CA1221238A - Process for the gasification of a solid carbon- containing fuel - Google Patents
Process for the gasification of a solid carbon- containing fuelInfo
- Publication number
- CA1221238A CA1221238A CA000425271A CA425271A CA1221238A CA 1221238 A CA1221238 A CA 1221238A CA 000425271 A CA000425271 A CA 000425271A CA 425271 A CA425271 A CA 425271A CA 1221238 A CA1221238 A CA 1221238A
- Authority
- CA
- Canada
- Prior art keywords
- gas
- nitrogen
- line
- synthesis gas
- fuel
- 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
-
- 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
- C10J2300/00—Details of gasification processes
- C10J2300/16—Integration of gasification processes with another plant or parts within the plant
- C10J2300/1678—Integration of gasification processes with another plant or parts within the plant with air separation
Abstract
A B S T R A C T
A PROCESS FOR THE GASIFICATION OF A SOLID
CARBON-CONTAINING FUEL
Coal is ground, dried and subsequently subjected to a partial combustion with oxygen or oxygen-enriched air, the oxygen having been obtained from an air separation plant. Hot synthesis gas produced by the partial combustion is first cooled to 100-500°C and then further cooled to 25-250°C by means of indirect heat exchange with a nitrogen-rich gas stream obtained in the air separation plant. Preferably, the heated nitrogen-rich gas stream is used to dry the coal.
A PROCESS FOR THE GASIFICATION OF A SOLID
CARBON-CONTAINING FUEL
Coal is ground, dried and subsequently subjected to a partial combustion with oxygen or oxygen-enriched air, the oxygen having been obtained from an air separation plant. Hot synthesis gas produced by the partial combustion is first cooled to 100-500°C and then further cooled to 25-250°C by means of indirect heat exchange with a nitrogen-rich gas stream obtained in the air separation plant. Preferably, the heated nitrogen-rich gas stream is used to dry the coal.
Description
A PROCESS E`OR THE G~SIFICATION OF A SOLID
CAP~ON-CO~TAINING FUEL
The invention relates to a process for the gasification of a solid carbon-containing fuel, wherein a) the fuel is ground fine and dried, k) the fuel is subseauently partially combusted to synthesis gas by means of oxygen or oxygen-enriched air, which oxygen originates from an air separation plant.
c) the synthesis gas is cooled to a temperature of 100-500C, and further comprising the step of d) further cooling the cooled synthesis gas to a temperature of 25-250C by means of indirect heat exchange with a nitrogen-rich gas originating from the air separation plant.
In the gasification (partial combustion) of a solid carbon-containing fuel synthesis gas is formedsubstantially con-sisting of carbon monoxide and hydrogen. Suitable solid fuels are coal, brown coal, co~e, peat, wood, etc.
A solid fuel is generally less reactive than a gaseous or a liquid fuel. In order nevertheless to obtain a rapid reaction the solid fuel is ground fine. The ground fuel i5 subsequently transported to a gasification reactor. A fuel con-taining a rela-tively large quantity of water may agglomerate during transport and thus cause bloc~ages in the transport line. In order to prevent this the solid fuel is dried before being transported to the reac-tor. After drying the moisture content of the fuel is preferably 0-10% by weight. ~he solid fuel is partially combusted with oxygen ' , ' .' ' . .' .
3 !3 - la -or with oxygen~e~rlched air, since the reaction then proceeds more rapidly than with air. Further, the synthesis gas formed now contains less nitrogen than when it is gasified with air. This simplifies the subsequent purification of the synthesis gas. More-over, synthesis gas prepared by means of oxygen is more suita'ole for certain synthesis, for example that of methanol or hydrocarbons.
,~
,~, ~ P.'23LZ38 The oxygen required as reactant is prepared in a plant where air is separated into an oxygen-rich and at least one nitro-gen-rich gas. To this end use is made of cryogenic distillation.
The partial combustion preferably takes place in the presence of a moderator. m e moderator has a moderating effect on the temperature in the reactor by endothermic reaction with the reactants and/or the partial oxidation products. Suitable mode-rators are steam and carbon dioxide.
After the fuel has reacted with the oxygen, the synthesis gas formed leaves the reactor at a temperature of 1200C-1700C. Apart from carbon monoxide and hydrogen the gas may also contain, inter alia, carbon dioxide, water vapour, sulphur co~,pounds, methane and small amounts of hydrogen cyanide and ammonia. Moreover, it entrains slag droplets. The slag droplets may present problems when they cool down. The fact is that they have no melting point but a melting range that can be hundreds of degrees centi~rade.
Since they are sticky in the melting range, they may cause block-ages. If coal is used as fuel, the slag is usually sticky in the temperature range of 900-1500C. Solid slag is no longer sticky.
Therefore, the hot gas is preferably rapidly cooled to a tempera-ture of 700-900C by injecting cold gas or a cold liquid. As a result of the rapid cooling the slag draplets quickly solidify to solid particlesD Suitable coolants are recycled synthesis gas, water and/or steam. The cooled synthesis gas is subsequently further cooled to 100-500C, preferably in a waste heat boiler in which useful high-pressure steam is generated. Subsequently, the solid slag particles are preferably removed from the gas.
After the solid slag particles have been separated from the gas, the synthesis gas is further processed. For example, the other impurities are then remLved from the synthesis gas. To this end it is advantageous to reduce the temperature of the impure synthesis gas to 25-250C. m is has so f æ been performed by means of air or water coolers. In this manner, hcw~ver, the residual heat of the synthesis yas was not applied usefully.
., . - ~
-.'~ ` .
` ' ' ~.;22~23~3 m e cryogenic distillation of air yields a nitrogen-rich gas which is qenerally discharged into the atmosphere. It is also possible that, in addition to an oxygen-rich gas, pure or substan-tially pure nitrogen and a stream of waste nitrogen is produced.
