CA1054088A - Process for continuous coking of peat, bovey coal and wood - Google Patents
Process for continuous coking of peat, bovey coal and woodInfo
- Publication number
- CA1054088A CA1054088A CA219,803A CA219803A CA1054088A CA 1054088 A CA1054088 A CA 1054088A CA 219803 A CA219803 A CA 219803A CA 1054088 A CA1054088 A CA 1054088A
- Authority
- CA
- Canada
- Prior art keywords
- particles
- reaction chamber
- coked
- gases
- peat
- 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
- 238000000034 method Methods 0.000 title claims abstract description 26
- 239000003415 peat Substances 0.000 title claims abstract description 16
- 238000004939 coking Methods 0.000 title claims abstract description 12
- 239000003245 coal Substances 0.000 title claims abstract description 11
- 239000002023 wood Substances 0.000 title claims abstract description 8
- 239000007789 gas Substances 0.000 claims abstract description 53
- 239000002245 particle Substances 0.000 claims abstract description 36
- 238000006243 chemical reaction Methods 0.000 claims abstract description 21
- 238000010438 heat treatment Methods 0.000 claims abstract description 13
- 238000001816 cooling Methods 0.000 claims abstract description 5
- 238000003756 stirring Methods 0.000 claims abstract 2
- 239000000463 material Substances 0.000 description 17
- 239000000571 coke Substances 0.000 description 14
- 239000000779 smoke Substances 0.000 description 12
- 239000011343 solid material Substances 0.000 description 9
- 238000003763 carbonization Methods 0.000 description 7
- 239000002956 ash Substances 0.000 description 4
- 239000000428 dust Substances 0.000 description 4
- 239000011269 tar Substances 0.000 description 4
- 239000003039 volatile agent Substances 0.000 description 4
- 238000001035 drying Methods 0.000 description 3
- 239000000203 mixture Substances 0.000 description 3
- 230000003647 oxidation Effects 0.000 description 3
- 238000007254 oxidation reaction Methods 0.000 description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 3
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 2
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 2
- 229910052799 carbon Inorganic materials 0.000 description 2
- 239000003610 charcoal Substances 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 239000011368 organic material Substances 0.000 description 2
- 230000005855 radiation Effects 0.000 description 2
- 230000001105 regulatory effect Effects 0.000 description 2
- 239000007787 solid Substances 0.000 description 2
- 235000002918 Fraxinus excelsior Nutrition 0.000 description 1
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- 239000012298 atmosphere Substances 0.000 description 1
- 238000005422 blasting Methods 0.000 description 1
- 239000001273 butane Substances 0.000 description 1
- 229910002092 carbon dioxide Inorganic materials 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 239000011261 inert gas Substances 0.000 description 1
- IJDNQMDRQITEOD-UHFFFAOYSA-N n-butane Chemical compound CCCC IJDNQMDRQITEOD-UHFFFAOYSA-N 0.000 description 1
- OFBQJSOFQDEBGM-UHFFFAOYSA-N n-pentane Natural products CCCCC OFBQJSOFQDEBGM-UHFFFAOYSA-N 0.000 description 1
- 239000004058 oil shale Substances 0.000 description 1
- 150000002989 phenols Chemical class 0.000 description 1
- 230000001681 protective effect Effects 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 238000005507 spraying Methods 0.000 description 1
- 231100000331 toxic Toxicity 0.000 description 1
- 230000002588 toxic effect Effects 0.000 description 1
Classifications
-
- 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
- C10B49/00—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated
- C10B49/02—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with hot gases or vapours, e.g. hot gases obtained by partial combustion of the charge
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E50/00—Technologies for the production of fuel of non-fossil origin
- Y02E50/10—Biofuels, e.g. bio-diesel
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Combustion & Propulsion (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Materials Engineering (AREA)
- Organic Chemistry (AREA)
- Coke Industry (AREA)
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
Abstract
Abstract of the Disclosure A process for the continuous coking of peat, bovey coal, wood and the like, in particle form. Dried particles are fed into one end of a reaction chamber, stirred, and coked in the reaction chamber by heating them with hot gases, and the coked particles are removed at the other end of the reaction chamber for the purpose of cooling. The hot gases are fed in the reaction chamber over the particles to be coked in order to achieve a direct heat exchange contact between the gases and the particles. Preferably the hot gases are contacted counter-currently with the upper surface of the particle bed moving through the reaction chamber and the reaction chamber comprises a cylindrical furnace which is rotated around its longitudinal axis to stir the particles and to move them forward in the form of a bed.
