CA1146720A - Production of calcium carbide - Google Patents
Production of calcium carbideInfo
- Publication number
- CA1146720A CA1146720A CA000354910A CA354910A CA1146720A CA 1146720 A CA1146720 A CA 1146720A CA 000354910 A CA000354910 A CA 000354910A CA 354910 A CA354910 A CA 354910A CA 1146720 A CA1146720 A CA 1146720A
- Authority
- CA
- Canada
- Prior art keywords
- coke
- oxygen
- furnace
- lime
- thermal
- 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
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B32/00—Carbon; Compounds thereof
- C01B32/90—Carbides
- C01B32/914—Carbides of single elements
- C01B32/942—Calcium carbide
-
- 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
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
- Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
Abstract
PRODUCTION OF CALCIUM CARBIDE
ABSTRACT OF THE DISCLOSURE:
The invention relates to the production of calcium carbide by reacting coke with lime in the presence of oxygen inside an oxygen-thermal furnace. To this end, coal is subjected to a coking reaction inside a hearth furnace at temperatures for the issuing gas of at least 750° C. The resulting coke with an inherent temperature of at least 500° C is directly introduced into the oxygen-thermal furnace, admixed with lime and oxygen, and calcium oxide is produced therefrom.
ABSTRACT OF THE DISCLOSURE:
The invention relates to the production of calcium carbide by reacting coke with lime in the presence of oxygen inside an oxygen-thermal furnace. To this end, coal is subjected to a coking reaction inside a hearth furnace at temperatures for the issuing gas of at least 750° C. The resulting coke with an inherent temperature of at least 500° C is directly introduced into the oxygen-thermal furnace, admixed with lime and oxygen, and calcium oxide is produced therefrom.
Description
HOE 79/H 01g The present invention relates to a process for the production ~f calcium carbide by reacting coke with lime in the presence of oxygen inside an oxygen-thermal furnace, also termed carbothermal furnace, the coke coming from a hearth furnace.
It has been described that calcium carbide can be made by a process, known as the oxygen-thermal process (cf. Chemie-Ingenieur-TechnLk 28 (1956), pages 4 - 5~, wherein coke is burnt together with high percentage oxygen to provide the energy necessary for carbide formation at the very high temperat~res of about 2000 to 2500 C. Needless to say, technical difficulties had to be overcome prior to operation of oxygen-thermal furnaces with a production capacity of 100 metric tons of carbide per day, with the use of lumpy coal coke. For lack of commercial attractiveness, the oxygen-thermal production of carbide has however been replaced by an electrothermal process, and it has been suggested that lignite coke should be used therein. It has been practically impossible however for the coal coke or anthracite quantities to be replaced by lignite coke to an extent of more than 66 percen~ (cf. Braunkohle 11 (1956), 361). For reasons of cost, the use OL formed lignite coke in mode~n carbide furnaces has, however, been stopped. On the other hand, it has not been possible heretofore to operate an electro-thermal carbide furnace exclusively with the use of ~ine coke.
~' ~ 7~ ~
Despite the fact that its co~mercial attractiveness is not fully satisfactory, the oxygen-thermal process has recen~ly regained interest as a potential alternative to the electrothermal production of calcium carbide.
The present invention now unexpectedly provides a process for the oxygen-thermal production of calcium carbide, in which use can be made of coal coke or anthracite or a mixture thereof with lignite coke or of lignite coke alone, the latter being an especially inexpensive carbon carrier in the form of fine coke, the process permitting the oxygen~thermal production of calcium carbide to be improved.
The present invention relates more particularly to a process for the production of calcium carbide by reacting coke with lime in the presence of oxygen inside an oxygen-thermal furnace, which comprises: subjecting coal to a coking reaction inside a hearth furnace at temperatures for the issuing gas of at least 750 C, preferably w~thin the range 1100 to 1500 C; directly introducing the re-sulting coke with an inherent temperature of at least500 C into the oxygen-thermal furnace; admixing the coke ~ith lime and oxygen, and producing calcium oxide therefrom.
The term "introduction of coke" into the oxygen-thermal furnace or process as used in accordance withthis invention should be interpreted in a broad sense, i. e. so as to comprise the direct introduction of coke into the reactor and also the introduction of coke into 7~
an apparatus unit arranged ahead of the oxygen-thermal furnace, between hearth furnace and oxygen-thermal furnace, wherein it is mixed with the other component forming the furnace burden, more especially with lime which is thereby heated. In other words, critical~ty just resides in the direct or indirect introduction of the total heat of the coke into the oxygen-thermal furnace.