The pure nitrogen is preferably used in the process, for example as carxier gas for the ground fuel during the transport to the reactor. Another application is in the synthesis of ammonia. The waste nitrogen stream, which still contains some per cents of oxygen, is usually discharged into the atmosphere. The temperature of the nitrogen-rich gas that is discharged is generally chosen about 10C lower than the temperature of the ambient air.
In the process according to the present invention the rela-tive cold of the nitrogen-rich gas is used. The synthesis gas is further cooled to a temperature of 25-250C by means of indirect heat exchange with the nitrogen-rich gas.
m e above-mentioned indirect heat exchange can take place immediately after the passage of the synthesis gas through the waste heat boiler. However, the solid slag particles are prefer-ably at least partly first removed from the synthesis gas. This is effected in a suitable separator, such as a cyclone/ bend separa-tor, filterj etc. The heat exchange between the synthesis gas and the nitrogen-rich gas preferably takes place after the gas has at least partly been freed from the solid slag particles in the separator. Although at least the greater part of the solid slag particles has been separated frcm the synthesis gas in the separa-tor, solid slag particles can remain behind in the gas and these remaining slag particles constitute a risk of fouling of the cooler. m e synthesis gas is therefore more preferably not further cooled by means of indirect heat exchange with the nitrogen-rich gas until after it has at least once been scrub~ed with water. m e washing step results in an aqueous suspension of solid slag particles and synthesis gas that has substantially been purified of slag particles. m e aqueous suspension is separated frcm the synthesis gas and is advantageously at least partly recycled into the system. Suitable scrubbers are Venturi scrubbers and gas , ~2231.2~8 ~ 4 --scrubbers m which gas and ~ater are countercurrently contacted with each other.
In the scru~bing step the synthesis gas is already cooled down. By means of the indirect heat exchange with the nitrogen-rich gas the synthesis gas is further cooled preferably to atemperature of 40-140C.
As a result of the scrubbing step the synthesis gas contains much water va~our. The gas is preferably dried. This is most simply effected by cooling the synthesis gas to below the dew-point, as a result of which part of the water vapour condenses. Ifit is cooled to far belcw the dewpoint, the greater part of the water vapour condenses. Subsequently, the dry gas is separated from the condensate. The synthesis gas is preferably cooled to far below the dewpoint in a cooling treatment taking place after the indirect heat exchange with the nitrogen-rich gas. During said cooling the synthesis gas is advantageously cooled to a tempera-ture of 10-75C. The cooling can be carried out both with air and with water. Since the synthesis gas has already bee: cooled to 25-250C by means of indirect heat exchange with the nitrogen-rich gas, a relatively small cooler will suffice.
The nitrogen-rich gas heated according to the invention is preferably applied usefully for drying the solid fuel. Drying takes place before the fuel is fed into the gasification reactor.
If the solid fuel is supplied as not too coarse lumps, drying can be performed before it is passed to the grinding mill. If the fuel consists of large lu~ps, then it is more efficient to dry it during and/or after grinding. If the fuel has a high water con-tent, the hot nitrogen-rich gas, optionally after further heating, can be used to dry the fuel entirely or partly. In the latter case drying to the required water content takes place afterwards in another manner or with another hot gas. It is possible to use many types of grinding mills. Depending on the type of grinding mill drying takes place during or after grinding. For example, if a ball mill or a roller mill is used, the hot nitrogen-rich gas is introduced into the mill and already exercises its drying .
::
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effect during gxinding. The hot nitrogen~rich gas is subsequently used to discharge ~le ground fuel from the grinding mill and dries the fuel particles during transport.
~efore the drying of the solid fuel the nitrogen-rich gas is preferably heated to a temperature in the range of 50 to 400C, depending on the water content of the fuel. For the greater part of the fuels a temperature of 90-150C is suitable. The lower temperature limit is such that just enough expelling power is available to remove the water present from the fuel. The upper temperature limit is determined by economic motives. The heat content of the synthesis gas is such that the required quantity of the nitrogen-rich gas can be heated to a temperature up to 400G.
As already stated before, the nitrogen-rich gas is preferably the waste nitrogen stream formed in the cryogenic distillation of air. The invention is not limited thereto. Use can be made of any nitrogen-rich gas originating from the air separation plant. If a nitrogen-rich gas having a relatively high oxygen content is used to dry the ground fuel, there is a risk of an explosive combustion of the fuel with the oxygen. Thexefore, the nitrogen-rich gas preferably contains less than 12~ by volume of oxygen, more preferably less than 10~ by volume. The waste nitrogen stream ccmplies with said requirements.
The invention is now further illustrated with reference to the Figures to which the invention is otherwise by no means limited. .~uxilial~ means, such as ccmpressors, pumps, valves, etc., are not shown in the diagrammatic figures.
