CA1161254A - Feeding of carbon to a carbon gasification plant - Google Patents
Feeding of carbon to a carbon gasification plantInfo
- Publication number
- CA1161254A CA1161254A CA000330931A CA330931A CA1161254A CA 1161254 A CA1161254 A CA 1161254A CA 000330931 A CA000330931 A CA 000330931A CA 330931 A CA330931 A CA 330931A CA 1161254 A CA1161254 A CA 1161254A
- Authority
- CA
- Canada
- Prior art keywords
- carbon
- carbon dioxide
- suspension
- reactor
- feeding
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired
Links
Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/46—Gasification of granular or pulverulent flues in suspension
- C10J3/466—Entrained flow processes
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/46—Gasification of granular or pulverulent flues in suspension
- C10J3/48—Apparatus; Plants
- C10J3/52—Ash-removing devices
- C10J3/526—Ash-removing devices for entrained flow gasifiers
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/72—Other features
- C10J3/78—High-pressure apparatus
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/72—Other features
- C10J3/82—Gas withdrawal means
- C10J3/84—Gas withdrawal means with means for removing dust or tar from the gas
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/72—Other features
- C10J3/86—Other features combined with waste-heat boilers
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0913—Carbonaceous raw material
- C10J2300/093—Coal
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0953—Gasifying agents
- C10J2300/0959—Oxygen
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0953—Gasifying agents
- C10J2300/0973—Water
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/18—Details of the gasification process, e.g. loops, autothermal operation
- C10J2300/1807—Recycle loops, e.g. gas, solids, heating medium, water
- C10J2300/1815—Recycle loops, e.g. gas, solids, heating medium, water for carbon dioxide
Abstract
ABSTRACT
A process for feeding a gas-containing suspension of carbon and a liquid to the reactor of a carbon gasification plant, which comprises admix-ing with the suspension of carbon and a liquid, a gas or a gas-forming sub-stance. This process has the advantage of improving the pumpability of such slurries, through control of their viscosity.
A process for feeding a gas-containing suspension of carbon and a liquid to the reactor of a carbon gasification plant, which comprises admix-ing with the suspension of carbon and a liquid, a gas or a gas-forming sub-stance. This process has the advantage of improving the pumpability of such slurries, through control of their viscosity.
Description
~ ~i125~
This invention relates to a process for feeding a sus-pension of carbon to the reactor of a carbon gasification plant.
The reactor of a carbon gasification plant is preferably operated at gauge pressure. The gauge pressure and its maintenance are ensured by installing pressure locks at the feeding and at the discharge end of the reactor. Certain types of locks for example, pumps, and worm gear, require at the feeding end usually the use of a liquid as a carrying agent, for the carbon, being particular-ly in the form of coal. Pumps and the like require a mixture adapted to being pumped, the liquid content of which is relatively high.
The liquid used is preferably water which is simultaneously used for the production of CO- and H2 -containing gas. The invention is based on the admixture of gas to the suspension o~
carbon known from the German patent ~,631,185. In that patent, pre~erably carbon dioxide in liquid Eorm is used as the ~as. The liquid carbon dioxide acts as a slurrying agent and means of conveyance for the coal dust. Moreover, the carbon dioxide acts as a moderator of the gasification process.
The admixture of gaseous media to the suspension of ; carbon is also known from the United States patent ~,07~,981, the ~; United States patent 40,976 and the German patent 2,130,120.
However, the use of liquid carbon dioxide involves con-siderable problems relating to temperature. Thus, ~or example, the temperature of the slurry must be maintained at over 0C to prevent the precipitation of the water contained in the suspension o~ carbon in the ~orm of ice. The structural and operational measures required for maintaining the desired temperature consti-tute a heavy economic burden for the production of synthesis gas.