Description
1~54~
The present invention relates to a process for the continuous cok-ing of peat, bovey coal, wood and the like, in particle form, wherein dried particles are fed into one end of the reaction chamber, the particles are stirred and coked in the reaction chamber by heating them with hot gases, and the o~ked particles are removed for cooling at the other end of the reaction chamber.
Previously known are a great number of different processes for coking or dry-distilling organic material, mainly coal and bovey coal. The coking takes place in these processes by heating the organic material in particle form with hot gases, usually hot smoke gases. These processes can thus be classified into two groups in regard to the manner in which heating with gas takes place: processes in which the heating takes place by an in- -direct heat exchange contact, and those in which the heating takes place by direct heat exchange contact between the hot smoke gases and the mater-ial to be coked in particle form.
Thus, it is known to coke coal in a cylindrical furnace by bring-ing the coal in the cylindrical furnace into indirect heat exchange with the hot smoke gases fed into the space between the cylindrical furnace and a stationary mantle around it. The greatest disadvantage of this process is the poor heat-transfer capacity due to indirect heat exchange, a factor which requires a great difference in temperature between the hGt smoke gases and the coal to be coked. In addition, the mantle has low durability owing ~ ~ ;
to the high temperature employed. It n~lst also be noted that such a furn-ace provided with a double mantle is much more expensive than an ordinary cylindrical furnace.
Also known are processes in which the material to be coked is fed ~`;
into the upper end of the reaction shaft and is removed at its lower end, and hot gases are blown, through nozzles extending into th0 reaction shaft, through the material settling in the shaft. These gases effectively heat .. - . .
... ~ ~ . . : . .
~5~8~
the material to be coked. Ilowever, such processes consume a great quantity of carbon wlth the result that the coke yield remains relatively low, es-pecially at high temperatures. The carbon dioxide and water vapor present in the hot gases are caused, by the good contact between the gases and the material to be cokecl~ to react with the coke, thereby forming carbon mono-xidc alld hydrogen gas, which naturally reduccs the coke yield considerably.
[n another similar process, oil shale is loaded into trolleys which are removed through an oblong horizontal tunnel, from the floor of which hot gases are blown upwards, and the gases flow through the trolleys and their load from below. The same disadvantages appear in this process as in the previous one.
The object of the present invention is to provide a process for the continuous coking of peat, bovey coal, wood and the like, in particle form. In the process, the heat exchange between the hot gases and the ;~
material to be coked is good without the heating gases being in too effec- 3 ' ' tive a contact with the material to be coked, and consequently, the coke yield is high. The object of the invention is, in other words, to achieve a good exchange of heat between the heating gas and the solid material with-out allowing the heating gases to react with the solid material.
The process according to the invention deviates from the above-mentioned processes and devices operating by direct heat exchange in that the hot smoke gases are not directed through the bed of material to be coked, but over it. Thereby the carbonization gases released from the material to be coked are able to effectively protect the solid bed from oxidation. The composition of the gas in the bed and even slightly above it is thus differ-ent from that in the furnace gas space, which has a carbon-consuming atmos-phere. The carbonization gases released from the bed of solid material serve -~
as a protective gas which prevents the oxidation of the coke.
In a kroàd aspect, the invention resides in a process for the - . ,, . - ~ ~ ~ . : ,' ' ' :.