In Fig. 1 a carbon-containing solid fuel is introduced into a grinding mill 2 via line 1. Via a line 3 a stream of hot nitrogen-rich gas is introduced into the grinding mill 2, where the gas 30 dries the finely ground fuel. Ground and dried fuel, together with the gas mixtuxe of inter alia nitrogen and water vapour, is conducted to a separator 5 through a line 4. Suitable separators are for example, bend separators, cyclones, filters etc. In the separator 5 the ground fuel is separated from the gas. The gas 35 mainly consisting of nitrogen and water vapour is vented through a ,. :;, "~
~.~2~L~38 line 7. m e separated fuel particles are passed to a reactor 8 through a line 6. (Since the gasification reactor 8 is preferably operated at elevated pressure, the fuel is brought to the desired press~e by means of compressors, supply vessels, locks etc. which are not shcwn in the Figure.) An oxygen-rich gas origlnating fro.m an air separation plant 10 is also introduced into the reactor 8 via a line 9. Air is fed into the air separation plant 10 via a line 11. In plant 10 are formed an oxygen rich gas stream that is passed to the reactox 8 via the line 9 and a substantially pure nitrcgen stream, which can at least partly be used in the trans-port of the fuel to the reactor through the line 6. (Said stream is not shown in the Figure.) The plant 10 also produces a waste nitrogen stream which is discharged via a line 12. The gasifica-tion of the carbon-containing fuel with the oxygen and a m~derator (steam or CO2) supplied via a line 13 takes place in the reactor 8. m e resulting synthesis gas loaded wi.th slag droplets is passed via a line 14 to a cooling zone 15 where it is cooled dawn by injecting a cooled ana purified recycled synthesis gas that is supplied via line 16. In the cooling zone 15 all slag droplets in the hot synthesis gas solidify. Via a line 17 a mixture of synthe sis gas and solid slag particles is discharged fro.m the cooling zone 15 and passed into a waste heat boiler 18 where it is cooled indirectly with water that is supplied via a line 19 and discharg-ed as steam via a line 20. Fro.m the waste heat boiler 18 the still warm mixture of synthesis gas and solid slag particles is passed to a Venturi tube 22 via a line 21. There it is contacted with a suspension of solid slag particles in water that is conducted to the Venturi tube 22 via a line 23. In the Venturi tube 22 all the water of the suspension evaporates and a mixture of synthesis gas, water vapour and solid slag particles is passed via a line 24 to a cyclone 25 where the greater part of the solid slag particles is separated from the gas mlxture and is discharged fram the installa-tion via a line 26. The remainder of the solid slag particles is passed, together with the gas mixture, via a line 27 Lnto a Venturi scrubber 28 where it is contacted with an aqueous suspen-~2;~:1238 sion of solid slag particles supplied via a line 29. The mixtureof synthesis gas, water vapour, drops of water and solid slag par-ticles formed in the Venturi scrubber 28 is conducted to a sepa-rator 31 via a line 30. Here an aqueous suspension of solid slag particles is separated from the gas mixture and discharged via the line 23 through which line the aqueous suspension is passed to the venturi tube 22. The mixture of synthesis gas and water vapour still containing a small quantity of solid slag particles is introduced via a line 32 into the lower part of a gas scrubber 33, where it is countercurrently contacted with water that is passed to the upper part of the column 33 via a line 35. In the column 33 the last residues of solid slag particles are removed from the gas mixture cwing to which an aqueous suspension of solid slag parti-cles is fonmed that is passed frcm the column 33 to the Venturi scrubber 28 via the line 29. The gas mixture that is now practical-ly free from solid slag particles is conducted via a line 34 to a ccoler 36 where the synthesis gas mixture.is further cooled by indirect heat exchange with the cold waste nitrogen stream from the line 12 and the waste nitrogen stream is heated. m e resulting hot stream is passed from the cooler 36 to the grinding mill 2 via the line 3. If the synthesis gas mixture is cooled to below the dewpoint in the cooler 36 a mixt~re of synthesis gas, water vapour and water is conducted via a line 37 to an air cooler 38 to which air is supplied via a line 39 and discharged via a line 40. Here cooling to far below the dewpoint takes place, owing to which `
substantially the whole quantity of water vapour condenses. If the synthesis gas mixture is cooled in the cooler 36 to a temperature : above the dewpoint of the gas mixture, the line 37 contains exclusively synthesis gas and water vapour. A mixture of a synthe-sis gas, condensation water and a small quantity of water vapour is passed frcm the cooler 38 to a separator 42 via a line 41. In the separator 42 the muxture is separated into condensate that is discharged via a line 43 and a substantially dry synthesis gas that is discharged via a line 44. Part of the condensate is recycled to the column 33 via the line 35. m e remaining part is ....
, ~22~3~3 8 ~
discharged from the apparatus via a line 45. Part of the substan-tially dry synthesis gas is recycled to the cooling zone 15 via the line 16. The remainLng part of synthesis gas is discharged as final product from the apparatus via`a line 46 for further proces-sing.
Fig. 2 shows another embodim~nt of the process according tothe invention. Said process is particularly suitable to be used for solid fuels containing a relatively large quantity of water.
Immediately after leaving the waste heat boiler 18 the synthesis 10 gas is passed via the line 21 to a heat exchanger 101 where it is cooled by means of a preheated stream of nitrogen-rich gas sup-plied to the heat exchanger 101 via a line 102 and discharged via a line 103 to the grinding mill 2. ~le cooled synthesis gas is passed via a line 105 to a Venturi tube 106. Here it is contacted 15 with a water stream via a line 107. All the water introduced evaporates in the Venturi tube 106. The gas mixture is passed via line 108 to a bag filter 109. Here the solid slag particles are separated from the gas mixture. The separated solid slag particles are discharged from the apparatus via a line 110. The gas mixture 20 is passed via a line 111 to the cooler 36 ~rom which it is conduc-ted to the cooler 38 via the line 37. Water vapour condenses in the coolers 36 and 38. After separation of the condensation water from the synthesis gas in the separator 42 part of the water is conducted to the Venturi tube 106 via the line 107. The cold 25 nitrogen-rich gas stream is introduced into the cooler 36 via the line 12 and after heating it is discharged via the line 3. me somewhat warm gas stream can be further heated by indirect heat exchange with superheated steam in a heat exchanger 104 to which the steam is supplied via a line 112 and from which it is discharg-30 ed via a line 113. To this end use can, for example, be made ofsteam obtained in the line 20. Instead of indirect heat exchange with steam it is also possible to use steam in~ection into the nitrogen-rich gas stream in order to raise the temperature of the gas stream. m e wanm nitrogen-rich gas stream is passed to the heat exchanger 101. Here it cools the synthesis gas further ~, ,, .
CAP~ON-CO~TAINING FUEL
The invention relates to a process for the gasification of a solid carbon-containing fuel, wherein a) the fuel is ground fine and dried, k) the fuel is subseauently partially combusted to synthesis gas by means of oxygen or oxygen-enriched air, which oxygen originates from an air separation plant.
c) the synthesis gas is cooled to a temperature of 100-500C, and further comprising the step of d) further cooling the cooled synthesis gas to a temperature of 25-250C by means of indirect heat exchange with a nitrogen-rich gas originating from the air separation plant.