According to the invention the economy of producing synthesis gas is improved considerably through the admixture of gas to the suspension of carbon. This admixing is obtained by adding an ammonium carbonate solution to the suspension of carbon; result~
ing suspension of carbon is mixed with an acid and/ox heated. This shows that small amounts of ammonium carbonate solution are al-ready sufficient to improve the flowing properties of the suspen-sion of carbon considerably.
Phosphoric acid is preferably used as the acid for sett-ing the carbon dioxide free. In accordance with a further feature of the invention the freed carbon dioxide comes from the carbon dioxide wash commonly used in a synthesis gas plant. The carbon dioxde is washed out or precipitated from the crude gas and dissol~ed in ammonia water and used as the ammonium carbonate solution.
The drawing illustrates one embodiment of this in~ention.
In a reactor of a carbon gasification plant a suspension of carbon is charged from above. This is accomplished with aid of a pump 2. Oxygen is passed, together with the suspension of carbon, through a conduit 3 into the reactor 1. The operating temperature inside the reactor is approximately 1,400C and the operating pressure is approximately 30 bar.
According to this embodiment, the liquid phase of the suspension of carbon comprises water. However, if a different consistency is desired, then oil, or an oil residue, or the like may be used. The water in the suspension of carbon evaporates under influence of the heat in the reactor. The carbon reacts 1 ~ 612~4 with the oxygen and the produced water vapoux. This reaction pro-duces a synthesis gas with a hlgh proportion of carbon monoxide and free hydrogen. This synthesis gas is an important raw material.
A slag or residue is produced simultaneously with the synthesis gas, derived from the non-combustible ash materials in the carbon, especially if the feed material is coal. The slag gathers predominantly in a water bath at the bottom of the reactor 1 and is discharged into the ambient atmosphere with the aid of a lock 4, while the operational pressure of 30 bar is main-- 2a -
This invention relates to a process for feeding a sus-pension of carbon to the reactor of a carbon gasification plant.
The reactor of a carbon gasification plant is preferably operated at gauge pressure. The gauge pressure and its maintenance are ensured by installing pressure locks at the feeding and at the discharge end of the reactor. Certain types of locks for example, pumps, and worm gear, require at the feeding end usually the use of a liquid as a carrying agent, for the carbon, being particular-ly in the form of coal. Pumps and the like require a mixture adapted to being pumped, the liquid content of which is relatively high.
The liquid used is preferably water which is simultaneously used for the production of CO- and H2 -containing gas. The invention is based on the admixture of gas to the suspension o~
carbon known from the German patent ~,631,185. In that patent, pre~erably carbon dioxide in liquid Eorm is used as the ~as. The liquid carbon dioxide acts as a slurrying agent and means of conveyance for the coal dust. Moreover, the carbon dioxide acts as a moderator of the gasification process.
The admixture of gaseous media to the suspension of ; carbon is also known from the United States patent ~,07~,981, the ~; United States patent 40,976 and the German patent 2,130,120.
However, the use of liquid carbon dioxide involves con-siderable problems relating to temperature. Thus, ~or example, the temperature of the slurry must be maintained at over 0C to prevent the precipitation of the water contained in the suspension o~ carbon in the ~orm of ice. The structural and operational measures required for maintaining the desired temperature consti-tute a heavy economic burden for the production of synthesis gas.
According to the invention the economy of producing synthesis gas is improved considerably through the admixture of gas to the suspension of carbon. This admixing is obtained by adding an ammonium carbonate solution to the suspension of carbon; result~
ing suspension of carbon is mixed with an acid and/ox heated. This shows that small amounts of ammonium carbonate solution are al-ready sufficient to improve the flowing properties of the suspen-sion of carbon considerably.
Phosphoric acid is preferably used as the acid for sett-ing the carbon dioxide free. In accordance with a further feature of the invention the freed carbon dioxide comes from the carbon dioxide wash commonly used in a synthesis gas plant. The carbon dioxde is washed out or precipitated from the crude gas and dissol~ed in ammonia water and used as the ammonium carbonate solution.
The drawing illustrates one embodiment of this in~ention.