The term "coal" as used herein denotes all car-bonaceous materials which are commonly employed in a hearth furnace, e. g. mineral coal, brown coal (lignite), petroleum coke. Coke produced inside the hearth furnace is always introduced into the oxygen-thermal furnace.
The use of brown coal has been found to have highly beneficial effects. With respect thereto, it is pre-ferable ~or brown coal to be dried with counterpressure steam so as to contain less than about 25 weight%,more preferably less than about 15 weight%, of water. It is also preferable for brown coal to be used in the form of particles with a size o~ less than 20 mm, more pre-ferably less than 6 mm and most preferably less than ~ mm. Needless to say,however, it is also possible to use lumpy, e. g. formed coal with a size of up to 150 mm. In any case, care should be taken to ensure that the coke coming from the hearth furnace has a maximum particle size which does not ~nterfere with its use in an oxygen-thermal furnace. The present process even permits advantageous use to be made of fine particula~e coke.
The carbonaceous starting material is subjected to cokinE inside the hearth furnace, in customary manner.
The issuing gas should have a te~perature higher than calcination temperature, i. e. higher than 900 C, and the coke which is taken from the hearth furnace should preferably be at calcination temperature, i. e. at more than 500 C. Coke materials made as described herein are normally free from water and contain 0.5 to 20.0 weight% oi volatile matter together with 3 to 12 weight%
of ash. The content of C-fix may be as high as 65 to 90 weight% or even higher.
A further feature of the present invention provides for waste heat originating from the hearth furnace and oxygen-thermal furnace, respectively, to be used at least partially, preferably completely, for the generation of steam. To this end, the invention provides for the waste-heat boiler to have an after-combustion unit associated with it, in which combustible matter forming part of the waste gas is burnt. By optimum use of waste gas heat, it is possible to provide the heat energy necessary for drying brown coal, the entire electric power for operation of the plant, and the energy necessary for oxygen production.
In other words, a preferred feature oi this invention pro-vides for generated steam to be partially used for the production oi oxygen and partially ior drying the coal for use in the hearth furnace.
Coke which is produced in, and taken from, the hearth iurnace is directly employed in the carbide '7~0 furnace process. This compares favorably with those prior art processes which are carried out ~ith customary coke material. More particularly, the present process permits the amount of energy which is necessary for heating coke to be considerably reduced and the expenses which are normally incurred by the step of cooling coke to be avoided. The coke coming from the hearth furnace is introduced in customary manner, e. g. via a lock or by means of a carrier gas or under the action of gravity, into the oxygen-thermal furnace which is incidentally operated in customary manner. The resulting calcium carbide has properties corresponding to those of electrothermally made carbide and can be put to customary uses, just as the crude furnace gas. Energy in excess, for example, can be used for converting the crude furnace gas to synthetic gas.
The process of this invention also provides for the coke coming from the hearth furnace ~ be introduced into the reactor of the carbothermal furnace via one or ~o more heat-insulated feed pipes which are down pipes, for example, the escape of gas through the feed pipes being avoided by pressure equalization inside the reactor. In accordance with this invention, it is particularly ad-vantageous for hot hearth furnace coke to be mixed at least with a portion of lime, the coke and lime being incidentally used in the form of particles approximately identical in size, and for the resulting mixture to be in-troduced into the reactor of the carbothermal furnace. It ~s gen~r~lly good practice to admix the hot coke with ~ '7Z 0 a quantity of lime, which is thereby preheated, sufficient for the resulting lime/coke-mixture to assume a temperature of about 600 C or less, ahead of the reactor. In other words, as a result of the lime componen~ having a portion of the heat absorbed ~erein, the mixture is at a temperature lower than the very hot coke and therefore relatively easy to handle technically in the absence of adverse effects.
Despite this, the entire heat is admitted to the reactor inside which temperature peaks are not liable to occur.
This is highly desirable inasmuch as a regular temperature gradient is established therein which makes it possible for the reaction to follow a regular course.