In the gasification (partial combustion) of a solid carbon-containing fuel synthesis gas is formedsubstantially con-sisting of carbon monoxide and hydrogen. Suitable solid fuels are coal, brown coal, co~e, peat, wood, etc.
A solid fuel is generally less reactive than a gaseous or a liquid fuel. In order nevertheless to obtain a rapid reaction the solid fuel is ground fine. The ground fuel i5 subsequently transported to a gasification reactor. A fuel con-taining a rela-tively large quantity of water may agglomerate during transport and thus cause bloc~ages in the transport line. In order to prevent this the solid fuel is dried before being transported to the reac-tor. After drying the moisture content of the fuel is preferably 0-10% by weight. ~he solid fuel is partially combusted with oxygen ' , ' .' ' . .' .
3 !3 - la -or with oxygen~e~rlched air, since the reaction then proceeds more rapidly than with air. Further, the synthesis gas formed now contains less nitrogen than when it is gasified with air. This simplifies the subsequent purification of the synthesis gas. More-over, synthesis gas prepared by means of oxygen is more suita'ole for certain synthesis, for example that of methanol or hydrocarbons.
,~
,~, ~ P.'23LZ38 The oxygen required as reactant is prepared in a plant where air is separated into an oxygen-rich and at least one nitro-gen-rich gas. To this end use is made of cryogenic distillation.
The partial combustion preferably takes place in the presence of a moderator. m e moderator has a moderating effect on the temperature in the reactor by endothermic reaction with the reactants and/or the partial oxidation products. Suitable mode-rators are steam and carbon dioxide.
After the fuel has reacted with the oxygen, the synthesis gas formed leaves the reactor at a temperature of 1200C-1700C. Apart from carbon monoxide and hydrogen the gas may also contain, inter alia, carbon dioxide, water vapour, sulphur co~,pounds, methane and small amounts of hydrogen cyanide and ammonia. Moreover, it entrains slag droplets. The slag droplets may present problems when they cool down. The fact is that they have no melting point but a melting range that can be hundreds of degrees centi~rade.
Since they are sticky in the melting range, they may cause block-ages. If coal is used as fuel, the slag is usually sticky in the temperature range of 900-1500C. Solid slag is no longer sticky.
Therefore, the hot gas is preferably rapidly cooled to a tempera-ture of 700-900C by injecting cold gas or a cold liquid. As a result of the rapid cooling the slag draplets quickly solidify to solid particlesD Suitable coolants are recycled synthesis gas, water and/or steam. The cooled synthesis gas is subsequently further cooled to 100-500C, preferably in a waste heat boiler in which useful high-pressure steam is generated. Subsequently, the solid slag particles are preferably removed from the gas.
After the solid slag particles have been separated from the gas, the synthesis gas is further processed. For example, the other impurities are then remLved from the synthesis gas. To this end it is advantageous to reduce the temperature of the impure synthesis gas to 25-250C. m is has so f æ been performed by means of air or water coolers. In this manner, hcw~ver, the residual heat of the synthesis yas was not applied usefully.
., . - ~
-.'~ ` .
` ' ' ~.;22~23~3 m e cryogenic distillation of air yields a nitrogen-rich gas which is qenerally discharged into the atmosphere. It is also possible that, in addition to an oxygen-rich gas, pure or substan-tially pure nitrogen and a stream of waste nitrogen is produced.
The pure nitrogen is preferably used in the process, for example as carxier gas for the ground fuel during the transport to the reactor. Another application is in the synthesis of ammonia. The waste nitrogen stream, which still contains some per cents of oxygen, is usually discharged into the atmosphere. The temperature of the nitrogen-rich gas that is discharged is generally chosen about 10C lower than the temperature of the ambient air.
In the process according to the present invention the rela-tive cold of the nitrogen-rich gas is used. The synthesis gas is further cooled to a temperature of 25-250C by means of indirect heat exchange with the nitrogen-rich gas.
m e above-mentioned indirect heat exchange can take place immediately after the passage of the synthesis gas through the waste heat boiler. However, the solid slag particles are prefer-ably at least partly first removed from the synthesis gas. This is effected in a suitable separator, such as a cyclone/ bend separa-tor, filterj etc. The heat exchange between the synthesis gas and the nitrogen-rich gas preferably takes place after the gas has at least partly been freed from the solid slag particles in the separator. Although at least the greater part of the solid slag particles has been separated frcm the synthesis gas in the separa-tor, solid slag particles can remain behind in the gas and these remaining slag particles constitute a risk of fouling of the cooler. m e synthesis gas is therefore more preferably not further cooled by means of indirect heat exchange with the nitrogen-rich gas until after it has at least once been scrub~ed with water. m e washing step results in an aqueous suspension of solid slag particles and synthesis gas that has substantially been purified of slag particles. m e aqueous suspension is separated frcm the synthesis gas and is advantageously at least partly recycled into the system. Suitable scrubbers are Venturi scrubbers and gas , ~2231.2~8 ~ 4 --scrubbers m which gas and ~ater are countercurrently contacted with each other.
In the scru~bing step the synthesis gas is already cooled down. By means of the indirect heat exchange with the nitrogen-rich gas the synthesis gas is further cooled preferably to atemperature of 40-140C.
As a result of the scrubbing step the synthesis gas contains much water va~our. The gas is preferably dried. This is most simply effected by cooling the synthesis gas to below the dew-point, as a result of which part of the water vapour condenses. Ifit is cooled to far belcw the dewpoint, the greater part of the water vapour condenses. Subsequently, the dry gas is separated from the condensate. The synthesis gas is preferably cooled to far below the dewpoint in a cooling treatment taking place after the indirect heat exchange with the nitrogen-rich gas. During said cooling the synthesis gas is advantageously cooled to a tempera-ture of 10-75C. The cooling can be carried out both with air and with water. Since the synthesis gas has already bee: cooled to 25-250C by means of indirect heat exchange with the nitrogen-rich gas, a relatively small cooler will suffice.