. :. , :
- 1~5408~3 ;
continuous coking of peat, bovey coal, wood and the like, in particle form, wherein dried particles are fed into one end of a reaction chamber, stirred, and coked in the reaction chamber by heating them with ho-t gases, and the coked particles are removed at the other end of the reaction chamber for the purpose o cooling, characterized in that the particles to be coked have a particle size of 100 mm. at the maximum, and the hot gases are fed into the reaction chamber over the particles to be coked in order to achieve a direct heat exchange contact between the gases and the particles.
By the process according to the invention, a high coke yield is obtained in spite of the fact that the smoke gases are brought into a direct heat exchange contact with the solid- `
material bed to be coked. The transfer of heat from the hot smoke gases into the solid material is very effective. Heat radiates from the burning gases both to the bed of solid material and to the furnace walls, and from the furnace walls heat is -~
transferred by conduction to the bed of solid material; this is especially effective if the furnace used is a cylindrical one in which the wall part heated by radiation and convection is transferred to a position below the bed of solid material, there-by giving heat to the material and causing the bed to rotate - `~
slightly.
The invention is described below in more detail with reference to the enclosed drawing in which, Figure 1 is schematic ~ ~
view of a system for the coking of peat by the process accord- ;; `
ing to the invention.
Dried peat is dry-distilled in a revolving cylindrical `
furnace 4 according to the countercurrent principle. An -~
auxiliary burner 5 is connected to the cylindrical furnace, and ',' ~':, ' ' ~ .
. ~ .
~ - 3 - ~ ~ `
~LIV5~8~
in this burner, flyiny dust, coke dust, cut peat or hot peat coke can be burned during the entire drying process. Most of the ashes produced can be eliminated by using a suitable separ-ate burner.
The hot smoke gases from the burner are fed into the hot end of the cylindrical furnace 4. Thereby, burning materials are released from the ~ .
'' ' `' '' :' ' ' ~ "' ' :
' ;; ., - - .
'' ' ` `
- 3a -```~ , ' ,.. , , .. . . . . : . . ~ : ~ - . . .
- , -- ~ .
macerial to be dry-distilled and are burned by an additional air blast re-presented by the vertical arrows over the cylindricaL furnace in ~he drawing.
The gas flow proceeds in the cylindrical furnace 4, giving heat to the solid material moving in the opposite direction. The heat is transEerred to the material to be dry-distiLlcd partly by conduction of the furnace wall and partly through radiation from the hot coking gases.
In the cylindrical furnace 4 only the surace o the peat layer is in contact with the mixture o smoke gases and carbonization gases. In addition, the released carbonization gases protect the bed of solid material from oxidation. The coke yield is thereore high.
The temperature and temperature profile of a furnace 4 with direct heating can be regulated quickly and within a wide range by means of an auxiliary burner and by an additional air blast~ Thus, the same unit can be used or manufacturing products suitable for different purposes. By regulating the number of revolutions and by selecting a large angle of in-clination for the urnace, a high heating rate is achieved, whereby part of the produced tars crack and the coke yield increases. The previously ~nown processes for manufacturing peat coke are not as flexible as the one accord~
ing to this invention.
Thereater, the coking-cylinder product proceeds in the direction of the heavy solid arrows, to a cooling unit 6, wherein the temperature can be lowered by~ for example, water spraying or inert gas~
The outlet gases rom the cylindrical furnace 4, which, moving in the direction of the heavy open arrows, contain dust and tar~ are burned in the gas burner 3. The toxic phenols are eliminated from the gases simul- ~ -taneously. An expensive dust and tar separation system is not necessary and the heat produced is used for the preliminary drying o the material to be coked.
The material to be coked is dried in some suitable unit, e~g., - : ' .' , ~
16:35~
in a cylinder drier or grate drier 1. The flying dusts separated in the cyclone 2 are used as fuel in ~he auxiliary burner 5 of the coking furance.