In a reactor of a carbon gasification plant a suspension of carbon is charged from above. This is accomplished with aid of a pump 2. Oxygen is passed, together with the suspension of carbon, through a conduit 3 into the reactor 1. The operating temperature inside the reactor is approximately 1,400C and the operating pressure is approximately 30 bar.
According to this embodiment, the liquid phase of the suspension of carbon comprises water. However, if a different consistency is desired, then oil, or an oil residue, or the like may be used. The water in the suspension of carbon evaporates under influence of the heat in the reactor. The carbon reacts 1 ~ 612~4 with the oxygen and the produced water vapoux. This reaction pro-duces a synthesis gas with a hlgh proportion of carbon monoxide and free hydrogen. This synthesis gas is an important raw material.
A slag or residue is produced simultaneously with the synthesis gas, derived from the non-combustible ash materials in the carbon, especially if the feed material is coal. The slag gathers predominantly in a water bath at the bottom of the reactor 1 and is discharged into the ambient atmosphere with the aid of a lock 4, while the operational pressure of 30 bar is main-- 2a -
2 ~ ~
tained.
The lock 4 comprises a container and a valve each at ita inlet and at its outlet end. ~Ihen the feeding end is open, slag gathers in the container o~ the lock 4 and sinks through the water ba-th to the bottom of the reactor 1. ~1hen a certain volume has accumulated in the contQiner, the valve at the inlet end is closed and the second valve is opened so that the slag can be removed from the container of the lock 4, without inter~ering with the operation oP the reactor. Thereupon the valve at the outlet end is closed again, the lock 4 is Pilled with water and the valve at the inlet end is opened.
Another portion of the slag produced in the reactor l, being the portion capable oP being air-borne, is discharged Prom the reactor l together with the synthesis gas. This gas iæ selectively cooled by means of a waste heat system, :~orming an integral part of the reactor l. After discharge Prom the reactor, further cooling may be carried out (not illustrated) before the crude gas en-ters a device for washing with carbon dioxide. This washing device 5 comprises two pressure tanks 6 and 7 which are interconnected by conduits 8 and 9. In the conduit 8 a pump lO is disposed and in the conduit 9 a choke ll. The conduit 8 terminates at either end at, the bottom of the tank, whereas the conduit 9 terminates at the end ~acing the tank 6 on its inside, below the level oP the water bath 12. The opposite end of the con-duit 9 terminates inside the tank 7 above the level of a water bath 13.
The water bath 13 is placed under either the same or a slightly lower pressure than the inside chamber o~ the reactor l. Due to this pres-sure, a substantial portion oP the carbon dioxide contained in the crude gas dissolves in the water. The water enriched with carbon dioxide enters the tank 7 through -the conduit 9 and the choke ll by virtue oP a considerable drop in pressure between the -two tanks 6 and 7. The water pressure is ~ ~ 612~a~
reduced with the aid o~ the choke 11 to the pressuredesired in-side the tank 7. After the reduction o~ pressure,the carbon diox-ide contained in the water bubbles off.
The water accumulating in the tank 7 is removed with the aid of a pump and returned to the tank 6 through the conduit 8.
The crude gas flowing through the water bath 12 in the tank 6 is prevented from entering the conduit 9 by maintaining the level in the water bath 12 above the termination of the conduit 9 in the tank 6. This is achieved with the aid of the choke 11 and/
or the pump 10. Any adjustment to the choke 11 and/or to the pump 10 is effected by means of a non-illustrated float inside the tank 6 which is connected with the choke 11 and/or the pump 10 by means of a suitable control system.
Any loss in water is compensated from a feeder line 14 by a slide 15 which functions either automatically, or is hand-operat-ed at intervals.
The slag washed out from the crude gas, together with the carbon dioxide, is collected inside a non-illustrated concen-trator, and is then discharged.
