CA2176354A1 - A method of reducing hydrogen halide(s) content in synthesis gas - Google Patents
A method of reducing hydrogen halide(s) content in synthesis gasInfo
- Publication number
- CA2176354A1 CA2176354A1 CA002176354A CA2176354A CA2176354A1 CA 2176354 A1 CA2176354 A1 CA 2176354A1 CA 002176354 A CA002176354 A CA 002176354A CA 2176354 A CA2176354 A CA 2176354A CA 2176354 A1 CA2176354 A1 CA 2176354A1
- Authority
- CA
- Canada
- Prior art keywords
- alkali metal
- metal compound
- gas
- hydrogen halide
- solids
- 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.)
- Abandoned
Links
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/68—Halogens or halogen compounds
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K1/00—Purifying combustible gases containing carbon monoxide
- C10K1/20—Purifying combustible gases containing carbon monoxide by treating with solids; Regenerating spent purifying masses
Abstract
A method for reducing the hydrogen halide(s) content of a synthesis gas stream by gasifying a carbonaceous feed material in a gasifier to produce a gas/solids mixture of hydrogen, carbon monoxide, hydrogen halide gas, and fly slag particles; passing the gas/solids mixture to a solids removal zone where at least a portion of the fly slag particles are removed, to produce a gas stream; admixing with the said gas stream an alkali metal oxide, hydroxide, bicarbonate, or carbonate to produce an alkali metal compound/gas mixture; passing the alkali metal compound/gas mixture to a means for increasing the contact time between said hydrogen halide(s) and said alkali metal compound(s) or their thermal docomposition products; reacting the alkali metal compound(s) with the said hydrogen halide(s) to produce solid alkali metal halide(s); and recovering a gas stream substantially free of hydrogen halide(s) and solids.
Description
~ WO 95/13340 2 ~ 7 ~ 3 c~ ~ r~ 99 A METHOD OF REDUCING HYDROGEN HALIDE(S) CONTENT IN SYNTHESIS GAS
The invention relates to a method for reducing hydrogen halide(s) content, in particular hydrog~n chloride content, of a aynthesis gas stream.
The combu~tion of a ~-A rhnn~ material ~uch ~ olid ~-~rhnn~ fuel by reaction with a ~ource of gaseous oxygen is well known. In such a reaction, ~m amount of air or oxygen equal to or greater than that required for complete combu~tion i~ u~ed, whereby the gaseous effluent contains c~rbon dioxide with little, if any, carbon monoxide. It is also known to carry out the gasification or partial oxidation of ~olid ~-~rhnnAn~ollc materials or fuels employing a limited quantity of oxygen or air so as to produce primarily carbon monoxide and hydrogen.
Fuel sources, in particular coals, often have an ~n~ ;rJhl -halide~s) content. The halogen~ in the halides, in p~rticular chlorine in chloridea and fluorine in fluorides, form Acids in the synthesis gas mixture which can cause severe corrosion in the downstream rro~ ; n7 equipment . The halides also poae environmental ~nd ~afety hazards if emitted to the atmo~phere.
Another problem c~u~ed by the halides is reduced efficiency of the gasification process. Condensation of some salts in the synthesis gas during cooling limits the overall efficiency of the heat recovery from the synthesis gas. This limitation in heat recovery occurs becauae some moderate sublimation ~ -r~t~re salts, such as ammonium chloride, are very corro~ive when per~itted to condense. Thus, to avoid having the ~alts conden~e, the synthesis gaJ cannot be cooled below the sublimation t- r~tl~re of various ~alts. Since the t- -r.~t--re to which the synthesis ga~ may be cooled is thus limited, the heat recovery from the gas is nrriin71y limited. In particular, chlorine-~nnt~tn;n7 salts are 30 formed due to the pre~ence of NCl. By removing HCl from the 2 ~ 7 ~ 699~
synthesis gas, formation of such salts in the gas stream is reduced or eliminated and the gas can be cooled further to permit more thermal recovery.
A prlor known method of removing HCl is by a wet absorption system. In this known method the synthesls gas must be cooled and passed through an aqueous absorption column. The HCl is absorbed in the water and neutralized with NaOH. This method has drawbacks since cooling the gas to remove the HCl is inefficient and results in heat/energy 109s. Also, additional equipment costs and ~-;ntPnAn~P costs result from the addition of an absorption column to the process. E:conomic drawbacks also result from the need for a large water treatment plant due to a build-up of salts in the water from the absorption column.
