices for feeding the shales into the low-tempera-ture carbonization chambers are displaced towards the cham-ber for producing and distributing the heat carrier. This is conducive to lower carry-over of shale dust together with a steam-gas mixture from said oven.
Abstract of the Disclosure An oven for thermal processing of lump solid fuel, low-energy oil shales in particular, which accommodates a low--temperature carbonization, a gasifying and a cooling shafts arranged one after another in said oven. The low-temperature carbonization shaft is provided with two vertical lattice partition walls subdividing said shaft along the oven axis into two low-temperature carbonization chambers, with a cham-ber for producing and distributing a heat carrier being for-med between said partition walls. This allows attaining a high degree of filling (60 - 70%) of the low-temperature car-bonization shaft volume with the shales and creates the pre-requisites for providing a high oven capacity in terms of shales (3000 - 4000 t per 24 hrs). Each of said low-tempera-ture carbonization chambers is provided with an individual gas offtake, and a discharging device enagles an individual control of the fuel descent rate in each of said chambers.
Charging devices for feeding the shales into the low-tempera-ture carbonization chambers are displaced towards the cham-ber for producing and distributing the heat carrier. This is conducive to lower carry-over of shale dust together with a steam-gas mixture from said oven.
Description
~ he present i~en-tion rel~tes to thermal processing o~
solid ~uels a.nd more pi~rticularly to ovens for -the~mal pro-cessing o~ a lump solid fuel. T~e herein-proposed o~en is par-ticu'arly useful for processing low-energy oil shales.
Known in the art is an oven for processing oil shales, in which they are subjec-ted to low--tempera-ture carboniza-tion by a tra~sv0rse-upward strei~m o~ a gaseous heat carrier (see, e.gO Y~A. D nilenko~ In~e~bor's Certi~ica-te o~ -the USS~
~o. 170463, Cl.10a~ 24, 1965)o In the top portion o~ said oven is arranged low-tsmperature carbonization sha~t, includ-~i~g two vertical shale distilla-tion c~ambers, a chamber ~or produci~g i~nd distribu~ing~-the hea~ carrier ("hot" chamber~
arranged ~xially to the u~it and intermedii~e of said shale distillation chambers, and two ch.ambers ~or accumulating i~nd .
disc~i~rging of a steam-gas mIxture Ci'cold't c~ambers)~ ~hus, t~e low-temperature carbonization sha~t is subdi~ided all alont its length. by ~our ver~icial lattice paxtitio~ wall~
into ~i~e c~h~ambers, with said l~ttice partition walls being made ~rom the heat carrier inlet side o~ said low-temperatu~
re carbonization c~ambers (~rom the llhot" side) o~ a re~rac-bory material and from its outlet side (the "cold" side) o~
me-tal. .-~ ounted abo~e the chambers are inclined bar screens with slot~ spreading out to~ards the side where large limps are rolli~ down, a ~eature ensuring the supply of a co~rse .
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solid ~uels a.nd more pi~rticularly to ovens for -the~mal pro-cessing o~ a lump solid fuel. T~e herein-proposed o~en is par-ticu'arly useful for processing low-energy oil shales.
Known in the art is an oven for processing oil shales, in which they are subjec-ted to low--tempera-ture carboniza-tion by a tra~sv0rse-upward strei~m o~ a gaseous heat carrier (see, e.gO Y~A. D nilenko~ In~e~bor's Certi~ica-te o~ -the USS~
~o. 170463, Cl.10a~ 24, 1965)o In the top portion o~ said oven is arranged low-tsmperature carbonization sha~t, includ-~i~g two vertical shale distilla-tion c~ambers, a chamber ~or produci~g i~nd distribu~ing~-the hea~ carrier ("hot" chamber~
arranged ~xially to the u~it and intermedii~e of said shale distillation chambers, and two ch.ambers ~or accumulating i~nd .
disc~i~rging of a steam-gas mIxture Ci'cold't c~ambers)~ ~hus, t~e low-temperature carbonization sha~t is subdi~ided all alont its length. by ~our ver~icial lattice paxtitio~ wall~
into ~i~e c~h~ambers, with said l~ttice partition walls being made ~rom the heat carrier inlet side o~ said low-temperatu~
re carbonization c~ambers (~rom the llhot" side) o~ a re~rac-bory material and from its outlet side (the "cold" side) o~
me-tal. .-~ ounted abo~e the chambers are inclined bar screens with slot~ spreading out to~ards the side where large limps are rolli~ down, a ~eature ensuring the supply of a co~rse .
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- 2 -~raction -to the "hot" side o~ the chamber and -the supply o~
a fine fraction being handled to its '1cold" side.
The bottom portio~ o~ said ove~ accommodates a shaft ~or gasi~i~g semicoke and ~or cooling a waste residue. Here ^the process is also carried out in a transverse-up~ard flow of a gasi~ying agent~
~ he shale is c~arged b~ a special device into the top portion o~ the distillation chamber where it is subjected to low-te~perature carboniza-tion by the action o~ the heat car rier havin~ a temperature o~ 600 - 900C. r~he heat reguired for tha-t process is obtained both by burni~g some circulati~g~
gas in -the hot chamber and due to gasi~ying the semicoke in ths bo~tom portion o~ the o~en. ~e steam-ga5 mixture pro-ceeds ~rom the shale-distillation to "cold" chambers, where-~20m it iS di~c~argad at a tem~eraturè varying ~rom 150C
to 200C i~to a co~densi~g system through gas offtakes runn-ing i~ the top portio~ o~ said '7cold" chambers. ~he waste residue is dischargod b~ special devic~3s ~rom the bottom portion o~ the oven to be ~andl~3d to du~ps~
~ n important disadv~ntag~3 of the prior-art ove~ is the acaumul~tio~ o~ fine fuel ~raction~ on the "cold" side o~
t~e low-temperature carbonization c~ambexs~ ~his promotes ~igh~rate bituminization of material, resulti~g in small pieces sticking together, in the clogging o~ -the metallic lattice partition wall, and ad~ersely a~fecting t~le hea~ing o~ a ~uel bed; it o~uaes a much greaber carry-over Or shale "~ ,.
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dust toge-ther with -t~e steam-ga~ mixtu~e, wlth small ~uel particles slipping through said metallic lattice partitio~
wall -from the low-teJ~pe~ature carbonization c~ambers into those for accu~ulating a~. discharging said steam-gas mjxtu-re. Inso-~ar as the bottom portion of said chambers has no openi~s -for discharging the -fine ~uel ~ractions, it leads to their rapid overloading and, naturally, decreases the degree of u-tiliza-tion o~ ~uel organic ~a-tters. As shown b~ -practice, after 2 or 3 weeks the chambers o-~ the abo~e de-~ign are completely fillad up wi-th the m~-terial composed o~
the ~allen -~ine ~ractions o~ bot~ the shale and ssmicoke~
Aq a result, the ov~n must be shut down ~or cleani~gg tbis being a ~er~ labour-consumi~g and di~icult operation. More-o~er9 a rather great car.ry o~er o~ s~ale dust entrained by the st~am-gas mi~ture causes sexious deterioration o~ the ~ax ~ualît~3 enhanci~g its ash content.
~ hus, ~he pr~sence in the prior~art oven o~ the bar screens arranged in the top pOI~iO~ O~ the low;tempera-ture G~rbonization chambers, an~ o~ the ~IcQld~ cham~ers adapted ~or accumulati~g and disc~arging o~ the steam-gas miY~ture bu~ ha~ing ~o ope~ings in t~eir bottom portio~s ~or discharg :
: ing t~e ~ine ~uel ~ractions that have bee~ accumul~t~d the-rein7 renders t~e prior-aF~ o~en ine~ecti~e ~or industrial ~-o~sration~
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a fine fraction being handled to its '1cold" side.