Ex_mple 1 Peat in particle form contained l.5% ash, 7l% volatiles, the analysis being C 56%, H 6%, 0 34%, N 2%. The peat was crushed to a particle size less than 50 mm. The particles may be even larger (up to 100 mm), but in that case the carbonization takes a longer time. The material was dried to a moisture content of 4.3%. It is advantageous to remove the mois~ure in a separate drying unit at least to a value below 20% to reduce the heat ~ ~
requirement of the coking and to raise the combustion temperature of the ~ ~;
carbonization gases. ~ `
The peat feed was 209 kg/h, which was dry-distilled according to the countercurrent principle in a cylindrical furnace 12 m long and with an inner diameter of 0.77 m. The mean delay of the material in the furnace ~.
was 2 h 34 min, the number of revolutions of the furnace being 0.5 rpm.
Smoke gases at 1000 C were fed at the rate 125 Nm3/h into the furnace from ~ ~ `
a separate peat burner. Most of the heat was, however, generated by blast-ing 75 ~m /h air into the hot end of the furnace, whereby part of the vola-tiles and stalks were burnedr The temperature of the hot end of the furnace was maintained at 750 C. A suitable temperature range is 550-1000 C. ~ ~
The mixture of the peat-burner smoke gases and the smoke and car- ;
bonization gases produced in the furnace emerged from the colder end of the furnace at 200 C. The gases, the analysis of which was (without water):
H2 6.8%, C0-C01 7%~ CH4 4.5%, N2 61.4%, Ar + 2 5 3%~ C2 11%, were burned after leaving the ~urnace.
The yield of coke was 62.8 kg/h, which is 31.5% of the dr~ weight of the feed. The analysis of the coke was: ash 4.8%, volatiles 5.9%, CfiX 89.3%.
.,.
. . ,: .
:
~5~
Exam~le 2 Carbonization of wood.
Wood chips with a moisture content of 11% were fed into the experi-mental apparatus described in the previous example. This time the auxili-ary burner was attached to the end of the furnace and butane was burned in it at the rate of 6 kg/h. The air blast was tlO Nm /h, the rotational velocity of the furnace 0.7 rpm, and the corresponding delay period 2 h 10 min.
When the dry weight of the ch-ips fed was 93 kg/h, charcoal was ~ ~ ;
obtained at 26 kg/h, the temperature of the hot end of furnace being 585 C.
The analysis of the charcoal was: ash 1.4%, volatiles 11~9~o~ C~i 86.5% .
~he gases emerging from the fu nace were fed into the tar eparation unit.
`','' ` ~' .
.
'~,'. ~.
~,,.''~`'~
' ' ': ' ' ~.. ' .
The present invention relates to a process for the continuous cok-ing of peat, bovey coal, wood and the like, in particle form, wherein dried particles are fed into one end of the reaction chamber, the particles are stirred and coked in the reaction chamber by heating them with hot gases, and the o~ked particles are removed for cooling at the other end of the reaction chamber.
Previously known are a great number of different processes for coking or dry-distilling organic material, mainly coal and bovey coal. The coking takes place in these processes by heating the organic material in particle form with hot gases, usually hot smoke gases. These processes can thus be classified into two groups in regard to the manner in which heating with gas takes place: processes in which the heating takes place by an in- -direct heat exchange contact, and those in which the heating takes place by direct heat exchange contact between the hot smoke gases and the mater-ial to be coked in particle form.
Thus, it is known to coke coal in a cylindrical furnace by bring-ing the coal in the cylindrical furnace into indirect heat exchange with the hot smoke gases fed into the space between the cylindrical furnace and a stationary mantle around it. The greatest disadvantage of this process is the poor heat-transfer capacity due to indirect heat exchange, a factor which requires a great difference in temperature between the hGt smoke gases and the coal to be coked. In addition, the mantle has low durability owing ~ ~ ;
to the high temperature employed. It n~lst also be noted that such a furn-ace provided with a double mantle is much more expensive than an ordinary cylindrical furnace.
Also known are processes in which the material to be coked is fed ~`;
into the upper end of the reaction shaft and is removed at its lower end, and hot gases are blown, through nozzles extending into th0 reaction shaft, through the material settling in the shaft. These gases effectively heat .. - . .
