CA1110068A - Method utilizing co.sub.2 for cooling agglomerates of coke - Google Patents
Method utilizing co.sub.2 for cooling agglomerates of cokeInfo
- Publication number
- CA1110068A CA1110068A CA300,456A CA300456A CA1110068A CA 1110068 A CA1110068 A CA 1110068A CA 300456 A CA300456 A CA 300456A CA 1110068 A CA1110068 A CA 1110068A
- Authority
- CA
- Canada
- Prior art keywords
- gas
- furnace
- agglomerates
- fuel
- coke
- 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
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B53/00—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form
- C10B53/08—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form in the form of briquettes, lumps and the like
-
- 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
- C10B49/04—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 while moving the solid material to be treated
- C10B49/06—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 while moving the solid material to be treated according to the moving bed type
-
- 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
- C10B57/00—Other carbonising or coking processes; Features of destructive distillation processes in general
- C10B57/04—Other carbonising or coking processes; Features of destructive distillation processes in general using charges of special composition
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Materials Engineering (AREA)
- Organic Chemistry (AREA)
- Combustion & Propulsion (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Industrial Gases (AREA)
- Solid Fuels And Fuel-Associated Substances (AREA)
- Coke Industry (AREA)
Abstract
ABSTRACT OF THE DISCLOSURE
Uncarbonized fuel agglomerates comprising a mixture of coking coal, or a mixture of fine coal, char, and non-coking agglomerates are fed into a countercurrent vessel such as a shaft furnace into which a stream of cool CO2 rich gas is injected which does not react with the agglomerates being discharged and thus provides a final cooling stage fiO that the fuel products can be handled without significant reoxidation;
the initial reaction of CO2 with fuel carbon provides the heat for temperature induration and also removes much of the excess reactivity in the product.
Uncarbonized fuel agglomerates comprising a mixture of coking coal, or a mixture of fine coal, char, and non-coking agglomerates are fed into a countercurrent vessel such as a shaft furnace into which a stream of cool CO2 rich gas is injected which does not react with the agglomerates being discharged and thus provides a final cooling stage fiO that the fuel products can be handled without significant reoxidation;
the initial reaction of CO2 with fuel carbon provides the heat for temperature induration and also removes much of the excess reactivity in the product.
Description
lll~Q68 BACKGROUND OF THE INVENTION
This invention relates generally to an improved method of cooling hot agglomerates of the type used for fuel in industrial application and processes such as, for example, the production of iron and steel, and in foundries.
More specifically the invention relates to a method of producing and cooli~g hot agglomerates in a continuous coking operation so that the resulting product will not oxidize with the atmosphere and provide a product of lower chemical reactivity with respect to CO2 so as to render the produced product more attractive to industrial use. The method of the invention utilizes a countercurrent furnace into which a strea.
of cool CO2 rich gas is injected. The cool CO2 gas does not react with the agglomerates being discharged because at the discharge end the products are sufficiently cool so the cooling stream of CO2 gas provides a final cooling sta~e wherein the fuel products can be handled without significant reoxidation.
Metallurgical coke is an essential material in an industrial society; it is indispensable for ironmaking opera-tions in blast furnaces--the most i.mportant source of iron for steel production. It is also utilized in selected steel.~akin3 processes and in the foundry industry.
Conventional coke is produced primarily in so-called "by-product coke ovens" where a blend of various coals is introduced and subjected to distillation to re~ove the volatile constituents from the coal. The end product is a porous m3ss that must be cooled to prevent burning durin~ stora3e under atmospheric conditions. The principal method to accomplish this is by quenchin~ with water, althou~h dry quenchin~ methods have recently been intrGduced as well.
111~(~68 These techniques suffer from the following disadvantages:
a) There is significant pollution associated with quenching operations, particularly with the most commonly practiced technique of water quenching.
b) The heat released in cooling operations is not recoverable and represents a significant fraction of the heat losses in cokemaking operations.
c) Such cooling operations cause thermal shock which in turn leads to product degradation, thereby increasing operating costs in ironmaking and in steelmaking.
d) Normally, the methods used for cooling permit moisture pickup in the product and this must be removed in subsequent operations, thus a~ain increasing thermal inefficiencies.