The bottom portio~ o~ said ove~ accommodates a shaft ~or gasi~i~g semicoke and ~or cooling a waste residue. Here ^the process is also carried out in a transverse-up~ard flow of a gasi~ying agent~
~ he shale is c~arged b~ a special device into the top portion o~ the distillation chamber where it is subjected to low-te~perature carboniza-tion by the action o~ the heat car rier havin~ a temperature o~ 600 - 900C. r~he heat reguired for tha-t process is obtained both by burni~g some circulati~g~
gas in -the hot chamber and due to gasi~ying the semicoke in ths bo~tom portion o~ the o~en. ~e steam-ga5 mixture pro-ceeds ~rom the shale-distillation to "cold" chambers, where-~20m it iS di~c~argad at a tem~eraturè varying ~rom 150C
to 200C i~to a co~densi~g system through gas offtakes runn-ing i~ the top portio~ o~ said '7cold" chambers. ~he waste residue is dischargod b~ special devic~3s ~rom the bottom portion o~ the oven to be ~andl~3d to du~ps~
~ n important disadv~ntag~3 of the prior-art ove~ is the acaumul~tio~ o~ fine fuel ~raction~ on the "cold" side o~
t~e low-temperature carbonization c~ambexs~ ~his promotes ~igh~rate bituminization of material, resulti~g in small pieces sticking together, in the clogging o~ -the metallic lattice partition wall, and ad~ersely a~fecting t~le hea~ing o~ a ~uel bed; it o~uaes a much greaber carry-over Or shale "~ ,.
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dust toge-ther with -t~e steam-ga~ mixtu~e, wlth small ~uel particles slipping through said metallic lattice partitio~
wall -from the low-teJ~pe~ature carbonization c~ambers into those for accu~ulating a~. discharging said steam-gas mjxtu-re. Inso-~ar as the bottom portion of said chambers has no openi~s -for discharging the -fine ~uel ~ractions, it leads to their rapid overloading and, naturally, decreases the degree of u-tiliza-tion o~ ~uel organic ~a-tters. As shown b~ -practice, after 2 or 3 weeks the chambers o-~ the abo~e de-~ign are completely fillad up wi-th the m~-terial composed o~
the ~allen -~ine ~ractions o~ bot~ the shale and ssmicoke~
Aq a result, the ov~n must be shut down ~or cleani~gg tbis being a ~er~ labour-consumi~g and di~icult operation. More-o~er9 a rather great car.ry o~er o~ s~ale dust entrained by the st~am-gas mi~ture causes sexious deterioration o~ the ~ax ~ualît~3 enhanci~g its ash content.
~ hus, ~he pr~sence in the prior~art oven o~ the bar screens arranged in the top pOI~iO~ O~ the low;tempera-ture G~rbonization chambers, an~ o~ the ~IcQld~ cham~ers adapted ~or accumulati~g and disc~arging o~ the steam-gas miY~ture bu~ ha~ing ~o ope~ings in t~eir bottom portio~s ~or discharg :
: ing t~e ~ine ~uel ~ractions that have bee~ accumul~t~d the-rein7 renders t~e prior-aF~ o~en ine~ecti~e ~or industrial ~-o~sration~
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~ $ to ~he processirlg in sa:id oren with :its ~arrow fuel b~d o~ shales low l.rl organic matt~r (kerogen), which are most widel~ distributed over -the globe, it i.s il~possible at allO
In view o~ its low hydraulic resi~tance and ra*her low f`il-teri~ capacit~ of said shale a grea-t amoun-t of shale ~ust and ash are carried awa~ ~rom the o~e~ together with the steam-gas mixture9 as shown b~ practical experience, with said dust and a~h clogging the metallic lattice partition wall9 the "cold" chamber, gas o~ftake and gas path which get completely b~ocked upO
~ I~reo~er, due to a low thermal conductivity of the fuel wit~ a low organic-matter co~ent characteristic o~ the nar-row ~uel b~d are heavy lo~ses o~ heat with said steam-gas mi~*ure, which does ~ot ma~e ib possible to attai~ a high ~:
utilization degree oî the shale organic matsrial ln the low--te~Lp~rature carbonization sha~t and accou~ts ~or low tar --yield and low thermal e~icienc~ o~ ~he proces~
Owin~ to t~e; abo~-me~tio~od. disad~a~tages of the prior~
art ove~ it wa~ not appro~ed Ior us~ o~ a~ indust~ial scale. ~:
~or tke same reason~ it9 construction co~cept~ ca:~ot be uti- -lized ~or developing plants o~ a high u~it ¢apaci~ (e.g., 3000 - 4000 t o:E shale per 2~ d tl:~ose ~or processing ~il shale~ h a low organic-ma~ter co~ent, in particularO :-.. . . . .
: ~lso know~ is another oven for processing oil shale, that ~as been sucoesefully coped uvith on an in~ustrial s¢ale and :, ~ "','' ."
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',, ' ' '. ' ~ ' " ' . ':' ", ' ' ,. ~ ,. ' , ': ' '` : ' '~ ' , ' . , ". ' ', ' ' . ' . "' . . ..
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wherein low--tel~perature carboniza-~ion is e~ected in an up-ward flow o~ a ga~eous heat carrier (see, e~g-~ M~ Bersch~v-sky, ~OS.Bezmozgin, ~.S~Zaglodi~, ~.S.Sinelnikov~ Inventor's Certificate o~ the USSR ~o. 109152~ Cl. 10a7 21, 1957). An upper portion of this oven accom~odates a low tem~erature carboniza-tion sha~t, including a cham~er with an opening and a covering adaptecL ~or distribu~ing a heat carrier, sai~ -chamber being arranged insid~ the bed axiall~ to tha planto ~e cham~er rests on a roo~ -t~at separates t~e low-tempera-ture carbonization shc~t ~rom that disposed in the bottom portion of the oven~ adapted for gasi~yi~g semicok0 and -F'or .
cooling a solid residue and wherein the process is al~o car-ried ou~ in an upward flow o~ a gasi~ing agent.
he shales are charged b~ a special de~ice into the top port~on o~ t~e low-temperatuxe carbonizatio~ ~ha~t where it .
is ~ubjected to ~emicoki~g b~ the action of the heat carrier:
having a ~emperature o~ from 600 to 900C.. ~!~e heat reguired ~ox ths procs~s is obtained due to ~asi~ication o~ the semi- -co~e i~ the bottom portion o~ the o~e~. Ga~i~y~ng ~ase~ pro duced therain ~t a te~perature OI 800-1000C flow i~o the distributing chambe~ wherein air and the return circulating gas are intr4duced. From ~aid distributing chamber the heat ca~rier at a temperature of 600 - 900C is pa~ed :L~o a fuel beda a~d a steam-gas mixtur~ i~ discharged ~rom th~
low-~emperatur~ oarboniza~ion sha~t at a temperature o~
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3 ~t3~
150 - 200C i~to a condensin~ s~stem through a gas o~ta~e loca-ted in the top portio~ of said sha~tO Waste shale resi-due is discharged by a special de~ice from the bottom por~ion-o~ the o~en -to be dumped~
~ consicLerable disadvantage o~ the prior~art ov~n cous~ .