It is known from U.S. Patent Specification No. 5,118,480 to add metal-containing compounds such as nahcolite to a synthesis gas downstream of the gasifier to remove HCl in conjunction with removing sulphur with a metal oxide sorbent. However, this process fails to address the problem of high cxpense associated with long piping necessary to have sufficient residence time for complete reaction.
It is therefore an object of the present invention to provide a practical and economical dry method of reducing the hydrogen halide (s) content of synthesis gas, without the high expense of long piping .
The invention provides a method for reducing the hydrogen halide(s) content of a synthesis gas stream comprising the steps of:
(a) gasifying a carbonaceous feed material in a gasifier under g2sifying conditions thereby producing a gas/solids mixture comprising hydrogen, carbon monoxide, one or more hydrogen halides, and fly slag particles;
(b) passing the said gas/solids rixture to a solids removal zone wherein at least a portion of the fly sl~g particles are removed, thereby producing a gas stream:
(c) admixing with the said gas stream obtained in step (b) at least an alkali metal compound, thereby producing an alkali metal WO 95/13340 2 1 7 B 3 ~ 4 P~ 699 compound/gas mixture~
(d) passing the said alkali metal compound/gas mixture obtained in step ~c~ to a means for increasing the contact time between the hydrogen halide~s) and the alkali metal compound~s) or their thermal decomposition products;
~e) reacting the alkali metal compound~s) or thermal decomposition products thereof, with the hydrogen halide~s) thereby producing solid alkali metal halide~s), wherein a cake of solids builds up on the surface of the said means for increasing the contact time between the hydrogen halide~s) and the alkali metal compound(s) or their thermal decomposition products;
(f) periodically removing at least a portion of the c~ke of solids;
and ~g) recoverlng from the said means for increasing the contact time between the hydrogen halide(s) and the alkali metal compound(s) or their thermal decomposition products a gas stream substantially free of hydrogen halide~s).
The invention will now be described in more detail by way of example by reference to specific process aspects thereof.
A. Feeds and alkali metal Compounds and Mixture Thereof Several types of carbonaceous materials are suitable as feed sources for gasification. These include bituminous coal, sub-bituminous coal, anthracite coal, lignite, li~juid hydrocarbons, petroleum coke, various organic scrap materials, munlcipal refuse, solid organic refuse contaminated with radioactive materi21s, paper industry refuse, and photographic scrap. Coal and petroleum coke are considered advantageous feeds.
The alkali metal compounds include for example potassium oxide, pota~sium hydroxide, potassium bicarbonate, potassium carbonate, sodium oxide, sodium hydroxide, sodium bicarbonate, and sodium carbonate. Nahcolite, a naturally occurring form of sodium bicarbonate, is advantageously applied for its economy and availability. The alkali metal compounds are optionally used individually or in combination.
The alkali metal compounds are mixed with the synthesis gas WO 9S113340 63 5 ~ 699--~fter the synthesis gas leaves the gasifier. AdvAn~ o- cly, an ~ntrained flow gasifier is applied. The alkali metal compound is in~ected, advantageously dry, into the synthesis gas stream in any way suitable for the purpos~. It i3 transported pneumatlcally in nitrogen or carbon dioxide or in any other conventional dry feed manner. Adv~n'r~g~ cl y, at least a portion of the sensible heat of the synthesis gas is recovered prior to adding the alkali metal compound. I~ore in particular, the synthesis gas passes through a first heat recovery zone, a solids removal zone, then a second heat recovery zone, and then the alkali metal compound is injected into the gas stream recovered from the second heat recovery zone.
The solids removal stage is advantageously a cyclone or ceramic candle filter, used individually or in combination. An electrostatic precipitator is optionally us~d where the system pressure is at or near atmospheric. Advantageously, the maximum amount of sensible heat is recovered which does not reduce the temperature of the synthesis gas below the condensation point of any chloride compounds present in the synthesis gas. Such condensation results in equipment corrosion problems.