A further feature of this invention provides for the hot coke or hot lime/coke-mixture to be injected at least partially into the reactor of the carbothermal furnace, with the use of an inert gas, or preferably with C0-containing furnace off-gas. In all those cases ; in which material coming from the hearth furnace is in-jected into the oxygen-thermal furnace, it is possible for the two furnaces to be positioned side by side~ i. e.
it is then not absolutely necessary for the latter furnace to have the hearth furnace mounted thereabove.
Beneficial effects of th~ present process reside in the possib~ity of operating a carbide furnace ex-clusively with the use of lignite coke, and of pro-ducing carbide ~y the oxygen-thermal process with the use just of fine coke. As a result, this process has been considerably improved as to energy balance and commercial attractiveness. Contributed to this has the possibility that limy ash constituents, if any, of the coal can also be transformed to calcium carbide.
The process of the present invention will now be described with reference to the accompanying drawing showing a diagrammatic and exemplary embodiment. Need-less to say, the invention which admits of various modi-fications without departing from its scope, is naturally not limited to the specific embodimen~ shown.
With reference to the drawings:
Brown coal ground to particles with a size of up to 10 mm is dried in an apparatus unit 1 so as to establish a water content of 14 weight% with the use of counter-pressure steam coming from a turbine 2. Vaporous matterand condensate~ respectively, obtained during drying is removed. Next~ the dry coal is introduced into hearth furnace 3 and subjected to coking therein in contact with air, at a temperature of 1400 C, for example, in the gas chamber. Off-gas coming from the gas chamber is introduced into waste-heat boiler 4 and used for generating superheated high pressure steam which is delivered to turbine 2. Power transformed to mechanical energy in the turbine 2 is used for low temperature decomposition of air in apparatus unit 5, i. e. for the production of oxygen needed in oxygen-thermal carbide furnace 6 and for the generation of electrical power in generator 8. Coke of 900 C which is taken ~rom hearth furnace 3 is introduced into the reactor with the use of an injector, for example, and a carrier gas, which is of~-gas coming from the carbide furnace. The reactor is also fed with lime and oxygen coming from unit 5. Off-gas of about 600 C from carbide furnace 6 is freed from dust in a cyclone 7 and used for heating boiler feed water, a portion of the off-gas being used as a carrier gas for hearth furnace coke~
Carbide is taken ~rom carbide furnace 6. Inasmuch as the crude furnace gas contains about 87 volume% CO and about 12 volume% H2, it is good practice for this gas to be converted to synthetic gas with the excess of energy aforesaid.
The following Examples illustrate the invention which is, however, not limited thereto:
EXAMPLE 1: (Comparative Example) 28 tons/h of lignite coke, 15 tons/h of lime (CaO-content = 94 weight%~ and 17 300 m3/h (S.T.P.) of oxygen were introduced into an oxygen-thermal furnace and reacted therein to give 13 tons/h of calcium carbide (carbide content = 80 weight%). 43 000 m3/h (S.T.P.) of crude ~as which had a temperature of about 600 C was recovered from the carbide furnace.
EXAMPLE 2: (Process of invention) The procedure was as in Example 1 but the coke was left uncooled and introduced, while hot, into the reactor. 139 tons/h of crude brown coal (water content = 60 weight%) was treated to obtain 65 tons/h of dry coal (particle size = up to 10 mm; water content =
7~
14 weight~o). As a result of the coke being introduced while hot, it was possible to reduce the quantity of coke to 23 tons/h. Downstream of the hearth furnace, it had a temperature of about 900 C. The coke was mixed with 7.5 tons/h of lime, which was used in the form of particles with a size of up to 5 rnm, and the resulting hot mixture (about 600 C) was introduced into the reactor for reaction therein with the balance quanti~y of llme and -- as a result of the coke being in-troduced while hot -- with a quantity of oxygen reduced to 13 400 m3/h (S.T.P.)~
EXAMPLE 3: (Process of invention) The procedure was as in Example 2 but the coke (23 tons/h) which had a temperature of about 900 C
downstream of the hearth furnace was used with that tempe-rature in the oxygen-thermal process. It was mixed with 15 tons/h of lime and the resulting hot mixture (about 400 C) was introduced into the reactor and reacted with oxygen therein.