1st in that it ~ails to pro~ide a possibilit~ o~ adjusting ~ :
heat carrier di~-tribution in the fuel bed and, to be more exactl~, t~le distribution o~ heat carrier ~lows on both si-des o~ the distributing chamber. I~, b~ some reason, (e~g., ;. . .- -shale segregation, its bituminization or slagging) an addi-tional resistance originates in the ~uel bed ~rom one side of the distributing c~amber9 the entire stream o~ the heat carrier will be turned to the fuel bed disposed o~ the other ~:
side o~ said c~amber ~ s, certain portion o~ th~ ~uel bed acco~mocLated i~
the low-temperature carbor~za-tion chamber happe~ to be highly~ ~
overheatad, whereas the ot~e~ ones are underheated to a low- ; ;
-temper~ture carboniæa~io~ poi~ his resul~s l~ lowor tar yiela and deterio~ates chemical e~icienc~ o~ the process.
~ he o~en o~ ~he above design ~ails also to pro~ide a pos~ibilit~ o~ con~rol the uni~orm ~eating o~ m~terial on both sides o~ the distributing chamber, inso~ar as t~e flows .
o~ the steam-~as mi~ture, upon outcoming ~rom the -~uel bed in ~aid o~e~ sections~ intermix, with the temperatuxe in -t~e gas o~take ~ich maD be i~dlcative o~ the uni~orm heating ' ':
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o* material in particular sectlons o~' the low-~t~ ,erature carbonization shaf't) will represerlt a mean temperature o~
said flows which does not contain -the re~uisite in-~ormation on the fuel hea~irlg in said low -ternpera-ture carboniæation sha~tO In an~ case this temperature is comple-tel~ un~it -~or ascertaining operat.ively o~ what ~ide o~ the distributing chamber the ~uel bed is subjected to intense heating and where i-t is underheated.
And when said irregular heating is ~inally recognized (a~ter the normal productio~ conditions h~e been completaly disturbed with either the shales being discharged from -the o~en ~thout passi~g low-temperature carbonization or with t~e material ~ot descending in that section owing to the ~or- -mation o~ sla~ in the low-temperat~re carbonization sh~ft), the eliminatio~ o~ ~aid irregularity in the o~en o~ the a~o~e co~str~ction pre~ent a serious engineeri~g problem. Under these circumstance~, as shown b~ ~asrt industiral experience mo~t ~regue~tly the o~en m~st be shut down ~or cleaning~
~i9 iS largel~ attributed -to t~e ~act that w~ile eliminating said disturban~es it is impossible to pro~ide di~erent rates o~ ~aterial descent o~ bot~ sides o~ t~e distributi~g chamber in the lo~-te~p3ratuxe c~rbonizatio~ sha~t b~ making use o~
a ~i~gle dischargi~ device arranged in -t~e bottom portion o~
said ov~nO
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~ nd, ~nall~ said o~en su:E~ers ~rom orle ~aore disa~an-tage 9 iOe. relatively great carr~-over o~' shale dust entrai-~ad by the st~am-gas mi~ture~ ~pon dr~ing o~ in the top por-tio~ o~ the low-te~perature carbonization shaft -the shales get into the high-rate stea~-ga~ ~Qixture strea~O l~Taturall~
the ~ine-disperse dust i~ blo~n o~ -tha shale lumps and as there is no filter bed in ~ro~t o~ it7 the du~t is carried away together wi~h said mIxture into the condensing syst~m, clogging -the gas o~ftakes and conta~inating commercial tar.
~ ho a~oresaid di~advantages o~ the prior-art oven are - :
aggra~ated w~e~ its co~structional principl0s ~re utilized for developing pla~ts o~ a grea~ u~it capacit~ (e.gO, 3000 - ~ ~
~ 4000 t o~ shalo per ~ hrs instead o~ the pr~se~-aFt . :
ovens o~.the abo~e-outlined co~struction, mastered o~ a~
du~trial scale but having a cap~cit~ o~ about 150 t o~ shale per 24 hrs)0 .
~ he main object of the present in~entio~ is to provide `~
a~ o~en, w~ose de~ would ensure a ~igh capacity in term~
o~ shale7 var~ing withi~ 3000 4000 t per 24 hrsO
Another obae~t o~ the in~e~tio~ is to pro~ide a pos~i- -bilit~ of processi~g oil shales lo~ in or~n;c ma~ters~ t~at ar~ widel~ di~tributed over the globe.
~ ill anothor object of the i~e~tio~ is to provide possibilit~ of adjusti~g a~d mo~itori~g o~ ~uel bed preheat .
'', '.''',. '.' ' '' ,' ''' " " ""' ' .. ' '" ' '"'',,, . ' ~ , , ' ' '' ' " '"""',, "'' ',' ' ' ~'' "''," ' '"' ' '' '' '' ' .' '' ". ',, ' . ', '. ' ' :. ' . , :, ' ' , ' ~, , ~8~5~
in a low-temperature carbonization shaf-t with the ensui.ny increase in tar yield and a higher thermal efficiency of the process, as well as of reducing carry-over of shale dust together with a steam~gas mixture, with the resulting ex-tension of the oven run between repairs and a higher qua].ity of tar - lower ash contents, with said new oven beiny simple in terrns of its construction and reliable in serivce.
According to the invention there is provided a vertical retort for thermal processing of lump shale, comprising a body which accommodates a low-temperature carbonization shaft arranged in an upper portion of said body and having a pair of spaced apart vertically di.sposed perforated partition walls extending along said shaft dividing it into a chamber extending along the axis of the shaft adapted for supplying and distribut-ing a heat carrier, flanked by a pair of low-temperature carbonization chambers, each of said chambers having a gas off-take, charging means disposed over said shaft adapted to supply lump shale into each of said low temperature carbonization chamber~; a gasifying shaft in said body belo~ said carbonization sha~t, and supply chamb~rs for gasifying gas disposed at the p~riphery of said gasifying shaft, a cooling shaft in said body below said gasifying shaft, and a discharging device disposed below said cooling shaft having means to adjust the shale descent rate in each of said low temperature carbonization chambers and to remove solid material from a bottom part of said body, and respective means for separately discharging solid residues from the cooling shaft at respective positions below : the respective low~temperature carbonization chambers.
It is expedient that the charging means be displaced -30 with respect to the axis of each low-temperature carbonization chamber towards its "hot'` side, i.e., toward the associated partition wall.
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It is especially appropriate to have the partition walls extend along the entire height of the carbonization 3haft.
Owing to a high degree of filling of the volume of said low-temperature carbonization shaft with the shales (60-7~/o) the inherent design of said oven provides for high capacities in terms of shale -3000-4000 t per 24 hrs. The presence in each low-temperature carbonization chamber of an individual gas offtake for discharging the steam-gas mixture and a self-con-tained dis-charging device enable the process conditions to be monitored and adjusted in each chamber individually~ This creates favourable conditions for obtaining high utilization factors of the organic matters of the shales being processed, ensuring high yield of tar and a high thermal efficiency of the process.
Owing to the absence in the proposed oven of "cold"
chambers which are not provided in their bottom portions with corresponding openings for the descent of fine-disperse fuel fractions, the proposed construction features high servicing endurance and extended life between repairs.