Moreover, precipitation may replace the washing with carbon dioxide. The precipitation is aimed at merely removing the carbon dioxide from the crude gas, whereas in the conventional washing with carbon dioxide usually an undesirable washing out of other components simultaneously takes place. In the case or pre-cipitation of the carbon dioxide a base solution is necessary to be present in the tank 6.
The reaction of the carbon dioxide with the base material produces a salt which is drawn from the tank 6 and char~edwi~ water and heated, so that a Free carbon dioxide is produced.
The carbon dioxide gathering in the tank 7 above the water bath 13 passes through a conduit 16, into which a non-return valve 17 has been inserted, on to a tank 18. Inside this tank is concentrated ammonium hydroxide. When the carbon dioxide flows through the tank 18 and the ammonium hydroxide, a substantial por-tion of the carbon dloxide is dissolved or is converted into ammonium carbonate. The ammonium hydroxide containing dissolved carbon dioxide an ammonium carbonate is drawn off with the aid of a pump 20 at the bottom of the tank 18 and passed to the carbon feed 21. The quantity of drawn-off solution is continuously re-placed through a feeder conduit 22, having a valve 23 inserted therein and with the aid of a pump 24.
Any carbon enterin~ the carbon feed 21 together with the ammonium hydroxide containing carbon dioxide as ammonium carbonate in dissolved form is wet -comminuted in a mill 25. However, the solution may likewise be added beyond the mill 25 after dry com-minution. The carbon dioxide is freed again by means of heating the suspension of carbon and liquid in the conduit to the reactor 1. The ammonium carbonate disintegrates after small quantities of phosphoric acid have been admi~ed. The necessary dosaging of phosphoric acid is provided from a conduit 26. To this ef~ect, a dosing pump is inserted into this conduit. The pump may be either of the continuous type continuously feeding through a suitable control valve, or of the intermittently injecting type.
5 ~
The carbon dioxide being released in the conduit forms a multitude of small bubbles which substantially improve the flowing properties of the suspension of carbon and liquid. Smal:L
bubbles have a slower rising speed than larger bubbles and are capable of maintaining the admixture of gas substantially stable.
- 5a -
tained.
The lock 4 comprises a container and a valve each at ita inlet and at its outlet end. ~Ihen the feeding end is open, slag gathers in the container o~ the lock 4 and sinks through the water ba-th to the bottom of the reactor 1. ~1hen a certain volume has accumulated in the contQiner, the valve at the inlet end is closed and the second valve is opened so that the slag can be removed from the container of the lock 4, without inter~ering with the operation oP the reactor. Thereupon the valve at the outlet end is closed again, the lock 4 is Pilled with water and the valve at the inlet end is opened.
Another portion of the slag produced in the reactor l, being the portion capable oP being air-borne, is discharged Prom the reactor l together with the synthesis gas. This gas iæ selectively cooled by means of a waste heat system, :~orming an integral part of the reactor l. After discharge Prom the reactor, further cooling may be carried out (not illustrated) before the crude gas en-ters a device for washing with carbon dioxide. This washing device 5 comprises two pressure tanks 6 and 7 which are interconnected by conduits 8 and 9. In the conduit 8 a pump lO is disposed and in the conduit 9 a choke ll. The conduit 8 terminates at either end at, the bottom of the tank, whereas the conduit 9 terminates at the end ~acing the tank 6 on its inside, below the level oP the water bath 12. The opposite end of the con-duit 9 terminates inside the tank 7 above the level of a water bath 13.
The water bath 13 is placed under either the same or a slightly lower pressure than the inside chamber o~ the reactor l. Due to this pres-sure, a substantial portion oP the carbon dioxide contained in the crude gas dissolves in the water. The water enriched with carbon dioxide enters the tank 7 through -the conduit 9 and the choke ll by virtue oP a considerable drop in pressure between the -two tanks 6 and 7. The water pressure is ~ ~ 612~a~
reduced with the aid o~ the choke 11 to the pressuredesired in-side the tank 7. After the reduction o~ pressure,the carbon diox-ide contained in the water bubbles off.