It has been described that calcium carbide can be made by a process, known as the oxygen-thermal process (cf. Chemie-Ingenieur-TechnLk 28 (1956), pages 4 - 5~, wherein coke is burnt together with high percentage oxygen to provide the energy necessary for carbide formation at the very high temperat~res of about 2000 to 2500 C. Needless to say, technical difficulties had to be overcome prior to operation of oxygen-thermal furnaces with a production capacity of 100 metric tons of carbide per day, with the use of lumpy coal coke. For lack of commercial attractiveness, the oxygen-thermal production of carbide has however been replaced by an electrothermal process, and it has been suggested that lignite coke should be used therein. It has been practically impossible however for the coal coke or anthracite quantities to be replaced by lignite coke to an extent of more than 66 percen~ (cf. Braunkohle 11 (1956), 361). For reasons of cost, the use OL formed lignite coke in mode~n carbide furnaces has, however, been stopped. On the other hand, it has not been possible heretofore to operate an electro-thermal carbide furnace exclusively with the use of ~ine coke.
~' ~ 7~ ~
Despite the fact that its co~mercial attractiveness is not fully satisfactory, the oxygen-thermal process has recen~ly regained interest as a potential alternative to the electrothermal production of calcium carbide.
The present invention now unexpectedly provides a process for the oxygen-thermal production of calcium carbide, in which use can be made of coal coke or anthracite or a mixture thereof with lignite coke or of lignite coke alone, the latter being an especially inexpensive carbon carrier in the form of fine coke, the process permitting the oxygen~thermal production of calcium carbide to be improved.
The present invention relates more particularly to a process for the production of calcium carbide by reacting coke with lime in the presence of oxygen inside an oxygen-thermal furnace, which comprises: subjecting coal to a coking reaction inside a hearth furnace at temperatures for the issuing gas of at least 750 C, preferably w~thin the range 1100 to 1500 C; directly introducing the re-sulting coke with an inherent temperature of at least500 C into the oxygen-thermal furnace; admixing the coke ~ith lime and oxygen, and producing calcium oxide therefrom.
The term "introduction of coke" into the oxygen-thermal furnace or process as used in accordance withthis invention should be interpreted in a broad sense, i. e. so as to comprise the direct introduction of coke into the reactor and also the introduction of coke into 7~
an apparatus unit arranged ahead of the oxygen-thermal furnace, between hearth furnace and oxygen-thermal furnace, wherein it is mixed with the other component forming the furnace burden, more especially with lime which is thereby heated. In other words, critical~ty just resides in the direct or indirect introduction of the total heat of the coke into the oxygen-thermal furnace.
The term "coal" as used herein denotes all car-bonaceous materials which are commonly employed in a hearth furnace, e. g. mineral coal, brown coal (lignite), petroleum coke. Coke produced inside the hearth furnace is always introduced into the oxygen-thermal furnace.
The use of brown coal has been found to have highly beneficial effects. With respect thereto, it is pre-ferable ~or brown coal to be dried with counterpressure steam so as to contain less than about 25 weight%,more preferably less than about 15 weight%, of water. It is also preferable for brown coal to be used in the form of particles with a size o~ less than 20 mm, more pre-ferably less than 6 mm and most preferably less than ~ mm. Needless to say,however, it is also possible to use lumpy, e. g. formed coal with a size of up to 150 mm. In any case, care should be taken to ensure that the coke coming from the hearth furnace has a maximum particle size which does not ~nterfere with its use in an oxygen-thermal furnace. The present process even permits advantageous use to be made of fine particula~e coke.
The carbonaceous starting material is subjected to cokinE inside the hearth furnace, in customary manner.
The issuing gas should have a te~perature higher than calcination temperature, i. e. higher than 900 C, and the coke which is taken from the hearth furnace should preferably be at calcination temperature, i. e. at more than 500 C. Coke materials made as described herein are normally free from water and contain 0.5 to 20.0 weight% oi volatile matter together with 3 to 12 weight%
of ash. The content of C-fix may be as high as 65 to 90 weight% or even higher.
A further feature of the present invention provides for waste heat originating from the hearth furnace and oxygen-thermal furnace, respectively, to be used at least partially, preferably completely, for the generation of steam. To this end, the invention provides for the waste-heat boiler to have an after-combustion unit associated with it, in which combustible matter forming part of the waste gas is burnt. By optimum use of waste gas heat, it is possible to provide the heat energy necessary for drying brown coal, the entire electric power for operation of the plant, and the energy necessary for oxygen production.