The absence of bar screens in the top portion of the low-temperature carbonization chambers makes it possible to avoid concentration of fine fuel fractions on the "cold"
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side o~ said cha~lbers. l'lIoreover; the dis~)lac~merlt o~ the c~arging devices wi-th r~spect to -the axes o~ the low-temp3-ra-ture carbonization chambers towards the f'~ot" end o~ said chambsrs enhances -the ~iltering capacity o-~ a ~uel bed i~
: terms o~ shale dust and ~ines (with the latter being accumu-lated owin~ -to the above charging -technique on the t1hot"
side o~ -the low--temperature carbonization c~ambers)~ This provides, as s~own by in~estig~-tions, a two-three~old decre-ase in the shale dust carry-over with the stea~-gas mixture, with the ~as o~takes being blocked up with deposits not so ~uickl~ as on the prior-art ovens. As a result, the oven run between repairs is extended and tar ~ontamination wit~ so-lids ~rom said carry~over and, he~ce, its as~ conten*s di-m~ LiS~.
~ us, the herei~proposecL oven of~ers, as corapared with the prior-art units, a hig~er capacity i~ terms of ~hale ranging within 3000~4000 ~ per 24 hr~, alon~side with higher tar yield and better t~er~al e~iciency of the process; it al80 make~ i~ pos~ible to eæte~d the o~e~ run be~wee~ repa-irs an~ to o~hance the quality o~ the tar ob~ai~ed (to de~
: , .
Grea~e its a~ conteD~
he nature o~ the in~ention will be clear ~rom the fol-lowin~ detailed deacriptio~ o~ its particular embodime~t to ~i: be had in c~njunctio~ with t~e accompan~in~ dra~ing~ in .-whic~
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Fig~ ows dia~rammaticall-~ a~ o~er~ i'or ther~l proces-sing o~' lump solid ~uel (a crosa-sectional view)~ according to -the invention~ -A~ o~en f'or t~erl-aal processi~g o~ solid ~uel~ oil shales in particular, compris~s a body 1 accon~odating a low-tempe-ra-ture carbonization sha-~t 2, a gasi~ying sha~t 3 and a coo-ling sha~t 4, said sha~ts beîng ~rranged one a-~ter another along the ~eight o~ said bod~
~ he low-temperature carboniæa-tio~ s~a~t 2 is provided with two vertical lattice parti~ion walls 5 subdividing said low-temperature carbonization ~ha-~-t 2 axially to the o~en and-along its entire height into two lo~J-temperature carbo~iza-tio~ c~amber~ 6~ with a chamber 7 ~or producing a~d distri-buti~g a heat carrisr being ~o~med betwee~ said partition wall~. Owing to ~aid embodiment o~ the low-tempera-ture carbo-nization sha~t 2 its shale ~i:Lli~g degree ca~ total 60-70%S
.
thi~ allowing comparati~ely h:igh capacities i~ term~ o~ shal~
' ~ ~ he semicoke gasi~yi~g sh~t ~ a~commodates ~ide c~ambers ;~ 8 with spray ~ozzles 9 mou~ed i~ a re~ractor~ wall 10. Said ~ -: cbamber~ 8 are adapted for suppl~ing a gasii~ying agen;~ vx t~e : hea~ carrier i~to the gasi~ing sha~t 35 ~he chamber~ 7 and 8: æ ~ provided with gas bur~ers 11 and circula~i~g gaB in-}et~ 12.
."
~he ~hal~s are ~ed i~to ths o~en ~rom bi~s ~3 b~ mea~s of automQtic ch~rgi~g devioes 1~ that are provided in t~eir -: top~portion wi~h a proportioni~ slide ga-te 15 i~ their :
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,,, :. . : . : , ~8;~ 3 bottom portio~ wi-th a su~pended co.ne 16 interconnecting the charging de~ice 1~ and the top portio:ns o~ the shale di~til-lation chamber 6~ ~he chargi~g devices 14 are displaced to-wards the "ho-t" side o~ -the cham~ers 6 (~rom -the side t~ro-ugh which the heat carrier i~ ~ed in-to the ~uel bed~. ~he steam gas mixture is dischar~ed from the o~en through gas o~takes 17.
~ he sha~t 4 ~or coolin~ solid shale residue accommodates d~vices 18 *or ~eeding the cooled circulating gas and bins 19 ~or discharging solid material, said bins being disposed abov~ the cylinder-s~aped bottom o~ a licluid seal 20 with a certai~ cle~rance therebetween. The liquid seal 20 is provi-ded with a s~tem o~ gears adapted ~or pu~hi~g and discharg-ing saicl solicl residue ~rom the oven.
~ he herein-proposed oven ~or thermal processing o~ solid ~uel, oil shales in particul~r7 operates in the ~`ollowi~g 3~n~er~ ~he lump ~hale~ is ~ed from -the bi:ns 1~ b~ the char~
ging de~rices 14 displaced towards the l'hot'7 side OI tha low- ~:
-bemperaturo carbonization c~ambars 6. Wit~ the abo~e c~arg- :
ing ~ystem ~ disperse shale fractio~s are accumula~ed on the "~ot" side of said c~ambers 6 wi-th the bed :Eiltering ca-pacity being en~ ced in terms of said fractionsO ~his con- :
tributes to a~ abrupt reduction i:~ c~rry-o~er of shale du~t togeth~r with t~e steam-gas mixture ~om said oven, precludes the Iouling o:~` the ga~ o~ftakes 17 ~nd9 hence, e}~ends oven ' .
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life betwee~ repairs a~d improves the ~uali~y o~ tar (dimi-nishing its ash conte~)O I~ case the shale bei~g processed on he~ting to ~00 - 450C undergoes bituminization, said con-centration of the ~ine -Eractions on the "hot" side of -the low-temperature carbonization chambers ~ allows to avoid se-rious after-e~fects o~ said bituminization o~ the shales dur-ing semicoking (wi-th the ~i~e shale fractions, accumulat0d in low-temperature zones, being responsible :Eor ~uel bitumi- .
nization) 9 Upon passing into -the low -teI~pera-ture carboniza-tion chambers 6 the shales are ~eated by a stream of the gase-ous heat carrier having a temperature of 500 - 900C (the latter bsing depe~den~ on the ~uality of shales bei~g proces-sed), being introduced ~rom the distributing chamber 7 thro- -ugh the vertical lattice partition walls 5 and passi~g in a tra~verse-upward directio~ throu~h the shales travelling downwardsO Some ~eat carrier is produced by burning the cir-:: cul~tl~ ~as, w~i¢h takes place in the bottom portion o~ the : :chambar 7 ~or producing and diatributi~g of the ~eat carrier, said part bei~g equipped to t~is e~d wit~ the bur~ers 11 and ga~ inlsts 12. By ~ar~ing the gas ~lowrate it is possible to eep the temperature o~ said ~eat carrier at a prescribed le-: ~el. ~e remaining heat carrier is ~ed from the gasi~y~ng sha~t 3. ~ :~
: ~he presence o~ a r~ther large ~uel bed (in the direction o~ heat carrler flow) in the low-temperature carbonization ckambers ~ craate~ ~n increased hydraulic resistance and , ~ ~ :
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~Q8~9 enharlces -the ~ tering capacit~ o~ the bed, this ~r oviding ~avourable conditions ~or louJ-te~perat;ure carbonization of the shales low in organic ma-kters, w~ich are widely spread over the globe~ .A higher hydraulic resis-tance o~' the ~uel bed ensures more uniform distribution of the heat carrier inside the bed and, hence~ irnproves heat trans-fer, this being conduci~e to hi~her tar yields and better thermal e~iciency of the process~
At the same time it enha~ces t~e ~'iltering capacit~ o~
said bed which also contributes to a reduction in s~ale dust carr~-o~er from t~e oven together with the s-team-gas mIxture.