The nitrogen-rich gas heated according to the invention is preferably applied usefully for drying the solid fuel. Drying takes place before the fuel is fed into the gasification reactor.
If the solid fuel is supplied as not too coarse lumps, drying can be performed before it is passed to the grinding mill. If the fuel consists of large lu~ps, then it is more efficient to dry it during and/or after grinding. If the fuel has a high water con-tent, the hot nitrogen-rich gas, optionally after further heating, can be used to dry the fuel entirely or partly. In the latter case drying to the required water content takes place afterwards in another manner or with another hot gas. It is possible to use many types of grinding mills. Depending on the type of grinding mill drying takes place during or after grinding. For example, if a ball mill or a roller mill is used, the hot nitrogen-rich gas is introduced into the mill and already exercises its drying .
::
~2Z~2~
effect during gxinding. The hot nitrogen~rich gas is subsequently used to discharge ~le ground fuel from the grinding mill and dries the fuel particles during transport.
~efore the drying of the solid fuel the nitrogen-rich gas is preferably heated to a temperature in the range of 50 to 400C, depending on the water content of the fuel. For the greater part of the fuels a temperature of 90-150C is suitable. The lower temperature limit is such that just enough expelling power is available to remove the water present from the fuel. The upper temperature limit is determined by economic motives. The heat content of the synthesis gas is such that the required quantity of the nitrogen-rich gas can be heated to a temperature up to 400G.
As already stated before, the nitrogen-rich gas is preferably the waste nitrogen stream formed in the cryogenic distillation of air. The invention is not limited thereto. Use can be made of any nitrogen-rich gas originating from the air separation plant. If a nitrogen-rich gas having a relatively high oxygen content is used to dry the ground fuel, there is a risk of an explosive combustion of the fuel with the oxygen. Thexefore, the nitrogen-rich gas preferably contains less than 12~ by volume of oxygen, more preferably less than 10~ by volume. The waste nitrogen stream ccmplies with said requirements.
The invention is now further illustrated with reference to the Figures to which the invention is otherwise by no means limited. .~uxilial~ means, such as ccmpressors, pumps, valves, etc., are not shown in the diagrammatic figures.
In Fig. 1 a carbon-containing solid fuel is introduced into a grinding mill 2 via line 1. Via a line 3 a stream of hot nitrogen-rich gas is introduced into the grinding mill 2, where the gas 30 dries the finely ground fuel. Ground and dried fuel, together with the gas mixtuxe of inter alia nitrogen and water vapour, is conducted to a separator 5 through a line 4. Suitable separators are for example, bend separators, cyclones, filters etc. In the separator 5 the ground fuel is separated from the gas. The gas 35 mainly consisting of nitrogen and water vapour is vented through a ,. :;, "~
~.~2~L~38 line 7. m e separated fuel particles are passed to a reactor 8 through a line 6. (Since the gasification reactor 8 is preferably operated at elevated pressure, the fuel is brought to the desired press~e by means of compressors, supply vessels, locks etc. which are not shcwn in the Figure.) An oxygen-rich gas origlnating fro.m an air separation plant 10 is also introduced into the reactor 8 via a line 9. Air is fed into the air separation plant 10 via a line 11. In plant 10 are formed an oxygen rich gas stream that is passed to the reactox 8 via the line 9 and a substantially pure nitrcgen stream, which can at least partly be used in the trans-port of the fuel to the reactor through the line 6. (Said stream is not shown in the Figure.) The plant 10 also produces a waste nitrogen stream which is discharged via a line 12. The gasifica-tion of the carbon-containing fuel with the oxygen and a m~derator (steam or CO2) supplied via a line 13 takes place in the reactor 8. m e resulting synthesis gas loaded wi.th slag droplets is passed via a line 14 to a cooling zone 15 where it is cooled dawn by injecting a cooled ana purified recycled synthesis gas that is supplied via line 16. In the cooling zone 15 all slag droplets in the hot synthesis gas solidify. Via a line 17 a mixture of synthe sis gas and solid slag particles is discharged fro.m the cooling zone 15 and passed into a waste heat boiler 18 where it is cooled indirectly with water that is supplied via a line 19 and discharg-ed as steam via a line 20. Fro.m the waste heat boiler 18 the still warm mixture of synthesis gas and solid slag particles is passed to a Venturi tube 22 via a line 21. There it is contacted with a suspension of solid slag particles in water that is conducted to the Venturi tube 22 via a line 23. In the Venturi tube 22 all the water of the suspension evaporates and a mixture of synthesis gas, water vapour and solid slag particles is passed via a line 24 to a cyclone 25 where the greater part of the solid slag particles is separated from the gas mlxture and is discharged fram the installa-tion via a line 26. The remainder of the solid slag particles is passed, together with the gas mixture, via a line 27 Lnto a Venturi scrubber 28 where it is contacted with an aqueous suspen-~2;~:1238 sion of solid slag particles supplied via a line 29. The mixtureof synthesis gas, water vapour, drops of water and solid slag par-ticles formed in the Venturi scrubber 28 is conducted to a sepa-rator 31 via a line 30. Here an aqueous suspension of solid slag particles is separated from the gas mixture and discharged via the line 23 through which line the aqueous suspension is passed to the venturi tube 22. The mixture of synthesis gas and water vapour still containing a small quantity of solid slag particles is introduced via a line 32 into the lower part of a gas scrubber 33, where it is countercurrently contacted with water that is passed to the upper part of the column 33 via a line 35. In the column 33 the last residues of solid slag particles are removed from the gas mixture cwing to which an aqueous suspension of solid slag parti-cles is fonmed that is passed frcm the column 33 to the Venturi scrubber 28 via the line 29. The gas mixture that is now practical-ly free from solid slag particles is conducted via a line 34 to a ccoler 36 where the synthesis gas mixture.is further cooled by indirect heat exchange with the cold waste nitrogen stream from the line 12 and the waste nitrogen stream is heated. m e resulting hot stream is passed from the cooler 36 to the grinding mill 2 via the line 3. If the synthesis gas mixture is cooled to below the dewpoint in the cooler 36 a mixt~re of synthesis gas, water vapour and water is conducted via a line 37 to an air cooler 38 to which air is supplied via a line 39 and discharged via a line 40. Here cooling to far below the dewpoint takes place, owing to which `
substantially the whole quantity of water vapour condenses. If the synthesis gas mixture is cooled in the cooler 36 to a temperature : above the dewpoint of the gas mixture, the line 37 contains exclusively synthesis gas and water vapour. A mixture of a synthe-sis gas, condensation water and a small quantity of water vapour is passed frcm the cooler 38 to a separator 42 via a line 41. In the separator 42 the muxture is separated into condensate that is discharged via a line 43 and a substantially dry synthesis gas that is discharged via a line 44. Part of the condensate is recycled to the column 33 via the line 35. m e remaining part is ....