B. Reaction, Cooling, and Solids Removal Sy way of example reference will in particular be made to the dry removal of hydrogen chloride from synthesis gas. However, it will be appreciated by those skilled in the art that the method of the invention is also applica}~le for removal of other hydrogen halide(s) from synthesis gas.
After the alkali metal compound i5 injected it will react with the halogen e. g. chlorine in the hydrogen halide e. g. hydrogen chloride to form a solid salt. The alkali metal compound either reacts directly with the hydrogen halide or the alkali metal compound may first thermally decompose prior to such reaction.
Where the alkali metal compound is a sodium compound, e.g., sodium bicarbonate, sodium halide is formed. The resulting alkali metal halide is a solid.
I'he solid-salt-containing synthesis gas stream then passes to a means for increasing the contact time between the hydrogen halide(s) WO 95rl334~1 2 1 7 G 3 ~ ~ p~ "~ , 99 and the alkali metal compound~s) e.g. a (c~ramic candle) ~ilter.
Additionally, much of the reaction between the alkali metal compound and the hydrogen halide occurs on the upstream surface of the (ceramic candle) filter. This is because the residence time between - 5 the point of alkali metal compound in~ection and the filter willtypically be too short for complete reaction. Extension of the pathway to increase the residence time wouLd be uneconomical.
A cake of salt solids builds up on the surface of the (ceramic candle) filter. For the synthesis gas to get through the cake to exit the filter, it must travel 2 convoluted pathway through the solids cake. Thus, the contact time between the hydrogen halide(s) and the alkali metal compound(s) or their thermal decomposition products is increased to provide a longer effective residence time without the uneconomical expense of lengthening the piping.
The synthesis gas recovered from the (ceramic candle) filter h~s r~duced amounts of hydrogen halides, e.g. hydrogen chloride, 2nd is advantageously substantially free of hydrogen halides, e. g.
hydrogen chloride. Advantageously, the synthesis gas is then passed to a third heat recovery ::one, to maximi~e sensible heat recovery before passing the synthesis gas to any wet cleanup units, such as a sulphur removal scrubbing unit.
C. Concentrations of halides, l~atios, and Percent Removal In the reducing atmosphere and elevated temperatures of the gasifier, a halide such as chloride in the coal evolves into 2~ hydrogen chloride. The initial concentrations of hydrogen chloride and other hydrogen halides in the synthesis gas vary widely with the type and source of the feed to the gasifier. Chloride concentrations in coal range from about 0. 01~ by weight chlorine to about O . 3~ by weight chlorine . Other halide concentrations in co~l are typicalLy much lower than chloride concentrations.
At least a stoichiometric amount of alkali metal compounds must be mixed with the synthesis gas with respect to the halide concentration in the synthesis gas. Advantageously, one to three times the stoichiometric ratio 15 used of alkali metal compounds to halides such as chlorides. This assures a high degree of removal of 111~1 1 ~n ~ ~5~
WO95/13340 ~ 63~ - 6-the chlorides. More than about three timea the stoichiometric ratio is wasteful of alkali metal compounds and makes the process uneconomical without any apparent benefit.
From about 959~ by weight to about 999 by welght of the halides ~.
such as chlorides, are removed in the practice of this method. For example, the synthesis gas will initially contaln from about 10 ppm by volume (ppmv) to about 1000 ppmv chloride where the feed is coal.
After gasification and reaction and Jolids removal of the metal halides, the concentration of chloride ln the synthesis gas is from about 0.1 ppmv to about S ppmv.
D. Operating Conditlons _ The gasifier is advAnt~7oo~ y an entrained flow gasifier and is operated at gasifying conditlons. These conditions are known to an expert and may vary from feed to feed. The temperature is a temperature high enough to gasify a substantial portion of the carbonaceous fe~d and to prevent the formation of lln~C~ r~ ' side-products, such as tars and phenols and other aromatics. Typical temperatures in the gasifier are from about 1100C to about 2000C.
Where the feed is coal, the gasifier temperature is advantageously from about 1450C to about 1575C. More in particular, the temperature is from about 1475C to about 1510C. The pressure of the gasifier is from about 14 bar to about 42 bar. AdvAnt~7~ cly, the pressure is from about 21 bar to about 31.5 bar.