Said st~am-gas mixture is discharged at a ~ empe - -rature o~ 150 - 200C ~rom the low-te~perature carbonization sha~t.6 through th~ gas o~takes 17. ~he use in eac~ o~ said chambers 6 of an individual gas of~take 17 enables a conti~
nuous control o~ technological condi~ions during shale semi-coking in said chambers~(depending on the temperatures o~ the steam-gas mixture in tha gas of~takes).
SemiGoke passes ~rom the low-temperature carbonizatio~
chambers 6 into t~e shaft 3 for gasi~in~ vr additio~al heak-ing b~ in~roducing accordingl~ eit~er a gasifying age~t (a steam-air, ga~-air or smo~e-air ~ and, possibly, ~lue gases) or a heat carrier (a mixture of flue gases and the oir~ulati~ cooled gas) ~rom the side cha~ber~ 8 provided with the burners 11 and circulating gas inlets 12 a~d with st~am iIllet~, li r~quirod (not show~ i~ the drawing).
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Gas streams proceed from the sha~'t 3 to both -the c~nber 7 for producing and distributing o~ the heat carrier and directly into the ~uel ~ed i~ the semicocking ch~ers 6, ensuring thereby uni~orm heating o-~ the fuelO The most ~ou-rable operating condi-tions of -the ~haft 3 ar~ selected expe-rimentall~0 ~ he ~olid residue is passed ~rom the shaft 3 into t~e cooling sha-~t 4 where it cools o~-~ to a temperature of 80 -100C by the circulating gas fed through the devices 180 Next it proceeds further i~to the bins 19 and water seals 20, where~rom it is discharged by the pushing g~ar~ onto conve~-i~g de~ices to be handled to ash dumps~
Owing to the i~dividual discharging device that is provi-:~
ded in each low-temperature carboni2ation chamber 6 the ~uel.
descending rate can be adjusted in each chamber 6 independen-tl~. In combin~tion with indi.~idual gas offtakes 17 mounted in each chamber 6 it af~ords the possibility o~ monitoring ~.
a~d adjusting t~e technical regime while distilling the sha-le~ in the semicocking sha~t 6~ t~is creating ~avourable pre-.:
requisites ~or bo~h high tar yield and impro~ed thermal e~fi-! cienc~ of the preoess~
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:
~ $ to ~he processirlg in sa:id oren with :its ~arrow fuel b~d o~ shales low l.rl organic matt~r (kerogen), which are most widel~ distributed over -the globe, it i.s il~possible at allO
In view o~ its low hydraulic resi~tance and ra*her low f`il-teri~ capacit~ of said shale a grea-t amoun-t of shale ~ust and ash are carried awa~ ~rom the o~e~ together with the steam-gas mixture9 as shown b~ practical experience, with said dust and a~h clogging the metallic lattice partition wall9 the "cold" chamber, gas o~ftake and gas path which get completely b~ocked upO
~ I~reo~er, due to a low thermal conductivity of the fuel wit~ a low organic-matter co~ent characteristic o~ the nar-row ~uel b~d are heavy lo~ses o~ heat with said steam-gas mi~*ure, which does ~ot ma~e ib possible to attai~ a high ~:
utilization degree oî the shale organic matsrial ln the low--te~Lp~rature carbonization sha~t and accou~ts ~or low tar --yield and low thermal e~icienc~ o~ ~he proces~
Owin~ to t~e; abo~-me~tio~od. disad~a~tages of the prior~
art ove~ it wa~ not appro~ed Ior us~ o~ a~ indust~ial scale. ~:
~or tke same reason~ it9 construction co~cept~ ca:~ot be uti- -lized ~or developing plants o~ a high u~it ¢apaci~ (e.g., 3000 - 4000 t o:E shale per 2~ d tl:~ose ~or processing ~il shale~ h a low organic-ma~ter co~ent, in particularO :-.. . . . .
: ~lso know~ is another oven for processing oil shale, that ~as been sucoesefully coped uvith on an in~ustrial s¢ale and :, ~ "','' ."
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wherein low--tel~perature carboniza-~ion is e~ected in an up-ward flow o~ a ga~eous heat carrier (see, e~g-~ M~ Bersch~v-sky, ~OS.Bezmozgin, ~.S~Zaglodi~, ~.S.Sinelnikov~ Inventor's Certificate o~ the USSR ~o. 109152~ Cl. 10a7 21, 1957). An upper portion of this oven accom~odates a low tem~erature carboniza-tion sha~t, including a cham~er with an opening and a covering adaptecL ~or distribu~ing a heat carrier, sai~ -chamber being arranged insid~ the bed axiall~ to tha planto ~e cham~er rests on a roo~ -t~at separates t~e low-tempera-ture carbonization shc~t ~rom that disposed in the bottom portion of the oven~ adapted for gasi~yi~g semicok0 and -F'or .
cooling a solid residue and wherein the process is al~o car-ried ou~ in an upward flow o~ a gasi~ing agent.
he shales are charged b~ a special de~ice into the top port~on o~ t~e low-temperatuxe carbonizatio~ ~ha~t where it .
is ~ubjected to ~emicoki~g b~ the action of the heat carrier:
having a ~emperature o~ from 600 to 900C.. ~!~e heat reguired ~ox ths procs~s is obtained due to ~asi~ication o~ the semi- -co~e i~ the bottom portion o~ the o~e~. Ga~i~y~ng ~ase~ pro duced therain ~t a te~perature OI 800-1000C flow i~o the distributing chambe~ wherein air and the return circulating gas are intr4duced. From ~aid distributing chamber the heat ca~rier at a temperature of 600 - 900C is pa~ed :L~o a fuel beda a~d a steam-gas mixtur~ i~ discharged ~rom th~
low-~emperatur~ oarboniza~ion sha~t at a temperature o~
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3 ~t3~
150 - 200C i~to a condensin~ s~stem through a gas o~ta~e loca-ted in the top portio~ of said sha~tO Waste shale resi-due is discharged by a special de~ice from the bottom por~ion-o~ the o~en -to be dumped~
~ consicLerable disadvantage o~ the prior~art ov~n cous~ .
1st in that it ~ails to pro~ide a possibilit~ o~ adjusting ~ :
heat carrier di~-tribution in the fuel bed and, to be more exactl~, t~le distribution o~ heat carrier ~lows on both si-des o~ the distributing chamber. I~, b~ some reason, (e~g., ;. . .- -shale segregation, its bituminization or slagging) an addi-tional resistance originates in the ~uel bed ~rom one side of the distributing c~amber9 the entire stream o~ the heat carrier will be turned to the fuel bed disposed o~ the other ~:
side o~ said c~amber ~ s, certain portion o~ th~ ~uel bed acco~mocLated i~
the low-temperature carbor~za-tion chamber happe~ to be highly~ ~
overheatad, whereas the ot~e~ ones are underheated to a low- ; ;
-temper~ture carboniæa~io~ poi~ his resul~s l~ lowor tar yiela and deterio~ates chemical e~icienc~ o~ the process.
~ he o~en o~ ~he above design ~ails also to pro~ide a pos~ibilit~ o~ con~rol the uni~orm ~eating o~ m~terial on both sides o~ the distributing chamber, inso~ar as t~e flows .
o~ the steam-~as mi~ture, upon outcoming ~rom the -~uel bed in ~aid o~e~ sections~ intermix, with the temperatuxe in -t~e gas o~take ~ich maD be i~dlcative o~ the uni~orm heating ' ':
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o* material in particular sectlons o~' the low-~t~ ,erature carbonization shaf't) will represerlt a mean temperature o~
said flows which does not contain -the re~uisite in-~ormation on the fuel hea~irlg in said low -ternpera-ture carboniæation sha~tO In an~ case this temperature is comple-tel~ un~it -~or ascertaining operat.ively o~ what ~ide o~ the distributing chamber the ~uel bed is subjected to intense heating and where i-t is underheated.