However, interest in coke coolin~ technology need not be limited to conventional cokemaking applications. In recent years, the general scarcity of good quality coking coals, plus the attendant price, and increases experienced by the industry have caused much interest in the so-called "formed cok~"
technology which does not require quality cokin3 coals as raw materials. These new processes reportedly operate with low-rank coals but provide a uniform metallur~ical coke that can replace the conventional product in most industrial applications. Unfortunately, formed coke technolo~y suffers from the same problems associated with conventional cokemakin~
applications, i.e., coolin~ of the final product. In addition, it has been found that formed coke tends to be ~ore reactive with respect to CO2 than conventional coke and this leads to lower productivity in blast furnaces.
1~10(~68 It is a general object of the present invention to provide an improved method to cool coke which avoids the above-stated problems.
Yet another object of the present invention is to provide an improved metho~ for co,oling coke products which not only eliminates the drawbacks of conventional cooling methods but can also reduce the chemical reactivities in the coke product.
SUMMARY OF THE INVENTION
According to the invention, there is provided a method of producing and cooling hot agglomerates of the type used for fuel to prevent oxidization of the agglomerates upon contact with atmosphere and to regenerate process gas, wherein a fuel material, such as coking coal or a mixture of fine coal, char, and non-coking agglomerates, is continuously moved therethrough to process gases which serve to preheat the material to form char, and then continue to heat the material to devolatilize the coal and form coke agglomerates of plastic consistency, characterized by the steps of:
(a) introducing CO2 rich gas into the formed agglomerates at a cooling stage in their production where the agglomerates are at a temperature in the range of 100 to ~00F., (b) heating the C~2 ga~ in the cooling stage to a temperature to initiate the reaction C~2 + C ~ 2 CO to cause unreacted carbon in the hot agglomerate to react and elevate the agglomerates to a final carbonization temperature not exceeding 2350F, (c) moving the gas to a heat-hardening and carbon-ization zone wherein the temperature of the a~lo~erates does not exceed 2000F, Q~i8 (d) introducing oxidizing gases into the agglomer-ates in the heat hardening and carbonization zone, (e) continuing the heating of the gas for a duration to cause the reaction CO ~ l/2 2 C ~ CO2 and to maintain the temperature of the agglomerate in the zone of step (c) in a range of 1200F to 2000F., (f) collecting the CO2 gas produced by step (e), and (g) re-introducing the CO2 gas as cooling gas into the process accordin3 to step (a).
Preferably, there is included the further step of:
continuing the reaction of step (b) until a tempera-ture is reached where the reaction becomes exothermic.
Preferably the CO2 gas is introduced into the agglomerates at a zone of the furnace where the agglomerates have a temperature of 600F. Preferably there is included the still further step of:
processing said gas through drying, preheating and incipient carbonization zones of the furnace at a rate which will enrich the gas in hydrogen according to the reaction (3) ~2 + CO ~ ~2 2 be seen that, in subsequent stages of the gas phase composition accordin3 to the method of the invention, several reactions occur. ~hese are:
(l) CO2 + C ~ 2C~
This invention relates generally to an improved method of cooling hot agglomerates of the type used for fuel in industrial application and processes such as, for example, the production of iron and steel, and in foundries.
More specifically the invention relates to a method of producing and cooli~g hot agglomerates in a continuous coking operation so that the resulting product will not oxidize with the atmosphere and provide a product of lower chemical reactivity with respect to CO2 so as to render the produced product more attractive to industrial use. The method of the invention utilizes a countercurrent furnace into which a strea.
of cool CO2 rich gas is injected. The cool CO2 gas does not react with the agglomerates being discharged because at the discharge end the products are sufficiently cool so the cooling stream of CO2 gas provides a final cooling sta~e wherein the fuel products can be handled without significant reoxidation.
Metallurgical coke is an essential material in an industrial society; it is indispensable for ironmaking opera-tions in blast furnaces--the most i.mportant source of iron for steel production. It is also utilized in selected steel.~akin3 processes and in the foundry industry.