... ~ ~ . . : . .
~5~8~
the material to be coked. Ilowever, such processes consume a great quantity of carbon wlth the result that the coke yield remains relatively low, es-pecially at high temperatures. The carbon dioxide and water vapor present in the hot gases are caused, by the good contact between the gases and the material to be cokecl~ to react with the coke, thereby forming carbon mono-xidc alld hydrogen gas, which naturally reduccs the coke yield considerably.
[n another similar process, oil shale is loaded into trolleys which are removed through an oblong horizontal tunnel, from the floor of which hot gases are blown upwards, and the gases flow through the trolleys and their load from below. The same disadvantages appear in this process as in the previous one.
The object of the present invention is to provide a process for the continuous coking of peat, bovey coal, wood and the like, in particle form. In the process, the heat exchange between the hot gases and the ;~
material to be coked is good without the heating gases being in too effec- 3 ' ' tive a contact with the material to be coked, and consequently, the coke yield is high. The object of the invention is, in other words, to achieve a good exchange of heat between the heating gas and the solid material with-out allowing the heating gases to react with the solid material.
The process according to the invention deviates from the above-mentioned processes and devices operating by direct heat exchange in that the hot smoke gases are not directed through the bed of material to be coked, but over it. Thereby the carbonization gases released from the material to be coked are able to effectively protect the solid bed from oxidation. The composition of the gas in the bed and even slightly above it is thus differ-ent from that in the furnace gas space, which has a carbon-consuming atmos-phere. The carbonization gases released from the bed of solid material serve -~
as a protective gas which prevents the oxidation of the coke.
In a kroàd aspect, the invention resides in a process for the - . ,, . - ~ ~ ~ . : ,' ' ' :.
. :. , :
- 1~5408~3 ;
continuous coking of peat, bovey coal, wood and the like, in particle form, wherein dried particles are fed into one end of a reaction chamber, stirred, and coked in the reaction chamber by heating them with ho-t gases, and the coked particles are removed at the other end of the reaction chamber for the purpose o cooling, characterized in that the particles to be coked have a particle size of 100 mm. at the maximum, and the hot gases are fed into the reaction chamber over the particles to be coked in order to achieve a direct heat exchange contact between the gases and the particles.
By the process according to the invention, a high coke yield is obtained in spite of the fact that the smoke gases are brought into a direct heat exchange contact with the solid- `
material bed to be coked. The transfer of heat from the hot smoke gases into the solid material is very effective. Heat radiates from the burning gases both to the bed of solid material and to the furnace walls, and from the furnace walls heat is -~
transferred by conduction to the bed of solid material; this is especially effective if the furnace used is a cylindrical one in which the wall part heated by radiation and convection is transferred to a position below the bed of solid material, there-by giving heat to the material and causing the bed to rotate - `~
slightly.
The invention is described below in more detail with reference to the enclosed drawing in which, Figure 1 is schematic ~ ~
view of a system for the coking of peat by the process accord- ;; `
ing to the invention.
Dried peat is dry-distilled in a revolving cylindrical `
furnace 4 according to the countercurrent principle. An -~
auxiliary burner 5 is connected to the cylindrical furnace, and ',' ~':, ' ' ~ .
. ~ .
~ - 3 - ~ ~ `
~LIV5~8~
in this burner, flyiny dust, coke dust, cut peat or hot peat coke can be burned during the entire drying process. Most of the ashes produced can be eliminated by using a suitable separ-ate burner.
The hot smoke gases from the burner are fed into the hot end of the cylindrical furnace 4. Thereby, burning materials are released from the ~ .
'' ' `' '' :' ' ' ~ "' ' :
' ;; ., - - .
'' ' ` `
- 3a -```~ , ' ,.. , , .. . . . . : . . ~ : ~ - . . .
- , -- ~ .
macerial to be dry-distilled and are burned by an additional air blast re-presented by the vertical arrows over the cylindricaL furnace in ~he drawing.