And when said irregular heating is ~inally recognized (a~ter the normal productio~ conditions h~e been completaly disturbed with either the shales being discharged from -the o~en ~thout passi~g low-temperature carbonization or with t~e material ~ot descending in that section owing to the ~or- -mation o~ sla~ in the low-temperat~re carbonization sh~ft), the eliminatio~ o~ ~aid irregularity in the o~en o~ the a~o~e co~str~ction pre~ent a serious engineeri~g problem. Under these circumstance~, as shown b~ ~asrt industiral experience mo~t ~regue~tly the o~en m~st be shut down ~or cleaning~
~i9 iS largel~ attributed -to t~e ~act that w~ile eliminating said disturban~es it is impossible to pro~ide di~erent rates o~ ~aterial descent o~ bot~ sides o~ t~e distributi~g chamber in the lo~-te~p3ratuxe c~rbonizatio~ sha~t b~ making use o~
a ~i~gle dischargi~ device arranged in -t~e bottom portion o~
said ov~nO
., :
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~ nd, ~nall~ said o~en su:E~ers ~rom orle ~aore disa~an-tage 9 iOe. relatively great carr~-over o~' shale dust entrai-~ad by the st~am-gas mi~ture~ ~pon dr~ing o~ in the top por-tio~ o~ the low-te~perature carbonization shaft -the shales get into the high-rate stea~-ga~ ~Qixture strea~O l~Taturall~
the ~ine-disperse dust i~ blo~n o~ -tha shale lumps and as there is no filter bed in ~ro~t o~ it7 the du~t is carried away together wi~h said mIxture into the condensing syst~m, clogging -the gas o~ftakes and conta~inating commercial tar.
~ ho a~oresaid di~advantages o~ the prior-art oven are - :
aggra~ated w~e~ its co~structional principl0s ~re utilized for developing pla~ts o~ a grea~ u~it capacit~ (e.gO, 3000 - ~ ~
~ 4000 t o~ shalo per ~ hrs instead o~ the pr~se~-aFt . :
ovens o~.the abo~e-outlined co~struction, mastered o~ a~
du~trial scale but having a cap~cit~ o~ about 150 t o~ shale per 24 hrs)0 .
~ he main object of the present in~entio~ is to provide `~
a~ o~en, w~ose de~ would ensure a ~igh capacity in term~
o~ shale7 var~ing withi~ 3000 4000 t per 24 hrsO
Another obae~t o~ the in~e~tio~ is to pro~ide a pos~i- -bilit~ of processi~g oil shales lo~ in or~n;c ma~ters~ t~at ar~ widel~ di~tributed over the globe.
~ ill anothor object of the i~e~tio~ is to provide possibilit~ of adjusti~g a~d mo~itori~g o~ ~uel bed preheat .
'', '.''',. '.' ' '' ,' ''' " " ""' ' .. ' '" ' '"'',,, . ' ~ , , ' ' '' ' " '"""',, "'' ',' ' ' ~'' "''," ' '"' ' '' '' '' ' .' '' ". ',, ' . ', '. ' ' :. ' . , :, ' ' , ' ~, , ~8~5~
in a low-temperature carbonization shaf-t with the ensui.ny increase in tar yield and a higher thermal efficiency of the process, as well as of reducing carry-over of shale dust together with a steam~gas mixture, with the resulting ex-tension of the oven run between repairs and a higher qua].ity of tar - lower ash contents, with said new oven beiny simple in terrns of its construction and reliable in serivce.
According to the invention there is provided a vertical retort for thermal processing of lump shale, comprising a body which accommodates a low-temperature carbonization shaft arranged in an upper portion of said body and having a pair of spaced apart vertically di.sposed perforated partition walls extending along said shaft dividing it into a chamber extending along the axis of the shaft adapted for supplying and distribut-ing a heat carrier, flanked by a pair of low-temperature carbonization chambers, each of said chambers having a gas off-take, charging means disposed over said shaft adapted to supply lump shale into each of said low temperature carbonization chamber~; a gasifying shaft in said body belo~ said carbonization sha~t, and supply chamb~rs for gasifying gas disposed at the p~riphery of said gasifying shaft, a cooling shaft in said body below said gasifying shaft, and a discharging device disposed below said cooling shaft having means to adjust the shale descent rate in each of said low temperature carbonization chambers and to remove solid material from a bottom part of said body, and respective means for separately discharging solid residues from the cooling shaft at respective positions below : the respective low~temperature carbonization chambers.
It is expedient that the charging means be displaced -30 with respect to the axis of each low-temperature carbonization chamber towards its "hot'` side, i.e., toward the associated partition wall.
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It is especially appropriate to have the partition walls extend along the entire height of the carbonization 3haft.
Owing to a high degree of filling of the volume of said low-temperature carbonization shaft with the shales (60-7~/o) the inherent design of said oven provides for high capacities in terms of shale -3000-4000 t per 24 hrs. The presence in each low-temperature carbonization chamber of an individual gas offtake for discharging the steam-gas mixture and a self-con-tained dis-charging device enable the process conditions to be monitored and adjusted in each chamber individually~ This creates favourable conditions for obtaining high utilization factors of the organic matters of the shales being processed, ensuring high yield of tar and a high thermal efficiency of the process.
Owing to the absence in the proposed oven of "cold"
chambers which are not provided in their bottom portions with corresponding openings for the descent of fine-disperse fuel fractions, the proposed construction features high servicing endurance and extended life between repairs.
The absence of bar screens in the top portion of the low-temperature carbonization chambers makes it possible to avoid concentration of fine fuel fractions on the "cold"
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side o~ said cha~lbers. l'lIoreover; the dis~)lac~merlt o~ the c~arging devices wi-th r~spect to -the axes o~ the low-temp3-ra-ture carbonization chambers towards the f'~ot" end o~ said chambsrs enhances -the ~iltering capacity o-~ a ~uel bed i~
: terms o~ shale dust and ~ines (with the latter being accumu-lated owin~ -to the above charging -technique on the t1hot"
side o~ -the low--temperature carbonization c~ambers)~ This provides, as s~own by in~estig~-tions, a two-three~old decre-ase in the shale dust carry-over with the stea~-gas mixture, with the ~as o~takes being blocked up with deposits not so ~uickl~ as on the prior-art ovens. As a result, the oven run between repairs is extended and tar ~ontamination wit~ so-lids ~rom said carry~over and, he~ce, its as~ conten*s di-m~ LiS~.
~ us, the herei~proposecL oven of~ers, as corapared with the prior-art units, a hig~er capacity i~ terms of ~hale ranging within 3000~4000 ~ per 24 hr~, alon~side with higher tar yield and better t~er~al e~iciency of the process; it al80 make~ i~ pos~ible to eæte~d the o~e~ run be~wee~ repa-irs an~ to o~hance the quality o~ the tar ob~ai~ed (to de~
: , .