Conventional coke is produced primarily in so-called "by-product coke ovens" where a blend of various coals is introduced and subjected to distillation to re~ove the volatile constituents from the coal. The end product is a porous m3ss that must be cooled to prevent burning durin~ stora3e under atmospheric conditions. The principal method to accomplish this is by quenchin~ with water, althou~h dry quenchin~ methods have recently been intrGduced as well.
111~(~68 These techniques suffer from the following disadvantages:
a) There is significant pollution associated with quenching operations, particularly with the most commonly practiced technique of water quenching.
b) The heat released in cooling operations is not recoverable and represents a significant fraction of the heat losses in cokemaking operations.
c) Such cooling operations cause thermal shock which in turn leads to product degradation, thereby increasing operating costs in ironmaking and in steelmaking.
d) Normally, the methods used for cooling permit moisture pickup in the product and this must be removed in subsequent operations, thus a~ain increasing thermal inefficiencies.
However, interest in coke coolin~ technology need not be limited to conventional cokemaking applications. In recent years, the general scarcity of good quality coking coals, plus the attendant price, and increases experienced by the industry have caused much interest in the so-called "formed cok~"
technology which does not require quality cokin3 coals as raw materials. These new processes reportedly operate with low-rank coals but provide a uniform metallur~ical coke that can replace the conventional product in most industrial applications. Unfortunately, formed coke technolo~y suffers from the same problems associated with conventional cokemakin~
applications, i.e., coolin~ of the final product. In addition, it has been found that formed coke tends to be ~ore reactive with respect to CO2 than conventional coke and this leads to lower productivity in blast furnaces.
1~10(~68 It is a general object of the present invention to provide an improved method to cool coke which avoids the above-stated problems.
Yet another object of the present invention is to provide an improved metho~ for co,oling coke products which not only eliminates the drawbacks of conventional cooling methods but can also reduce the chemical reactivities in the coke product.
SUMMARY OF THE INVENTION
According to the invention, there is provided a method of producing and cooling hot agglomerates of the type used for fuel to prevent oxidization of the agglomerates upon contact with atmosphere and to regenerate process gas, wherein a fuel material, such as coking coal or a mixture of fine coal, char, and non-coking agglomerates, is continuously moved therethrough to process gases which serve to preheat the material to form char, and then continue to heat the material to devolatilize the coal and form coke agglomerates of plastic consistency, characterized by the steps of:
(a) introducing CO2 rich gas into the formed agglomerates at a cooling stage in their production where the agglomerates are at a temperature in the range of 100 to ~00F., (b) heating the C~2 ga~ in the cooling stage to a temperature to initiate the reaction C~2 + C ~ 2 CO to cause unreacted carbon in the hot agglomerate to react and elevate the agglomerates to a final carbonization temperature not exceeding 2350F, (c) moving the gas to a heat-hardening and carbon-ization zone wherein the temperature of the a~lo~erates does not exceed 2000F, Q~i8 (d) introducing oxidizing gases into the agglomer-ates in the heat hardening and carbonization zone, (e) continuing the heating of the gas for a duration to cause the reaction CO ~ l/2 2 C ~ CO2 and to maintain the temperature of the agglomerate in the zone of step (c) in a range of 1200F to 2000F., (f) collecting the CO2 gas produced by step (e), and (g) re-introducing the CO2 gas as cooling gas into the process accordin3 to step (a).
Preferably, there is included the further step of:
continuing the reaction of step (b) until a tempera-ture is reached where the reaction becomes exothermic.
Preferably the CO2 gas is introduced into the agglomerates at a zone of the furnace where the agglomerates have a temperature of 600F. Preferably there is included the still further step of:
processing said gas through drying, preheating and incipient carbonization zones of the furnace at a rate which will enrich the gas in hydrogen according to the reaction (3) ~2 + CO ~ ~2 2 be seen that, in subsequent stages of the gas phase composition accordin3 to the method of the invention, several reactions occur. ~hese are:
(l) CO2 + C ~ 2C~
(2) CO + l/2 32~ 2
(3) H20 + CO----~H2 + C~2 AS a result, the gas becomes pro~essively enriched in H2 and CO until the tempe~ature drops sufficiently to reverse lll~Q68 such reactions with the eventual precipitation of carbon black and moisture pickup. However, since the uncarbonized fuel consists primarily of chars and coal fractions with significant volatile content, such volatiles are incorporated into the gas stream. The final gas compositi4n of the gas at the exit point will then consist of coal volatiles, C02, plus varying amounts of hydrogen and CO depending on the gas temperature. It is expected that the entrained carbon black particles would be removed in conventional dust control systems; they are valuable for reuse during fuel agglomeration, both to achieve higher agglomerate densities resulting in hi~her product strength and also because of their low impurity levels. The gas would also be cooled by heat exchange for steam or power generation and to permit recycling into the vessel.