The gas flow proceeds in the cylindrical furnace 4, giving heat to the solid material moving in the opposite direction. The heat is transEerred to the material to be dry-distiLlcd partly by conduction of the furnace wall and partly through radiation from the hot coking gases.
In the cylindrical furnace 4 only the surace o the peat layer is in contact with the mixture o smoke gases and carbonization gases. In addition, the released carbonization gases protect the bed of solid material from oxidation. The coke yield is thereore high.
The temperature and temperature profile of a furnace 4 with direct heating can be regulated quickly and within a wide range by means of an auxiliary burner and by an additional air blast~ Thus, the same unit can be used or manufacturing products suitable for different purposes. By regulating the number of revolutions and by selecting a large angle of in-clination for the urnace, a high heating rate is achieved, whereby part of the produced tars crack and the coke yield increases. The previously ~nown processes for manufacturing peat coke are not as flexible as the one accord~
ing to this invention.
Thereater, the coking-cylinder product proceeds in the direction of the heavy solid arrows, to a cooling unit 6, wherein the temperature can be lowered by~ for example, water spraying or inert gas~
The outlet gases rom the cylindrical furnace 4, which, moving in the direction of the heavy open arrows, contain dust and tar~ are burned in the gas burner 3. The toxic phenols are eliminated from the gases simul- ~ -taneously. An expensive dust and tar separation system is not necessary and the heat produced is used for the preliminary drying o the material to be coked.
The material to be coked is dried in some suitable unit, e~g., - : ' .' , ~
16:35~
in a cylinder drier or grate drier 1. The flying dusts separated in the cyclone 2 are used as fuel in ~he auxiliary burner 5 of the coking furance.
Ex_mple 1 Peat in particle form contained l.5% ash, 7l% volatiles, the analysis being C 56%, H 6%, 0 34%, N 2%. The peat was crushed to a particle size less than 50 mm. The particles may be even larger (up to 100 mm), but in that case the carbonization takes a longer time. The material was dried to a moisture content of 4.3%. It is advantageous to remove the mois~ure in a separate drying unit at least to a value below 20% to reduce the heat ~ ~
requirement of the coking and to raise the combustion temperature of the ~ ~;
carbonization gases. ~ `
The peat feed was 209 kg/h, which was dry-distilled according to the countercurrent principle in a cylindrical furnace 12 m long and with an inner diameter of 0.77 m. The mean delay of the material in the furnace ~.
was 2 h 34 min, the number of revolutions of the furnace being 0.5 rpm.
Smoke gases at 1000 C were fed at the rate 125 Nm3/h into the furnace from ~ ~ `
a separate peat burner. Most of the heat was, however, generated by blast-ing 75 ~m /h air into the hot end of the furnace, whereby part of the vola-tiles and stalks were burnedr The temperature of the hot end of the furnace was maintained at 750 C. A suitable temperature range is 550-1000 C. ~ ~
The mixture of the peat-burner smoke gases and the smoke and car- ;
bonization gases produced in the furnace emerged from the colder end of the furnace at 200 C. The gases, the analysis of which was (without water):
H2 6.8%, C0-C01 7%~ CH4 4.5%, N2 61.4%, Ar + 2 5 3%~ C2 11%, were burned after leaving the ~urnace.
The yield of coke was 62.8 kg/h, which is 31.5% of the dr~ weight of the feed. The analysis of the coke was: ash 4.8%, volatiles 5.9%, CfiX 89.3%.
.,.
. . ,: .
:
~5~
Exam~le 2 Carbonization of wood.
Wood chips with a moisture content of 11% were fed into the experi-mental apparatus described in the previous example. This time the auxili-ary burner was attached to the end of the furnace and butane was burned in it at the rate of 6 kg/h. The air blast was tlO Nm /h, the rotational velocity of the furnace 0.7 rpm, and the corresponding delay period 2 h 10 min.