At the point of injection of the alkali metal compound the ~ynthesis gas t~ . rAtllre is above the point at which any corrosive ammonium halide compounds, such as ammonium chlorides, will condense. This temperature varies with the type and concentration of halide compound. This is typically at least about 150 C. The temperature at the point of in~ection, however, is adV~ntAg~ cl y not above the condensation point of sodium chloride. This is typically below about 670 C~ This limitation ls necessary since sodium chloride must be a solid to be removed by the (ceramic c~ndle) filter. It is not essential, however, that the temperature at the point of in~ection be above the point of condensation of ~odium chloride, so long as the mixture reaches this temperature ~ WO~5113340 2 17 6 3 ~ 4 PCTIEP9~103699 prior to reaching the upstream surface of the (ceramic c~ndle) filter. Advantageously, the t~, r~t~lre of the synthesis gas stream at the point of alkali metal compound in~ection is from about 180 C
to about 370 C, more in particular from about 230 C to about 260 C.
Various modifications of the present inYention will become apparent to those skilled in the art from the foregoing description.
Such modifications are intended to fall within the scope of the appended claims.
The invention relates to a method for reducing hydrogen halide(s) content, in particular hydrog~n chloride content, of a aynthesis gas stream.
The combu~tion of a ~-A rhnn~ material ~uch ~ olid ~-~rhnn~ fuel by reaction with a ~ource of gaseous oxygen is well known. In such a reaction, ~m amount of air or oxygen equal to or greater than that required for complete combu~tion i~ u~ed, whereby the gaseous effluent contains c~rbon dioxide with little, if any, carbon monoxide. It is also known to carry out the gasification or partial oxidation of ~olid ~-~rhnnAn~ollc materials or fuels employing a limited quantity of oxygen or air so as to produce primarily carbon monoxide and hydrogen.
Fuel sources, in particular coals, often have an ~n~ ;rJhl -halide~s) content. The halogen~ in the halides, in p~rticular chlorine in chloridea and fluorine in fluorides, form Acids in the synthesis gas mixture which can cause severe corrosion in the downstream rro~ ; n7 equipment . The halides also poae environmental ~nd ~afety hazards if emitted to the atmo~phere.
Another problem c~u~ed by the halides is reduced efficiency of the gasification process. Condensation of some salts in the synthesis gas during cooling limits the overall efficiency of the heat recovery from the synthesis gas. This limitation in heat recovery occurs becauae some moderate sublimation ~ -r~t~re salts, such as ammonium chloride, are very corro~ive when per~itted to condense. Thus, to avoid having the ~alts conden~e, the synthesis gaJ cannot be cooled below the sublimation t- r~tl~re of various ~alts. Since the t- -r.~t--re to which the synthesis ga~ may be cooled is thus limited, the heat recovery from the gas is nrriin71y limited. In particular, chlorine-~nnt~tn;n7 salts are 30 formed due to the pre~ence of NCl. By removing HCl from the 2 ~ 7 ~ 699~
synthesis gas, formation of such salts in the gas stream is reduced or eliminated and the gas can be cooled further to permit more thermal recovery.
A prlor known method of removing HCl is by a wet absorption system. In this known method the synthesls gas must be cooled and passed through an aqueous absorption column. The HCl is absorbed in the water and neutralized with NaOH. This method has drawbacks since cooling the gas to remove the HCl is inefficient and results in heat/energy 109s. Also, additional equipment costs and ~-;ntPnAn~P costs result from the addition of an absorption column to the process. E:conomic drawbacks also result from the need for a large water treatment plant due to a build-up of salts in the water from the absorption column.
It is known from U.S. Patent Specification No. 5,118,480 to add metal-containing compounds such as nahcolite to a synthesis gas downstream of the gasifier to remove HCl in conjunction with removing sulphur with a metal oxide sorbent. However, this process fails to address the problem of high cxpense associated with long piping necessary to have sufficient residence time for complete reaction.
It is therefore an object of the present invention to provide a practical and economical dry method of reducing the hydrogen halide (s) content of synthesis gas, without the high expense of long piping .