, ~22~3~3 8 ~
discharged from the apparatus via a line 45. Part of the substan-tially dry synthesis gas is recycled to the cooling zone 15 via the line 16. The remainLng part of synthesis gas is discharged as final product from the apparatus via`a line 46 for further proces-sing.
Fig. 2 shows another embodim~nt of the process according tothe invention. Said process is particularly suitable to be used for solid fuels containing a relatively large quantity of water.
Immediately after leaving the waste heat boiler 18 the synthesis 10 gas is passed via the line 21 to a heat exchanger 101 where it is cooled by means of a preheated stream of nitrogen-rich gas sup-plied to the heat exchanger 101 via a line 102 and discharged via a line 103 to the grinding mill 2. ~le cooled synthesis gas is passed via a line 105 to a Venturi tube 106. Here it is contacted 15 with a water stream via a line 107. All the water introduced evaporates in the Venturi tube 106. The gas mixture is passed via line 108 to a bag filter 109. Here the solid slag particles are separated from the gas mixture. The separated solid slag particles are discharged from the apparatus via a line 110. The gas mixture 20 is passed via a line 111 to the cooler 36 ~rom which it is conduc-ted to the cooler 38 via the line 37. Water vapour condenses in the coolers 36 and 38. After separation of the condensation water from the synthesis gas in the separator 42 part of the water is conducted to the Venturi tube 106 via the line 107. The cold 25 nitrogen-rich gas stream is introduced into the cooler 36 via the line 12 and after heating it is discharged via the line 3. me somewhat warm gas stream can be further heated by indirect heat exchange with superheated steam in a heat exchanger 104 to which the steam is supplied via a line 112 and from which it is discharg-30 ed via a line 113. To this end use can, for example, be made ofsteam obtained in the line 20. Instead of indirect heat exchange with steam it is also possible to use steam in~ection into the nitrogen-rich gas stream in order to raise the temperature of the gas stream. m e wanm nitrogen-rich gas stream is passed to the heat exchanger 101. Here it cools the synthesis gas further ~, ,, .
2~23~3 g and is further heated itself. m e hot gas stream is subsequently passed to the grinding mill 2 via the line 103 in order to dry the fuel.
EX~LE 1 By a process, as described in Fig. 1, 45.8 tons per hour (t/h) of coal having the following composition is passed to the mill 2:
C 67.3 % by wt.
H 4.4 "
N 1.5 "
O 5.9 "
S 2.9 "
ash 12.0 "
water 6.0 "
A quantity of 123.3 t/h of a nitrogen-rich gas stream of 120C is added thereto. The gas has the following composition:
N2~Ar 95 mole %
2 4 "
H20 1 "
The ground coal is separated from the gas in a filter 5. A quanti-ty of 43.93 tth of coal p~wder is passed to the reactor 8 via the line 6. 125.17 t/h of the nitrogen-rich gas with water vapour is vented via the line 7. The gas has a te~perat~re of 70C and the following ccmposition:
N2+Ax 92.8 mole %
2 3 9 "
H2O 3.3 "
The water content of the coal powder is still 2.0% by weightO The temperature of the synthesis gas generated in the reactor 8 is 360C in the line 21.
After the washing step wi~h water the temperature is still 130C. In the cooler 36 a quantity of 176.5 t/h of synthesis gas is cooled wlth 123.3 t/h nitrogen-rich gas of 10C. The tempera-ture of the resulting mixture of synthesis gas, water vapour and water is 122C; the nitrogen-rich gas is heated to 120C.
.
.
, .
3LZZ~238 In the cooler 33 the t~?erature of the synthesis gas-containing mlxture is reduced to 50C by air cooling, owing to which a total quantity of 19.1 t/h of water vapour condenses. After the separa-tion of the mixture in the separator 42 the line 45 discharges 1.55 t/h of water and the line 46 discharges 84.5 t/h of synthesis gas of the following composition frcm the apparatus:
CO 62.6 mole %
H2 27.6 "
C2 2.0 "
H2S 1.0 "
H2O 0.6 "
N2 5.6 "
Ar 1 . O "
EXAMæLE 2 In a process as described in Fig. 2 a quantity of 50 t/h of brcwn coal is passed to the mill 2. The brown coal has the follo~
wing ccmposition:
C 39.6 % by wt.
H 3.0 "
N 0.7 "
o 10.3 "
S 0.7 "
ash 10.8 "
water 34.9 "
135 t/h of nitrogen-rich gas of 370C having the following composi-tion is added thereto via the line 103:
N2+Ar 95 mole %
H20 1 "
After separation in filter 5 35.8 t/h of brown coal powder is conducted to the reactor 8 via the line 6 and 149.2 t/h of nitrogen-rich gas with water vapour is vented via the line 7, The vented . .
'':
.