In other words, a preferred feature oi this invention pro-vides for generated steam to be partially used for the production oi oxygen and partially ior drying the coal for use in the hearth furnace.
Coke which is produced in, and taken from, the hearth iurnace is directly employed in the carbide '7~0 furnace process. This compares favorably with those prior art processes which are carried out ~ith customary coke material. More particularly, the present process permits the amount of energy which is necessary for heating coke to be considerably reduced and the expenses which are normally incurred by the step of cooling coke to be avoided. The coke coming from the hearth furnace is introduced in customary manner, e. g. via a lock or by means of a carrier gas or under the action of gravity, into the oxygen-thermal furnace which is incidentally operated in customary manner. The resulting calcium carbide has properties corresponding to those of electrothermally made carbide and can be put to customary uses, just as the crude furnace gas. Energy in excess, for example, can be used for converting the crude furnace gas to synthetic gas.
The process of this invention also provides for the coke coming from the hearth furnace ~ be introduced into the reactor of the carbothermal furnace via one or ~o more heat-insulated feed pipes which are down pipes, for example, the escape of gas through the feed pipes being avoided by pressure equalization inside the reactor. In accordance with this invention, it is particularly ad-vantageous for hot hearth furnace coke to be mixed at least with a portion of lime, the coke and lime being incidentally used in the form of particles approximately identical in size, and for the resulting mixture to be in-troduced into the reactor of the carbothermal furnace. It ~s gen~r~lly good practice to admix the hot coke with ~ '7Z 0 a quantity of lime, which is thereby preheated, sufficient for the resulting lime/coke-mixture to assume a temperature of about 600 C or less, ahead of the reactor. In other words, as a result of the lime componen~ having a portion of the heat absorbed ~erein, the mixture is at a temperature lower than the very hot coke and therefore relatively easy to handle technically in the absence of adverse effects.
Despite this, the entire heat is admitted to the reactor inside which temperature peaks are not liable to occur.
This is highly desirable inasmuch as a regular temperature gradient is established therein which makes it possible for the reaction to follow a regular course.
A further feature of this invention provides for the hot coke or hot lime/coke-mixture to be injected at least partially into the reactor of the carbothermal furnace, with the use of an inert gas, or preferably with C0-containing furnace off-gas. In all those cases ; in which material coming from the hearth furnace is in-jected into the oxygen-thermal furnace, it is possible for the two furnaces to be positioned side by side~ i. e.
it is then not absolutely necessary for the latter furnace to have the hearth furnace mounted thereabove.
Beneficial effects of th~ present process reside in the possib~ity of operating a carbide furnace ex-clusively with the use of lignite coke, and of pro-ducing carbide ~y the oxygen-thermal process with the use just of fine coke. As a result, this process has been considerably improved as to energy balance and commercial attractiveness. Contributed to this has the possibility that limy ash constituents, if any, of the coal can also be transformed to calcium carbide.
The process of the present invention will now be described with reference to the accompanying drawing showing a diagrammatic and exemplary embodiment. Need-less to say, the invention which admits of various modi-fications without departing from its scope, is naturally not limited to the specific embodimen~ shown.
With reference to the drawings:
Brown coal ground to particles with a size of up to 10 mm is dried in an apparatus unit 1 so as to establish a water content of 14 weight% with the use of counter-pressure steam coming from a turbine 2. Vaporous matterand condensate~ respectively, obtained during drying is removed. Next~ the dry coal is introduced into hearth furnace 3 and subjected to coking therein in contact with air, at a temperature of 1400 C, for example, in the gas chamber. Off-gas coming from the gas chamber is introduced into waste-heat boiler 4 and used for generating superheated high pressure steam which is delivered to turbine 2. Power transformed to mechanical energy in the turbine 2 is used for low temperature decomposition of air in apparatus unit 5, i. e. for the production of oxygen needed in oxygen-thermal carbide furnace 6 and for the generation of electrical power in generator 8. Coke of 900 C which is taken ~rom hearth furnace 3 is introduced into the reactor with the use of an injector, for example, and a carrier gas, which is of~-gas coming from the carbide furnace. The reactor is also fed with lime and oxygen coming from unit 5. Off-gas of about 600 C from carbide furnace 6 is freed from dust in a cyclone 7 and used for heating boiler feed water, a portion of the off-gas being used as a carrier gas for hearth furnace coke~
Carbide is taken ~rom carbide furnace 6. Inasmuch as the crude furnace gas contains about 87 volume% CO and about 12 volume% H2, it is good practice for this gas to be converted to synthetic gas with the excess of energy aforesaid.