The water accumulating in the tank 7 is removed with the aid of a pump and returned to the tank 6 through the conduit 8.
The crude gas flowing through the water bath 12 in the tank 6 is prevented from entering the conduit 9 by maintaining the level in the water bath 12 above the termination of the conduit 9 in the tank 6. This is achieved with the aid of the choke 11 and/
or the pump 10. Any adjustment to the choke 11 and/or to the pump 10 is effected by means of a non-illustrated float inside the tank 6 which is connected with the choke 11 and/or the pump 10 by means of a suitable control system.
Any loss in water is compensated from a feeder line 14 by a slide 15 which functions either automatically, or is hand-operat-ed at intervals.
The slag washed out from the crude gas, together with the carbon dioxide, is collected inside a non-illustrated concen-trator, and is then discharged.
Moreover, precipitation may replace the washing with carbon dioxide. The precipitation is aimed at merely removing the carbon dioxide from the crude gas, whereas in the conventional washing with carbon dioxide usually an undesirable washing out of other components simultaneously takes place. In the case or pre-cipitation of the carbon dioxide a base solution is necessary to be present in the tank 6.
The reaction of the carbon dioxide with the base material produces a salt which is drawn from the tank 6 and char~edwi~ water and heated, so that a Free carbon dioxide is produced.
The carbon dioxide gathering in the tank 7 above the water bath 13 passes through a conduit 16, into which a non-return valve 17 has been inserted, on to a tank 18. Inside this tank is concentrated ammonium hydroxide. When the carbon dioxide flows through the tank 18 and the ammonium hydroxide, a substantial por-tion of the carbon dloxide is dissolved or is converted into ammonium carbonate. The ammonium hydroxide containing dissolved carbon dioxide an ammonium carbonate is drawn off with the aid of a pump 20 at the bottom of the tank 18 and passed to the carbon feed 21. The quantity of drawn-off solution is continuously re-placed through a feeder conduit 22, having a valve 23 inserted therein and with the aid of a pump 24.
Any carbon enterin~ the carbon feed 21 together with the ammonium hydroxide containing carbon dioxide as ammonium carbonate in dissolved form is wet -comminuted in a mill 25. However, the solution may likewise be added beyond the mill 25 after dry com-minution. The carbon dioxide is freed again by means of heating the suspension of carbon and liquid in the conduit to the reactor 1. The ammonium carbonate disintegrates after small quantities of phosphoric acid have been admi~ed. The necessary dosaging of phosphoric acid is provided from a conduit 26. To this ef~ect, a dosing pump is inserted into this conduit. The pump may be either of the continuous type continuously feeding through a suitable control valve, or of the intermittently injecting type.
5 ~
The carbon dioxide being released in the conduit forms a multitude of small bubbles which substantially improve the flowing properties of the suspension of carbon and liquid. Smal:L
bubbles have a slower rising speed than larger bubbles and are capable of maintaining the admixture of gas substantially stable.
- 5a -
Claims (4)
PROPERTY OR PRIVILEGE IS CLAIMED ARE DEFINED AS FOLLOWS:
1. A method for feeding a suspension of carbon to the reactor of a carbon gasification plant, characterized in that an ammonium carbonate solution is admixed with the suspension of car-bon and that the resulting suspension of carbon is mixed with an acid and/or heated.
2. A method according to claim 1, characterized in that phosphoric acid is used as the acid.
3. A method according to claim 1, characterized in that carbon dioxide is washed out or precipitated from the crude gas and the washed carbon dioxide is dissolved in ammonia water and used as an ammonium carbonate solution.