DESCRIPTION OF THE DRAWING
The invention will now be described in detail, with reference, by way of example, to the accompanying diagrammatic drawing which is a schematic view of a vertical shaft furnace and associated gas and solid flow diagram.
DESCRIPTION OF T~E INV~NTION
In the method of the invention a~glomerates are cooled so that the resulting product will not react (oxidize) with the atmosphere, while concurrently providing a product of lower chemical reactivity with respect to C~2 so as to render such product more attractive for industrial use.
The method is utilized in a countercurrent vessel which can be either vertically or horizontally arranged and depicted as a vertical shaft furnace 10 into which process gas flows upwardly countercurrent to the pro3ressive downward movement of the fuel material.
lllQ~68 According to the invention, a stream of CO2 rich gas comprising approximately 0.4-2% 2; 60-70~ N2; 15-25~ CO2;
5-10% CO is injected via pipes 11 at a temperature approximately 200-300F into a mass of uncarbonized fuel agglomerates comprising fine coa~, char and noncoking coal which has been charged into the furnace at the top thereof.
The cool CO2 gas does not react with the a3glomerates being discharged because at the discharge end such products are sufficiently cool already; at this point the cooling stream of CO2 simply provides a final cooling stage so that the fuel products can be handled without significant reoxidation.
As the CO2 enters the cooling section of the vessel it becomes heated due to heat exchange between the warm fuel and the gas. At temperatures of several hundred degrees F, however, the gas reacts with the carbon-rich fuel according to the following reaction:
(1) CO2 + C ~ 2 CO.
Since the reaction becomes exothermic at high temperatures, both the gas and the solids will show a steep but transient temperature increase. Such a sta3e provides the necessary heat for the final induration step in carbonization. At the same time, since the chemical reaction shifts toward the right at higher temperatures, the gas becomes CO rich an~ CO2 poor.
This prevents further CO2 conversion while providing a relatively stable temperature regime during final carboniza-tion. An important feature at this sta~e is that the chemical reaction occurs preferentially at those sites where there is an excess of free energy, i.e., at those points that are respon-sible for the hi3h chemical reactivity of the fuel a~31Omer-ates. Therefore, the initial reaction of CO2 with carbon not 1110~i8 only provides the heat for temperature induration but alsoremoves much of the excess reactivity in the product.
As the gas stream progresses inside the vessel it transfers heat to the solids that move countercurrently. To provide sufficient heat so as to maintain carbonization as well as to raise the temperature to the carbonization range (1290-1830~F), it becomes necessary to oxidize the gas by injecting air, oxygen, or similar gases (such as blast furnace top gases) via pipes 14 containing sufficient oxidating constitutes. The chemical reaction is: !
(2) CO + 1/2 2 ~ CO2;
which again permits reaction 1 to take place. Because these two reactions are strongly exothermic the result is sufficient heat being released into the solid phase, thus increasing the temperature to the point of incipient carbonization and beyond.
In subsequent stages, the gas phase composition is regulated by reactions 1 and 2, plus reaction of:
(8) H2O + CO ~ H2 + C2;
which tends to enrich the gas in hydrogen. The water, of course, derives from moisture elimination near the feed end of the vessel.
As a result of these reactions, the gas becomes progressively enriched in H2 and CO until the temperature drops sufficiently to reverse such reactions with the eventual precipitation of carbon black and moisture pickup. However, since the uncarbonized fuel consists primarily of chars and coal fractions with significant volatile content, such vola-tiles are incorporated into the gas stream. The final gascomposition of the gas at the exit point will then consist of coal volatiles, C02, plus varying amounts of hydrogen and CO, depending on the gas temperature. The entrained carbon black particles will be removed in conventional dust control systems and reuse during fuel agglomeration, both to achieve higher agglomerate densities (leading to higher product strength) and also because of their low impurity levels. The gas would also be cooled by heat exchange for steam or power generation, and to permit recycling into the vessel.