The following Examples illustrate the invention which is, however, not limited thereto:
EXAMPLE 1: (Comparative Example) 28 tons/h of lignite coke, 15 tons/h of lime (CaO-content = 94 weight%~ and 17 300 m3/h (S.T.P.) of oxygen were introduced into an oxygen-thermal furnace and reacted therein to give 13 tons/h of calcium carbide (carbide content = 80 weight%). 43 000 m3/h (S.T.P.) of crude ~as which had a temperature of about 600 C was recovered from the carbide furnace.
EXAMPLE 2: (Process of invention) The procedure was as in Example 1 but the coke was left uncooled and introduced, while hot, into the reactor. 139 tons/h of crude brown coal (water content = 60 weight%) was treated to obtain 65 tons/h of dry coal (particle size = up to 10 mm; water content =
7~
14 weight~o). As a result of the coke being introduced while hot, it was possible to reduce the quantity of coke to 23 tons/h. Downstream of the hearth furnace, it had a temperature of about 900 C. The coke was mixed with 7.5 tons/h of lime, which was used in the form of particles with a size of up to 5 rnm, and the resulting hot mixture (about 600 C) was introduced into the reactor for reaction therein with the balance quanti~y of llme and -- as a result of the coke being in-troduced while hot -- with a quantity of oxygen reduced to 13 400 m3/h (S.T.P.)~
EXAMPLE 3: (Process of invention) The procedure was as in Example 2 but the coke (23 tons/h) which had a temperature of about 900 C
downstream of the hearth furnace was used with that tempe-rature in the oxygen-thermal process. It was mixed with 15 tons/h of lime and the resulting hot mixture (about 400 C) was introduced into the reactor and reacted with oxygen therein.
Claims (13)
PROPERTY OR PRIVILEGE IS CLAIMED ARE DEFINED AS FOLLOWS:
1. A process for the production of calcium carbide by reacting coke with lime in the presence of oxygen inside an oxygen-thermal furnace, which comprises: subjecting coal to a coking reaction inside a hearth furnace at temperatures for the issuing gas of at least 750°C; directly introducing the resulting coke with an inherent temperature of at least 500°C into the oxygen-thermal furnace; admixing the coke with lime and oxygen, and producing calcium oxide therefrom.
2. The process as claimed in claim 1, wherein the coal used in the hearth furnace is brown coal consisting of particles with a size of up to 150 mm and the resulting coke is introduced into the oxygen-thermal furnace.
3. The process as claimed in claim 2, wherein the brown coal is used in the form of particles with a size of up to 20 mm, and contains not more than 25 weight% of water.
4. The process as claimed in claim 2, wherein the brown coal is used in the form of particles with a size of up to 6 mm, and contains not more than 25 weight% of water.
5. The process as claimed in claim 1, wherein waste heat coming from the hearth furnace and oxygen-thermal furnace, respectively, is at least partially used for the generation of steam.
6. The process as claimed in claim 5, wherein the generated steam is at least partially used for the production of oxygen.
7. The process as claimed in claim 5, wherein the generated steam is at least partially used for drying the coal for use in the hearth furnace.
8. The process as claimed in claim 1, wherein the coke coming from the hearth furnace is introduced into the reactor of the oxygen-thermal furnace via one or more heat-insulated feed pipes, designed as down pipes, the escape of gas through the feed pipes being avoided by pressure equalization inside the reactor.
9. The process as claimed in claim 1, wherein the hot hearth furnace coke is mixed at least with a portion of lime, the coke and lime being used in the form of particles approxi-mately identical in size, and the resulting mixture is introduced into the reactor of the oxygen-thermal furnace.
10. The process as claimed in claim 9, wherein the hot coke is admixed with a quantity of lime, which is thereby pre-heated, sufficient for the resulting lime/coke-mixture to have a temperature of about 600° C or less, ahead of the reactor.
11. The process as claimed in claim 1, wherein the hot coke and hot lime/coke-mixture, respectively, is injected at least partially into the reactor of the oxygen-thermal furnace.