When the dry weight of the ch-ips fed was 93 kg/h, charcoal was ~ ~ ;
obtained at 26 kg/h, the temperature of the hot end of furnace being 585 C.
The analysis of the charcoal was: ash 1.4%, volatiles 11~9~o~ C~i 86.5% .
~he gases emerging from the fu nace were fed into the tar eparation unit.
`','' ` ~' .
.
'~,'. ~.
~,,.''~`'~
' ' ': ' ' ~.. ' .
Claims (6)
PROPERTY OR PRIVILEGE IS CLAIMED ARE DEFINED AS FOLLOWS:
1. A process for the continuous coking of peat, bovey coal, wood, in particle form, wherein dried particles are fed into one end of a reaction chamber, stirred, and coked in the reaction chamber by heating them with hot gases, and the coked particles are removed at the other end of the reaction chamber for the purpose of cooling, characterized in that the particles to be coked have a particle size of 100 mm. at the maximum, and the hot gases are fed into the reaction chamber over the particles to be coked in order to achieve a direct heat exchange contact between the gases and the particles.
2. A process according to claim 1, characterized in that the hot gases are contacted countercurrently with the upper surface of the particle bed moving through the reaction chamber.
3. A process according to claim 1, characterized in that the reaction chamber used is a cylindrical furnace which is rotated around its longitudinal axis to stir the particles and to move them forward in the form of a bed.
4. A process according to claim 1, 2 or 3, characterized in that the particles to be coked have a particle size of less than 50 mm.
5. A process according to claim 1, 2 or 3, characterized in that the particles to be coked have a moisture content of less than 20% by weight.
6. A process according to claim 1, 2 or 3, characterized in that the temperature of the furnace at the entrance end of the hot gases is maintained at 550-1000°C.
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| FI401/74A FI56549C (en) | 1974-02-12 | 1974-02-12 | FOERFARANDE FOER KONTINUERLIG KOKSNING AV TORV BRUNKOL TRAE OCH DYLIKT I PARTIKELFORM |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CA1054088A true CA1054088A (en) | 1979-05-08 |
Family
ID=8504054
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA219,803A Expired CA1054088A (en) | 1974-02-12 | 1975-02-11 | Process for continuous coking of peat, bovey coal and wood |
Country Status (4)
| Country | Link |
|---|---|
| CA (1) | CA1054088A (en) |
| FI (1) | FI56549C (en) |
| IE (1) | IE41468B1 (en) |
| SE (1) | SE7501509L (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2012164160A1 (en) | 2011-05-27 | 2012-12-06 | Outotec Oyj | Method for producing charcoal |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CA907188A (en) * | 1970-04-27 | 1972-08-08 | Ronald C. B. Smith | Electronic telephone call restricting device |
-
1974
- 1974-02-12 FI FI401/74A patent/FI56549C/en active
-
1975
- 1975-01-23 IE IE129/75A patent/IE41468B1/en unknown
- 1975-02-11 CA CA219,803A patent/CA1054088A/en not_active Expired
- 1975-02-11 SE SE7501509A patent/SE7501509L/en unknown
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2012164160A1 (en) | 2011-05-27 | 2012-12-06 | Outotec Oyj | Method for producing charcoal |
| WO2012164162A1 (en) | 2011-05-27 | 2012-12-06 | Outotec Oyj | Method for producing bio-coke |
| EP2829589A1 (en) * | 2011-05-27 | 2015-01-28 | Outotec (Finland) Oy | Method for producing charcoal |
| EP2829588A1 (en) | 2011-05-27 | 2015-01-28 | Outotec (Finland) Oy | Method for producing bio-coke |
Also Published As
| Publication number | Publication date |
|---|---|
| FI40174A7 (en) | 1975-08-13 |
| IE41468B1 (en) | 1980-01-16 |
| SE7501509L (en) | 1975-08-13 |
| IE41468L (en) | 1975-08-12 |
| FI56549C (en) | 1980-02-11 |
| FI56549B (en) | 1979-10-31 |
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