Grea~e its a~ conteD~
he nature o~ the in~ention will be clear ~rom the fol-lowin~ detailed deacriptio~ o~ its particular embodime~t to ~i: be had in c~njunctio~ with t~e accompan~in~ dra~ing~ in .-whic~
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~ ~2 ~
Fig~ ows dia~rammaticall-~ a~ o~er~ i'or ther~l proces-sing o~' lump solid ~uel (a crosa-sectional view)~ according to -the invention~ -A~ o~en f'or t~erl-aal processi~g o~ solid ~uel~ oil shales in particular, compris~s a body 1 accon~odating a low-tempe-ra-ture carbonization sha-~t 2, a gasi~ying sha~t 3 and a coo-ling sha~t 4, said sha~ts beîng ~rranged one a-~ter another along the ~eight o~ said bod~
~ he low-temperature carboniæa-tio~ s~a~t 2 is provided with two vertical lattice parti~ion walls 5 subdividing said low-temperature carbonization ~ha-~-t 2 axially to the o~en and-along its entire height into two lo~J-temperature carbo~iza-tio~ c~amber~ 6~ with a chamber 7 ~or producing a~d distri-buti~g a heat carrisr being ~o~med betwee~ said partition wall~. Owing to ~aid embodiment o~ the low-tempera-ture carbo-nization sha~t 2 its shale ~i:Lli~g degree ca~ total 60-70%S
.
thi~ allowing comparati~ely h:igh capacities i~ term~ o~ shal~
' ~ ~ he semicoke gasi~yi~g sh~t ~ a~commodates ~ide c~ambers ;~ 8 with spray ~ozzles 9 mou~ed i~ a re~ractor~ wall 10. Said ~ -: cbamber~ 8 are adapted for suppl~ing a gasii~ying agen;~ vx t~e : hea~ carrier i~to the gasi~ing sha~t 35 ~he chamber~ 7 and 8: æ ~ provided with gas bur~ers 11 and circula~i~g gaB in-}et~ 12.
."
~he ~hal~s are ~ed i~to ths o~en ~rom bi~s ~3 b~ mea~s of automQtic ch~rgi~g devioes 1~ that are provided in t~eir -: top~portion wi~h a proportioni~ slide ga-te 15 i~ their :
' ~ . ~ .
~' ~
j , ,;
,,, :. . : . : , ~8;~ 3 bottom portio~ wi-th a su~pended co.ne 16 interconnecting the charging de~ice 1~ and the top portio:ns o~ the shale di~til-lation chamber 6~ ~he chargi~g devices 14 are displaced to-wards the "ho-t" side o~ -the cham~ers 6 (~rom -the side t~ro-ugh which the heat carrier i~ ~ed in-to the ~uel bed~. ~he steam gas mixture is dischar~ed from the o~en through gas o~takes 17.
~ he sha~t 4 ~or coolin~ solid shale residue accommodates d~vices 18 *or ~eeding the cooled circulating gas and bins 19 ~or discharging solid material, said bins being disposed abov~ the cylinder-s~aped bottom o~ a licluid seal 20 with a certai~ cle~rance therebetween. The liquid seal 20 is provi-ded with a s~tem o~ gears adapted ~or pu~hi~g and discharg-ing saicl solicl residue ~rom the oven.
~ he herein-proposed oven ~or thermal processing o~ solid ~uel, oil shales in particul~r7 operates in the ~`ollowi~g 3~n~er~ ~he lump ~hale~ is ~ed from -the bi:ns 1~ b~ the char~
ging de~rices 14 displaced towards the l'hot'7 side OI tha low- ~:
-bemperaturo carbonization c~ambars 6. Wit~ the abo~e c~arg- :
ing ~ystem ~ disperse shale fractio~s are accumula~ed on the "~ot" side of said c~ambers 6 wi-th the bed :Eiltering ca-pacity being en~ ced in terms of said fractionsO ~his con- :
tributes to a~ abrupt reduction i:~ c~rry-o~er of shale du~t togeth~r with t~e steam-gas mixture ~om said oven, precludes the Iouling o:~` the ga~ o~ftakes 17 ~nd9 hence, e}~ends oven ' .
'.'`
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;...... . ~, ~ . , - . . ., , . ~,. .
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, - .. . . .
~L~8~
life betwee~ repairs a~d improves the ~uali~y o~ tar (dimi-nishing its ash conte~)O I~ case the shale bei~g processed on he~ting to ~00 - 450C undergoes bituminization, said con-centration of the ~ine -Eractions on the "hot" side of -the low-temperature carbonization chambers ~ allows to avoid se-rious after-e~fects o~ said bituminization o~ the shales dur-ing semicoking (wi-th the ~i~e shale fractions, accumulat0d in low-temperature zones, being responsible :Eor ~uel bitumi- .
nization) 9 Upon passing into -the low -teI~pera-ture carboniza-tion chambers 6 the shales are ~eated by a stream of the gase-ous heat carrier having a temperature of 500 - 900C (the latter bsing depe~den~ on the ~uality of shales bei~g proces-sed), being introduced ~rom the distributing chamber 7 thro- -ugh the vertical lattice partition walls 5 and passi~g in a tra~verse-upward directio~ throu~h the shales travelling downwardsO Some ~eat carrier is produced by burning the cir-:: cul~tl~ ~as, w~i¢h takes place in the bottom portion o~ the : :chambar 7 ~or producing and diatributi~g of the ~eat carrier, said part bei~g equipped to t~is e~d wit~ the bur~ers 11 and ga~ inlsts 12. By ~ar~ing the gas ~lowrate it is possible to eep the temperature o~ said ~eat carrier at a prescribed le-: ~el. ~e remaining heat carrier is ~ed from the gasi~y~ng sha~t 3. ~ :~
: ~he presence o~ a r~ther large ~uel bed (in the direction o~ heat carrler flow) in the low-temperature carbonization ckambers ~ craate~ ~n increased hydraulic resistance and , ~ ~ :
;: ' , .:
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:~ , :
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, . .. . . .
~Q8~9 enharlces -the ~ tering capacit~ o~ the bed, this ~r oviding ~avourable conditions ~or louJ-te~perat;ure carbonization of the shales low in organic ma-kters, w~ich are widely spread over the globe~ .A higher hydraulic resis-tance o~' the ~uel bed ensures more uniform distribution of the heat carrier inside the bed and, hence~ irnproves heat trans-fer, this being conduci~e to hi~her tar yields and better thermal e~iciency of the process~
At the same time it enha~ces t~e ~'iltering capacit~ o~
said bed which also contributes to a reduction in s~ale dust carr~-o~er from t~e oven together with the s-team-gas mIxture.
Said st~am-gas mixture is discharged at a ~ empe - -rature o~ 150 - 200C ~rom the low-te~perature carbonization sha~t.6 through th~ gas o~takes 17. ~he use in eac~ o~ said chambers 6 of an individual gas of~take 17 enables a conti~
nuous control o~ technological condi~ions during shale semi-coking in said chambers~(depending on the temperatures o~ the steam-gas mixture in tha gas of~takes).
SemiGoke passes ~rom the low-temperature carbonizatio~
chambers 6 into t~e shaft 3 for gasi~in~ vr additio~al heak-ing b~ in~roducing accordingl~ eit~er a gasifying age~t (a steam-air, ga~-air or smo~e-air ~ and, possibly, ~lue gases) or a heat carrier (a mixture of flue gases and the oir~ulati~ cooled gas) ~rom the side cha~ber~ 8 provided with the burners 11 and circulating gas inlets 12 a~d with st~am iIllet~, li r~quirod (not show~ i~ the drawing).
:
:
:: ~
.