12. The process as claimed in claim 10, wherein the inject-ion is effected by means of an inert gas.
13. The process as claimed in claim 10, wherein the inject-ion is effected by means of inert CO-containing furnace off gas.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| DEP2925897.7 | 1979-06-27 | ||
| DE19792925897 DE2925897A1 (en) | 1979-06-27 | 1979-06-27 | METHOD FOR PRODUCING CALCIUM CARBIDE |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CA1146720A true CA1146720A (en) | 1983-05-24 |
Family
ID=6074275
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA000354910A Expired CA1146720A (en) | 1979-06-27 | 1980-06-26 | Production of calcium carbide |
Country Status (9)
| Country | Link |
|---|---|
| EP (1) | EP0020957B1 (en) |
| JP (1) | JPS5641819A (en) |
| AU (1) | AU544486B2 (en) |
| CA (1) | CA1146720A (en) |
| DD (1) | DD151736A5 (en) |
| DE (2) | DE2925897A1 (en) |
| IN (1) | IN154590B (en) |
| PL (1) | PL122735B1 (en) |
| ZA (1) | ZA803816B (en) |
Families Citing this family (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE3035026A1 (en) * | 1980-09-17 | 1982-04-22 | Hoechst Ag, 6000 Frankfurt | METHOD FOR PRODUCING CALCIUM CARBIDE |
| DE3124672A1 (en) * | 1981-06-24 | 1983-01-13 | Hoechst Ag, 6000 Frankfurt | METHOD FOR PRODUCING CALCIUM CARBIDE |
| EP0428148A3 (en) * | 1989-11-13 | 1992-02-12 | Aeci Limited | Process for producing calcium carbide |
| CN106276901B (en) * | 2015-05-28 | 2020-07-24 | 中国科学院上海高等研究院 | Method and system for producing calcium carbide and CO gas by using oxygen thermal method |
| CN106241809B (en) * | 2016-08-31 | 2024-01-12 | 浙江嵘润机械有限公司 | Complete equipment for calcium carbide production |
Family Cites Families (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| FR605530A (en) * | 1925-10-09 | 1926-05-28 | Method and device for the simultaneous manufacture of calcium carbide, coke and synthetic products | |
| FR1063300A (en) * | 1951-07-30 | 1954-04-30 | Air Reduction | Process for preparing charges for calcium carbide furnaces |
| FR1090320A (en) * | 1952-12-30 | 1955-03-29 | Stamicarbon | Process for initiating the production of calcium carbide in a shaft furnace |
| US3623839A (en) * | 1968-08-21 | 1971-11-30 | Standard Oil Co | Method of making alkaline earth metal carbide |
-
1979
- 1979-06-27 DE DE19792925897 patent/DE2925897A1/en not_active Withdrawn
-
1980
- 1980-05-06 EP EP80102455A patent/EP0020957B1/en not_active Expired
- 1980-05-06 DE DE8080102455T patent/DE3063271D1/en not_active Expired
- 1980-06-24 DD DD80222118A patent/DD151736A5/en unknown
- 1980-06-26 ZA ZA00803816A patent/ZA803816B/en unknown
- 1980-06-26 AU AU59668/80A patent/AU544486B2/en not_active Ceased
- 1980-06-26 PL PL1980225235A patent/PL122735B1/en unknown
- 1980-06-26 CA CA000354910A patent/CA1146720A/en not_active Expired
- 1980-06-27 IN IN741/CAL/80A patent/IN154590B/en unknown
- 1980-06-27 JP JP8668980A patent/JPS5641819A/en active Pending
Also Published As
| Publication number | Publication date |
|---|---|
| AU544486B2 (en) | 1985-05-30 |
| PL122735B1 (en) | 1982-08-31 |
| EP0020957B1 (en) | 1983-05-18 |
| JPS5641819A (en) | 1981-04-18 |
| PL225235A1 (en) | 1981-05-08 |
| DE2925897A1 (en) | 1981-01-22 |
| DD151736A5 (en) | 1981-11-04 |
| DE3063271D1 (en) | 1983-07-07 |
| ZA803816B (en) | 1981-07-29 |
| EP0020957A1 (en) | 1981-01-07 |
| IN154590B (en) | 1984-11-17 |
| AU5966880A (en) | 1981-01-08 |
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| MKEX | Expiry |