~L22~2~8 gas has a temperature of 90C and the following camposition:
N2+Ar 81.6 mole %
2 3.4 "
H2O 15.0 "
The water content in the brown coal pcwder is still 9% by weight.
m e temperature of the synthesis gas generated in reactor 8 is 400C in the line 21. Said temperature is reduced to 220C in 5 the heat exchanger lO1, while the nitrogen-rich gas in the line 102 is heated from 180C to gas of 370C, which is passed to the mill 2 via the line 103. The gas leaving the bag filter lO9 still has a temperature of 180C. 103.1 t/h of synthesis gas is cooled in the cooler 36 to 98C with 135 t/h of cool nitrogen-rich gas of 10 10C. In thls cooling step the nitrogen-rich gas is heated to 160C. Said gas is further heated to 180C with steam in the heat exchanger 104, after which it is passed to the heat exchanger 101 via the line 102. The n~xture of s~nthesis gas, water vapour and water formed in the cooler 36 is cooled to 50C in the air cooler 15 38, owing to which a total quantity of 7.1 t/h of water vapour condenses. After the separation of the mixture in the separator 42 the line 45 discharges 5.4 t/h of water and the line 46 discharges 58.0 t/h of synthesis gas of the following composition frcm the apparatus:
CO 59.1 mole %
H2 28.1 C32 6.1 H~S 0.5 ll H2O 0.6 "
N2 4.4 "
Ar 1.2 "
.
EX~LE 1 By a process, as described in Fig. 1, 45.8 tons per hour (t/h) of coal having the following composition is passed to the mill 2:
C 67.3 % by wt.
H 4.4 "
N 1.5 "
O 5.9 "
S 2.9 "
ash 12.0 "
water 6.0 "
A quantity of 123.3 t/h of a nitrogen-rich gas stream of 120C is added thereto. The gas has the following composition:
N2~Ar 95 mole %
2 4 "
H20 1 "
The ground coal is separated from the gas in a filter 5. A quanti-ty of 43.93 tth of coal p~wder is passed to the reactor 8 via the line 6. 125.17 t/h of the nitrogen-rich gas with water vapour is vented via the line 7. The gas has a te~perat~re of 70C and the following ccmposition:
N2+Ax 92.8 mole %
2 3 9 "
H2O 3.3 "
The water content of the coal powder is still 2.0% by weightO The temperature of the synthesis gas generated in the reactor 8 is 360C in the line 21.
After the washing step wi~h water the temperature is still 130C. In the cooler 36 a quantity of 176.5 t/h of synthesis gas is cooled wlth 123.3 t/h nitrogen-rich gas of 10C. The tempera-ture of the resulting mixture of synthesis gas, water vapour and water is 122C; the nitrogen-rich gas is heated to 120C.
.
.
, .
3LZZ~238 In the cooler 33 the t~?erature of the synthesis gas-containing mlxture is reduced to 50C by air cooling, owing to which a total quantity of 19.1 t/h of water vapour condenses. After the separa-tion of the mixture in the separator 42 the line 45 discharges 1.55 t/h of water and the line 46 discharges 84.5 t/h of synthesis gas of the following composition frcm the apparatus:
CO 62.6 mole %
H2 27.6 "
C2 2.0 "
H2S 1.0 "
H2O 0.6 "
N2 5.6 "
Ar 1 . O "
EXAMæLE 2 In a process as described in Fig. 2 a quantity of 50 t/h of brcwn coal is passed to the mill 2. The brown coal has the follo~
wing ccmposition:
C 39.6 % by wt.
H 3.0 "
N 0.7 "
o 10.3 "
S 0.7 "
ash 10.8 "
water 34.9 "
135 t/h of nitrogen-rich gas of 370C having the following composi-tion is added thereto via the line 103:
N2+Ar 95 mole %
H20 1 "
After separation in filter 5 35.8 t/h of brown coal powder is conducted to the reactor 8 via the line 6 and 149.2 t/h of nitrogen-rich gas with water vapour is vented via the line 7, The vented . .
'':
.
~L22~2~8 gas has a temperature of 90C and the following camposition:
N2+Ar 81.6 mole %
2 3.4 "
H2O 15.0 "
The water content in the brown coal pcwder is still 9% by weight.
m e temperature of the synthesis gas generated in reactor 8 is 400C in the line 21. Said temperature is reduced to 220C in 5 the heat exchanger lO1, while the nitrogen-rich gas in the line 102 is heated from 180C to gas of 370C, which is passed to the mill 2 via the line 103. The gas leaving the bag filter lO9 still has a temperature of 180C. 103.1 t/h of synthesis gas is cooled in the cooler 36 to 98C with 135 t/h of cool nitrogen-rich gas of 10 10C. In thls cooling step the nitrogen-rich gas is heated to 160C. Said gas is further heated to 180C with steam in the heat exchanger 104, after which it is passed to the heat exchanger 101 via the line 102. The n~xture of s~nthesis gas, water vapour and water formed in the cooler 36 is cooled to 50C in the air cooler 15 38, owing to which a total quantity of 7.1 t/h of water vapour condenses. After the separation of the mixture in the separator 42 the line 45 discharges 5.4 t/h of water and the line 46 discharges 58.0 t/h of synthesis gas of the following composition frcm the apparatus:
CO 59.1 mole %
H2 28.1 C32 6.1 H~S 0.5 ll H2O 0.6 "
N2 4.4 "
Ar 1.2 "
.
Claims (5)
PROPERTY OR PRIVILEGE IS CLAIMED ARE DEFINED AS FOLLOWS:
1. A process for gasifying a solid carbon-containing fuel, wherein a) the fuel is ground fine and dried, b) the fuel is subsequently partially combusted to synthesis gas by means of oxygen or oxygen-enriched air, which oxygen originates from an air separation plant, c) the synthesis gas is cooled to a temperature of 100 °C-500 °C, and further comprising the step of d) further cooling the cooled synthesis gas to a temperature of 25-250 °C by means of indirect heat exchange with a nitrogen-rich gas originating from the air separation plant, wherein the nitrogen-rich gas thus heated is used to dry the solid carbon-containing fuel.