DESCRIPTION OF THE DRAWING
The invention will now be described in detail, with reference, by way of example, to the accompanying diagrammatic drawing which is a schematic view of a vertical shaft furnace and associated gas and solid flow diagram.
DESCRIPTION OF T~E INV~NTION
In the method of the invention a~glomerates are cooled so that the resulting product will not react (oxidize) with the atmosphere, while concurrently providing a product of lower chemical reactivity with respect to C~2 so as to render such product more attractive for industrial use.
The method is utilized in a countercurrent vessel which can be either vertically or horizontally arranged and depicted as a vertical shaft furnace 10 into which process gas flows upwardly countercurrent to the pro3ressive downward movement of the fuel material.
lllQ~68 According to the invention, a stream of CO2 rich gas comprising approximately 0.4-2% 2; 60-70~ N2; 15-25~ CO2;
5-10% CO is injected via pipes 11 at a temperature approximately 200-300F into a mass of uncarbonized fuel agglomerates comprising fine coa~, char and noncoking coal which has been charged into the furnace at the top thereof.
The cool CO2 gas does not react with the a3glomerates being discharged because at the discharge end such products are sufficiently cool already; at this point the cooling stream of CO2 simply provides a final cooling stage so that the fuel products can be handled without significant reoxidation.
As the CO2 enters the cooling section of the vessel it becomes heated due to heat exchange between the warm fuel and the gas. At temperatures of several hundred degrees F, however, the gas reacts with the carbon-rich fuel according to the following reaction:
(1) CO2 + C ~ 2 CO.
Since the reaction becomes exothermic at high temperatures, both the gas and the solids will show a steep but transient temperature increase. Such a sta3e provides the necessary heat for the final induration step in carbonization. At the same time, since the chemical reaction shifts toward the right at higher temperatures, the gas becomes CO rich an~ CO2 poor.
This prevents further CO2 conversion while providing a relatively stable temperature regime during final carboniza-tion. An important feature at this sta~e is that the chemical reaction occurs preferentially at those sites where there is an excess of free energy, i.e., at those points that are respon-sible for the hi3h chemical reactivity of the fuel a~31Omer-ates. Therefore, the initial reaction of CO2 with carbon not 1110~i8 only provides the heat for temperature induration but alsoremoves much of the excess reactivity in the product.
As the gas stream progresses inside the vessel it transfers heat to the solids that move countercurrently. To provide sufficient heat so as to maintain carbonization as well as to raise the temperature to the carbonization range (1290-1830~F), it becomes necessary to oxidize the gas by injecting air, oxygen, or similar gases (such as blast furnace top gases) via pipes 14 containing sufficient oxidating constitutes. The chemical reaction is: !
(2) CO + 1/2 2 ~ CO2;
which again permits reaction 1 to take place. Because these two reactions are strongly exothermic the result is sufficient heat being released into the solid phase, thus increasing the temperature to the point of incipient carbonization and beyond.
In subsequent stages, the gas phase composition is regulated by reactions 1 and 2, plus reaction of:
(8) H2O + CO ~ H2 + C2;
which tends to enrich the gas in hydrogen. The water, of course, derives from moisture elimination near the feed end of the vessel.
As a result of these reactions, the gas becomes progressively enriched in H2 and CO until the temperature drops sufficiently to reverse such reactions with the eventual precipitation of carbon black and moisture pickup. However, since the uncarbonized fuel consists primarily of chars and coal fractions with significant volatile content, such vola-tiles are incorporated into the gas stream. The final gascomposition of the gas at the exit point will then consist of coal volatiles, C02, plus varying amounts of hydrogen and CO, depending on the gas temperature. The entrained carbon black particles will be removed in conventional dust control systems and reuse during fuel agglomeration, both to achieve higher agglomerate densities (leading to higher product strength) and also because of their low impurity levels. The gas would also be cooled by heat exchange for steam or power generation, and to permit recycling into the vessel.