4. A process according to claim 1 wherein the carbon feed is comminuted coal.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| DE19782828457 DE2828457A1 (en) | 1978-06-29 | 1978-06-29 | ENTRY OF COAL INTO A COAL GASIFICATION PLANT |
| DEP2828457.3 | 1978-06-29 |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CA1161254A true CA1161254A (en) | 1984-01-31 |
Family
ID=6043046
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA000330931A Expired CA1161254A (en) | 1978-06-29 | 1979-06-29 | Feeding of carbon to a carbon gasification plant |
Country Status (9)
| Country | Link |
|---|---|
| EP (1) | EP0009073B1 (en) |
| JP (1) | JPS5844111B2 (en) |
| AU (1) | AU533129B2 (en) |
| BR (1) | BR7904150A (en) |
| CA (1) | CA1161254A (en) |
| DE (2) | DE2828457A1 (en) |
| PL (1) | PL120472B1 (en) |
| SU (1) | SU936817A3 (en) |
| ZA (1) | ZA793254B (en) |
Families Citing this family (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5849790A (en) * | 1981-09-19 | 1983-03-24 | Kawasaki Heavy Ind Ltd | Gasification of coal |
| JPS58136694A (en) * | 1982-02-08 | 1983-08-13 | Kawasaki Heavy Ind Ltd | Coal gasification |
| JPS58154796A (en) * | 1982-03-09 | 1983-09-14 | Ube Ind Ltd | Partial oxidation of solid fuel/water slurry |
| DE4129037C2 (en) * | 1991-08-31 | 1995-03-30 | Steag Ag | Method for introducing fuel into a fuel gasifier coupled to a power plant |
Family Cites Families (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE2130120B2 (en) * | 1971-06-18 | 1980-04-30 | Texaco Development Corp., White Plains, N.Y. (V.St.A.) | Process for the production of synthesis gas |
| US3929429A (en) * | 1974-09-26 | 1975-12-30 | Texaco Inc | Fuel gas from solid carbonaceous fuels |
| US4007017A (en) * | 1975-12-22 | 1977-02-08 | Slater William L | Production of clean synthesis or fuel gas |
| US4040976A (en) * | 1976-07-06 | 1977-08-09 | Cities Service Company | Process of treating carbonaceous material with carbon dioxide |
| DE2631185A1 (en) * | 1976-07-10 | 1978-01-19 | Texaco Development Corp | Gasification of solid carbonaceous fuels - slurried in liquid carbon dioxide, by continuous partial oxidation |
| US4074981A (en) * | 1976-12-10 | 1978-02-21 | Texaco Inc. | Partial oxidation process |
-
1978
- 1978-06-29 DE DE19782828457 patent/DE2828457A1/en not_active Withdrawn
-
1979
- 1979-06-26 DE DE7979102116T patent/DE2963101D1/en not_active Expired
- 1979-06-26 EP EP79102116A patent/EP0009073B1/en not_active Expired
- 1979-06-28 SU SU792781855A patent/SU936817A3/en active
- 1979-06-28 PL PL1979216682A patent/PL120472B1/en unknown
- 1979-06-28 AU AU48502/79A patent/AU533129B2/en not_active Expired
- 1979-06-29 JP JP54081565A patent/JPS5844111B2/en not_active Expired
- 1979-06-29 ZA ZA793254A patent/ZA793254B/en unknown
- 1979-06-29 BR BR7904150A patent/BR7904150A/en not_active IP Right Cessation
- 1979-06-29 CA CA000330931A patent/CA1161254A/en not_active Expired
Also Published As
| Publication number | Publication date |
|---|---|
| AU4850279A (en) | 1980-01-03 |
| EP0009073A1 (en) | 1980-04-02 |
| JPS5844111B2 (en) | 1983-09-30 |
| EP0009073B1 (en) | 1982-06-16 |
| PL216682A1 (en) | 1980-05-19 |
| SU936817A3 (en) | 1982-06-15 |
| AU533129B2 (en) | 1983-11-03 |
| PL120472B1 (en) | 1982-03-31 |
| JPS557893A (en) | 1980-01-21 |
| BR7904150A (en) | 1980-03-25 |
| DE2828457A1 (en) | 1980-01-10 |
| DE2963101D1 (en) | 1982-08-05 |
| ZA793254B (en) | 1980-08-27 |
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