~.o~r3~
Gas streams proceed from the sha~'t 3 to both -the c~nber 7 for producing and distributing o~ the heat carrier and directly into the ~uel ~ed i~ the semicocking ch~ers 6, ensuring thereby uni~orm heating o-~ the fuelO The most ~ou-rable operating condi-tions of -the ~haft 3 ar~ selected expe-rimentall~0 ~ he ~olid residue is passed ~rom the shaft 3 into t~e cooling sha-~t 4 where it cools o~-~ to a temperature of 80 -100C by the circulating gas fed through the devices 180 Next it proceeds further i~to the bins 19 and water seals 20, where~rom it is discharged by the pushing g~ar~ onto conve~-i~g de~ices to be handled to ash dumps~
Owing to the i~dividual discharging device that is provi-:~
ded in each low-temperature carboni2ation chamber 6 the ~uel.
descending rate can be adjusted in each chamber 6 independen-tl~. In combin~tion with indi.~idual gas offtakes 17 mounted in each chamber 6 it af~ords the possibility o~ monitoring ~.
a~d adjusting t~e technical regime while distilling the sha-le~ in the semicocking sha~t 6~ t~is creating ~avourable pre-.:
requisites ~or bo~h high tar yield and impro~ed thermal e~fi-! cienc~ of the preoess~
`:
' ': :
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:
Claims (5)
1. A vertical retort for thermal processing of lump shale, comprising a body which accommodates a low-temperature carbonization shaft arranged in an upper portion of said body and having a pair of spaced apart vertically disposed perforated partition walls extending along said shaft and dividing it into a chamber extending along the axis of the shaft adapted for supplying and distributing a heat carrier, flanked by a pair of low-temperature carbonization chamb-ers, each of said carbonization chambers having a gas off-take, charging means disposed over said shaft adapted to supply lump shale into each of said low temperature carbonization chambers;
a gasifying shaft in said body below said carbonization shaft, and supply chambers for gasifying gas disposed at the periphery of said gasifying shaft;
a cooling shaft in said body below said gasifying shaft;
and a discharging device disposed below said cooling shaft having means to adjust the shale descent rate in each of said low temperature carbonization chambers and to remove solid material from a bottom part of said body, and respective means for separately discharging solid residues from the cooling shaft at respective positions below the respective low-temperature carbonization chambers.
a gasifying shaft in said body below said carbonization shaft, and supply chambers for gasifying gas disposed at the periphery of said gasifying shaft;
a cooling shaft in said body below said gasifying shaft;
and a discharging device disposed below said cooling shaft having means to adjust the shale descent rate in each of said low temperature carbonization chambers and to remove solid material from a bottom part of said body, and respective means for separately discharging solid residues from the cooling shaft at respective positions below the respective low-temperature carbonization chambers.
2. A retort as claimed in claim 1, in which the charging means is adapted to feed shale into each carbonization chamber at a position which is displaced with respect to the median axis of each carbonization chamber toward the associated partition wall.
3. A retort as claimed in claim 1, in which said partition walls extend along the entire height of said carbonization shaft.
4. A retort as claimed in claim 1, 2 or 3, wherein said chamber for supplying and distributing a heat carrier is generally centrally disposed in said carbonization shaft
5. A vertical retort for thermal processing of lump shale, comprising a body which accommodates a low-temperature carbonization shaft arranged in an upper portion of said body and having a pair of spaced apart vertically disposed perforated partition walls extending along the entire height of said shaft and dividing it into a supply chamber extending along the axis of the shaft, flanked by a pair of low-temperature carbonization chambers, each of said carbonization chambers having a gas off-take, said supply chamber being adapted to supply and distribute a heat carrier in a transverse upward direction through said carbonization chambers, charging means disposed over said shaft adapted to supply lump shale into each of said low temperature carbonization chambers adapted to feed shale into each carbonization chamber at a position which is displaced with respect to the median axis of each carbonization chamber toward the associated partition wall, a gasifying shaft in said body below said carbonization shaft, and supply chambers for gasifying gas or heat carrier disposed at the periphery of said gasifying shaft, a cooling shaft in said body below said gasifying shaft, and a discharging device disposed below said cooling shaft having means to adjust the shale descent rate in each of said low temperature carbonization chambers and to remove solid material from a bottom part of said body, and respective means for separately discharging solid residues from the cooling shaft at respective positions below the respective low-temperature carbonization chambers.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| SU2118204 | 1975-04-01 | ||
| SU2118204 | 1975-04-01 |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CA1083059A true CA1083059A (en) | 1980-08-05 |
Family
ID=20614212
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA249,289A Expired CA1083059A (en) | 1975-04-01 | 1976-03-31 | Oven for thermal processing of lump solid fuel |
Country Status (9)
| Country | Link |
|---|---|
| AU (1) | AU498283B2 (en) |
| BG (1) | BG27640A1 (en) |
| BR (1) | BR7601992A (en) |
| CA (1) | CA1083059A (en) |
| GB (1) | GB1491645A (en) |
| NL (1) | NL167191C (en) |
| OA (1) | OA05306A (en) |
| SE (1) | SE410976B (en) |
| YU (1) | YU40645B (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105018116A (en) * | 2015-07-08 | 2015-11-04 | 中国矿业大学(北京) | Pyrolysis method for low-rank coal or oil shale with higher tar yield |
Families Citing this family (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| FR2544737B1 (en) * | 1983-04-21 | 1987-11-27 | Duchene Paul | BITUMINOUS SHALE TREATMENT OVEN |
| US6800113B2 (en) | 2001-06-28 | 2004-10-05 | Startec Iron Llc | Equipment for distribution and feeding of charge and fuel in shaft furnaces of rectangular cross section |
| DE202006009174U1 (en) * | 2006-06-08 | 2007-10-11 | Rudolf Hörmann GmbH & Co. KG | Apparatus for producing fuel gas from a solid fuel |
| CN102746864A (en) * | 2012-07-23 | 2012-10-24 | 李柯 | Gas heat carrier multifunctional round furnace |
| CN113416562B (en) * | 2021-07-16 | 2022-07-05 | 中煤能源研究院有限责任公司 | Oxygen-enriched low-carbon pyrolysis system utilizing boiler flue gas and using method |
-
1976
- 1976-03-30 YU YU826/76A patent/YU40645B/en unknown
- 1976-03-30 NL NL7603310.A patent/NL167191C/en not_active IP Right Cessation
- 1976-03-31 SE SE7603833A patent/SE410976B/en not_active IP Right Cessation
- 1976-03-31 CA CA249,289A patent/CA1083059A/en not_active Expired
- 1976-03-31 AU AU12538/76A patent/AU498283B2/en not_active Expired
- 1976-04-01 BR BR7601992A patent/BR7601992A/en unknown
- 1976-04-01 GB GB13319/76A patent/GB1491645A/en not_active Expired
- 1976-04-01 BG BG7632771A patent/BG27640A1/en unknown
- 1976-04-15 OA OA55801A patent/OA05306A/en unknown
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105018116A (en) * | 2015-07-08 | 2015-11-04 | 中国矿业大学(北京) | Pyrolysis method for low-rank coal or oil shale with higher tar yield |
Also Published As
| Publication number | Publication date |
|---|---|
| BR7601992A (en) | 1976-10-05 |
| SE410976B (en) | 1979-11-19 |
| NL167191C (en) | 1981-11-16 |
| OA05306A (en) | 1981-02-28 |
| AU1253876A (en) | 1977-10-06 |
| NL7603310A (en) | 1976-10-05 |
| GB1491645A (en) | 1977-11-09 |
| BG27640A1 (en) | 1979-12-12 |
| AU498283B2 (en) | 1979-03-01 |
| SE7603833L (en) | 1976-10-02 |
| YU40645B (en) | 1986-04-30 |
| NL167191B (en) | 1981-06-16 |
| YU82676A (en) | 1983-01-21 |
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