Claims (7)
1. The method of cooling hot agglomerates in artificial fuel production wherein the resulting product will have a lower reactivity or oxidizing tendency with the atmosphere;
continuously processing a mixture of fine coal, char and low grade coal agglomates through a countercurrent furnace to preheat the mixture to form char and to degasify the coal;
devolatizing the degasified coal into coke in a plastic form;
cooling the plastic coke in the furnace by introduc-ing a stream of CO2 rich gas into the furnace in a manner so that the introduced gas passes through the agglomerates therein which have reached a zone in the furnace wherein the tempera-ture of the agglomerates has been reduced to approximately 600°F.
continuously processing a mixture of fine coal, char and low grade coal agglomates through a countercurrent furnace to preheat the mixture to form char and to degasify the coal;
devolatizing the degasified coal into coke in a plastic form;
cooling the plastic coke in the furnace by introduc-ing a stream of CO2 rich gas into the furnace in a manner so that the introduced gas passes through the agglomerates therein which have reached a zone in the furnace wherein the tempera-ture of the agglomerates has been reduced to approximately 600°F.
2. The method according to claim 1 wherein the CO2 gas introduced into the furnace and passed through the cooled agglomerates to effect a final hardening of the agglomerates becomes heated due to the heat exchange between the warm fuel and the relatively cool gas to thereby elevate the temperature of the gas to a temperature wherein the gas reacts with the carbon rich fuel according to the reaction:
C02 + C ? 2 Co which reaction becomes exothermic at the higher temperature so that both the gases and the fuel show a relatively steep transient temperature increase to effect the final hardening of the fuel.
C02 + C ? 2 Co which reaction becomes exothermic at the higher temperature so that both the gases and the fuel show a relatively steep transient temperature increase to effect the final hardening of the fuel.
3. The method according to claim 2 wherein the CO2 gas introduced into the furnace and passes through the cooled agglomerates to effect a final hardening of the agglomerates becomes heated due to the heat exchange between the warm fuel and the relatively cool gas to thereby elevate the temperature of the gas several hundred degrees F wherein the gas reacts with the carbon rich fuel according to the reaction:
C02 + C ? 2 Co which results in the gas becoming CO rich and C02 poor to prevent further C02 conversion wherein the initial reaction of C02 with the carbon of the fuel provides the heat for final hardening of the fuel and removes a substantial portion of the excess reactivity in the hardened fuel.
C02 + C ? 2 Co which results in the gas becoming CO rich and C02 poor to prevent further C02 conversion wherein the initial reaction of C02 with the carbon of the fuel provides the heat for final hardening of the fuel and removes a substantial portion of the excess reactivity in the hardened fuel.
4. The method defined in claim 1 including collect-ing the off-gases from the coal being processed through the furnace from the input end of the furnace;
cooling the collected gases to form condensation of distillates;
adjusting the composition of the gas from which the distillates have been removed to obtain a coal reducing gas;
utilizing the reducing gas as the cooling medium which is introduced into the furnace at the discharge end thereof.
cooling the collected gases to form condensation of distillates;
adjusting the composition of the gas from which the distillates have been removed to obtain a coal reducing gas;
utilizing the reducing gas as the cooling medium which is introduced into the furnace at the discharge end thereof.
5. The method according to claim 1 wherein the mixture as it is being degasified is subjected to a counter-current flow of oxidizing gas which has been enriched by the gases given off by the coal during its progression through the furnace;
cooling the coke resulting from the degasifying of the mixture with reduction gases by introducing the reduction gases into the furnace at the discharge end thereof to cool the coke mass that resulted from the degasifying of the material progressing through the furnace to thereby harden the coke into a solid form which will not oxidize with the atmosphere, discharging the hardened coke from the furnace.
cooling the coke resulting from the degasifying of the mixture with reduction gases by introducing the reduction gases into the furnace at the discharge end thereof to cool the coke mass that resulted from the degasifying of the material progressing through the furnace to thereby harden the coke into a solid form which will not oxidize with the atmosphere, discharging the hardened coke from the furnace.
6. The method according to claim 5 wherein the reduction gas introduced into the furnace is takeoff gas from the furnace which has been cooled by a heat exchange process to a temperature which permits recycling of the gas into the furnace.