2. The process as claimed in claim 1, wherein the synthesis gas is further cooled by means of indirect heat exchange with the nitrogen-rich gas after the solid slag particles have at least partly been removed from the synthesis gas.
3. The process as claimed in claim 2, wherein the synthesis gas is further cooled to a temperature of 40-140 °C by means of in-direct heat exchange with the nitrogen-rich gas.
4, The process as claimed in claim 1, wherein after the in-direct heat exchange with the nitrogen-rich gas the synthesis gas is further cooled to a temperature of 10-75 °C in a cooler.
5. The process as claimed in claim 1, wherein the nitrogen-rich gas is heated to a temperature in the range of 50-400 °C.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| NL8201715A NL8201715A (en) | 1982-04-26 | 1982-04-26 | PROCESS FOR GASIFICATION OF A SOLID CARBON-FUEL FUEL. |
| NL8201715 | 1982-04-26 |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CA1221238A true CA1221238A (en) | 1987-05-05 |
Family
ID=19839653
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA000425271A Expired CA1221238A (en) | 1982-04-26 | 1983-04-06 | Process for the gasification of a solid carbon- containing fuel |
Country Status (7)
| Country | Link |
|---|---|
| EP (1) | EP0092856B1 (en) |
| JP (1) | JPS58194987A (en) |
| AU (1) | AU550402B2 (en) |
| CA (1) | CA1221238A (en) |
| DE (1) | DE3371358D1 (en) |
| NL (1) | NL8201715A (en) |
| ZA (1) | ZA832885B (en) |
Families Citing this family (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE3446715A1 (en) * | 1984-12-21 | 1986-06-26 | Krupp Koppers GmbH, 4300 Essen | METHOD FOR COOLING PARTIAL OXIDATION GAS CONTAINING DUST-BASED IMPURITIES, INTENDED FOR USE IN A COMBINED GAS STEAM TURBINE POWER PLANT |
| JPH0678531B2 (en) * | 1986-06-11 | 1994-10-05 | 株式会社日立製作所 | Coal gasification method and apparatus |
| DE4103362C1 (en) * | 1991-02-05 | 1992-04-23 | Voest Alpine Ind Anlagen | |
| AU730980B2 (en) * | 1996-05-20 | 2001-03-22 | Babcock-Hitachi Kabushiki Kaisha | Coal gasification apparatus and a coal gasification hybrid power generation system |
| AUPO910097A0 (en) * | 1997-09-10 | 1997-10-02 | Generation Technology Research Pty Ltd | Power generation process and apparatus |
| US7503947B2 (en) * | 2005-12-19 | 2009-03-17 | Eastman Chemical Company | Process for humidifying synthesis gas |
| EP2119668A3 (en) * | 2008-05-16 | 2012-04-18 | Haldor Topsoe A/S | Process for the preparation of synthesis gas from black liquor |
| JP2010059383A (en) * | 2008-09-08 | 2010-03-18 | Mitsubishi Heavy Ind Ltd | Gasification furnace apparatus |
| US8349036B2 (en) * | 2010-01-06 | 2013-01-08 | General Electric Company | Systems and method for heating and drying solid feedstock in a gasification system |
| EP2487439B1 (en) * | 2011-02-14 | 2019-05-08 | General Electric Technology GmbH | Method and system for milling a fuel for an oxy-fuel combustion burner |
| CN102604685B (en) * | 2011-12-29 | 2014-11-26 | 武汉凯迪工程技术研究总院有限公司 | Biomass synthesis gas positive pressure purification process and system configuration for oil production |
Family Cites Families (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB1370410A (en) * | 1973-01-26 | 1974-10-16 | Texaco Development Corp | Multi-hydrotorting of coal |
| US3976442A (en) * | 1974-12-18 | 1976-08-24 | Texaco Inc. | Synthesis gas from gaseous CO2 -solid carbonaceous fuel feeds |
| DE2503193A1 (en) * | 1975-01-27 | 1976-07-29 | Linde Ag | PROCESS FOR PRODUCING A HEATING GAS BY PRESSURE GASIFICATION OF CARBON FUELS |
| US4152122A (en) * | 1977-12-05 | 1979-05-01 | Syngas International, Ltd. | Apparatus for the production of methane containing gas by hydrogasification |
| US4158948A (en) * | 1978-08-16 | 1979-06-26 | Texaco Inc. | Conversion of solid fuels into fluid fuels |
| DD143712A3 (en) * | 1978-08-18 | 1980-09-10 | Manfred Schingnitz | PROCESS FOR PROVISION OF PROCESS STEAM IN INTEGRATED BROWN COATING PLANTS |
| US4272256A (en) * | 1979-10-15 | 1981-06-09 | Koppers Company Inc. | Method for heating oxygen containing gas in conjunction with a gasification system |
-
1982
- 1982-04-26 NL NL8201715A patent/NL8201715A/en not_active Application Discontinuation
-
1983
- 1983-03-28 DE DE8383200434T patent/DE3371358D1/en not_active Expired
- 1983-03-28 EP EP83200434A patent/EP0092856B1/en not_active Expired
- 1983-04-06 CA CA000425271A patent/CA1221238A/en not_active Expired
- 1983-04-22 AU AU13867/83A patent/AU550402B2/en not_active Ceased
- 1983-04-25 ZA ZA832885A patent/ZA832885B/en unknown
- 1983-04-25 JP JP58071566A patent/JPS58194987A/en active Pending
Also Published As
| Publication number | Publication date |
|---|---|
| NL8201715A (en) | 1983-11-16 |
| DE3371358D1 (en) | 1987-06-11 |
| AU550402B2 (en) | 1986-03-20 |
| EP0092856A3 (en) | 1984-07-04 |
| EP0092856A2 (en) | 1983-11-02 |
| JPS58194987A (en) | 1983-11-14 |
| AU1386783A (en) | 1983-11-03 |
| EP0092856B1 (en) | 1987-05-06 |
| ZA832885B (en) | 1984-01-25 |
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