7. The method according to claim 3 wherein the gas phase composition is regulated by the reactions:
(1) CO2 + C ? 2CO
(2) CO + 1/2 02 ? C02 (3) H2O + CO? H2 + C02 wherein the gas becomes progressively enriched in H2 and CO
until the temperature drops sufficiently to reverse the reactions and the final composition of the gas as it exits from the furnace can be cooled by heat exchange and recycled into the furnace to cool the agglomerate to a temperature below 600°F to a point that the agglomerates can be handled without significant oxidation.
(1) CO2 + C ? 2CO
(2) CO + 1/2 02 ? C02 (3) H2O + CO? H2 + C02 wherein the gas becomes progressively enriched in H2 and CO
until the temperature drops sufficiently to reverse the reactions and the final composition of the gas as it exits from the furnace can be cooled by heat exchange and recycled into the furnace to cool the agglomerate to a temperature below 600°F to a point that the agglomerates can be handled without significant oxidation.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US80754577A | 1977-06-17 | 1977-06-17 | |
| US807,545 | 1977-06-17 |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CA1110068A true CA1110068A (en) | 1981-10-06 |
Family
ID=25196634
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA300,456A Expired CA1110068A (en) | 1977-06-17 | 1978-04-04 | Method utilizing co.sub.2 for cooling agglomerates of coke |
Country Status (10)
| Country | Link |
|---|---|
| JP (1) | JPS547402A (en) |
| AU (1) | AU515392B2 (en) |
| BE (1) | BE868082A (en) |
| BR (1) | BR7803832A (en) |
| CA (1) | CA1110068A (en) |
| DE (1) | DE2825692A1 (en) |
| FR (1) | FR2394599A1 (en) |
| GB (1) | GB1595825A (en) |
| IN (1) | IN147338B (en) |
| ZA (1) | ZA783134B (en) |
Families Citing this family (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5666991A (en) * | 1979-11-02 | 1981-06-05 | Nippon Telegr & Teleph Corp <Ntt> | Communication channel assignment change control system |
| AT387977B (en) * | 1986-12-18 | 1989-04-10 | Waagner Biro Ag | METHOD FOR OBTAINING A GAS-EMISSING GAS AND DEVICE FOR CARRYING OUT THE METHOD |
| KR100206500B1 (en) * | 1995-12-29 | 1999-07-01 | 이구택 | Method of block coke for iron melting furnace |
Family Cites Families (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| FR1535303A (en) * | 1966-08-31 | 1968-08-02 | Metallgesellschaft Ag | Process for the production of agglomerated coke |
| US3969088A (en) * | 1975-04-28 | 1976-07-13 | Peabody Coal Company | Formcoke process |
-
1978
- 1978-04-04 CA CA300,456A patent/CA1110068A/en not_active Expired
- 1978-05-26 GB GB23030/78A patent/GB1595825A/en not_active Expired
- 1978-05-30 IN IN403/DEL/78A patent/IN147338B/en unknown
- 1978-05-31 AU AU36743/78A patent/AU515392B2/en not_active Expired
- 1978-06-01 ZA ZA00783134A patent/ZA783134B/en unknown
- 1978-06-07 FR FR7817062A patent/FR2394599A1/en not_active Withdrawn
- 1978-06-12 DE DE19782825692 patent/DE2825692A1/en not_active Withdrawn
- 1978-06-13 BE BE188540A patent/BE868082A/en unknown
- 1978-06-15 BR BR787803832A patent/BR7803832A/en unknown
- 1978-06-16 JP JP7313478A patent/JPS547402A/en active Pending
Also Published As
| Publication number | Publication date |
|---|---|
| IN147338B (en) | 1980-02-02 |
| GB1595825A (en) | 1981-08-19 |
| AU3674378A (en) | 1979-12-06 |
| BE868082A (en) | 1978-12-13 |
| FR2394599A1 (en) | 1979-01-12 |
| JPS547402A (en) | 1979-01-20 |
| BR7803832A (en) | 1979-02-20 |
| DE2825692A1 (en) | 1979-01-04 |
| AU515392B2 (en) | 1981-04-02 |
| ZA783134B (en) | 1979-07-25 |
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