The invention provides a method for reducing the hydrogen halide(s) content of a synthesis gas stream comprising the steps of:
(a) gasifying a carbonaceous feed material in a gasifier under g2sifying conditions thereby producing a gas/solids mixture comprising hydrogen, carbon monoxide, one or more hydrogen halides, and fly slag particles;
(b) passing the said gas/solids rixture to a solids removal zone wherein at least a portion of the fly sl~g particles are removed, thereby producing a gas stream:
(c) admixing with the said gas stream obtained in step (b) at least an alkali metal compound, thereby producing an alkali metal WO 95/13340 2 1 7 B 3 ~ 4 P~ 699 compound/gas mixture~
(d) passing the said alkali metal compound/gas mixture obtained in step ~c~ to a means for increasing the contact time between the hydrogen halide~s) and the alkali metal compound~s) or their thermal decomposition products;
~e) reacting the alkali metal compound~s) or thermal decomposition products thereof, with the hydrogen halide~s) thereby producing solid alkali metal halide~s), wherein a cake of solids builds up on the surface of the said means for increasing the contact time between the hydrogen halide~s) and the alkali metal compound(s) or their thermal decomposition products;
(f) periodically removing at least a portion of the c~ke of solids;
and ~g) recoverlng from the said means for increasing the contact time between the hydrogen halide(s) and the alkali metal compound(s) or their thermal decomposition products a gas stream substantially free of hydrogen halide~s).
The invention will now be described in more detail by way of example by reference to specific process aspects thereof.
A. Feeds and alkali metal Compounds and Mixture Thereof Several types of carbonaceous materials are suitable as feed sources for gasification. These include bituminous coal, sub-bituminous coal, anthracite coal, lignite, li~juid hydrocarbons, petroleum coke, various organic scrap materials, munlcipal refuse, solid organic refuse contaminated with radioactive materi21s, paper industry refuse, and photographic scrap. Coal and petroleum coke are considered advantageous feeds.
The alkali metal compounds include for example potassium oxide, pota~sium hydroxide, potassium bicarbonate, potassium carbonate, sodium oxide, sodium hydroxide, sodium bicarbonate, and sodium carbonate. Nahcolite, a naturally occurring form of sodium bicarbonate, is advantageously applied for its economy and availability. The alkali metal compounds are optionally used individually or in combination.
The alkali metal compounds are mixed with the synthesis gas WO 9S113340 63 5 ~ 699--~fter the synthesis gas leaves the gasifier. AdvAn~ o- cly, an ~ntrained flow gasifier is applied. The alkali metal compound is in~ected, advantageously dry, into the synthesis gas stream in any way suitable for the purpos~. It i3 transported pneumatlcally in nitrogen or carbon dioxide or in any other conventional dry feed manner. Adv~n'r~g~ cl y, at least a portion of the sensible heat of the synthesis gas is recovered prior to adding the alkali metal compound. I~ore in particular, the synthesis gas passes through a first heat recovery zone, a solids removal zone, then a second heat recovery zone, and then the alkali metal compound is injected into the gas stream recovered from the second heat recovery zone.
The solids removal stage is advantageously a cyclone or ceramic candle filter, used individually or in combination. An electrostatic precipitator is optionally us~d where the system pressure is at or near atmospheric. Advantageously, the maximum amount of sensible heat is recovered which does not reduce the temperature of the synthesis gas below the condensation point of any chloride compounds present in the synthesis gas. Such condensation results in equipment corrosion problems.
B. Reaction, Cooling, and Solids Removal Sy way of example reference will in particular be made to the dry removal of hydrogen chloride from synthesis gas. However, it will be appreciated by those skilled in the art that the method of the invention is also applica}~le for removal of other hydrogen halide(s) from synthesis gas.
After the alkali metal compound i5 injected it will react with the halogen e. g. chlorine in the hydrogen halide e. g. hydrogen chloride to form a solid salt. The alkali metal compound either reacts directly with the hydrogen halide or the alkali metal compound may first thermally decompose prior to such reaction.
Where the alkali metal compound is a sodium compound, e.g., sodium bicarbonate, sodium halide is formed. The resulting alkali metal halide is a solid.
I'he solid-salt-containing synthesis gas stream then passes to a means for increasing the contact time between the hydrogen halide(s) WO 95rl334~1 2 1 7 G 3 ~ ~ p~ "~ , 99 and the alkali metal compound~s) e.g. a (c~ramic candle) ~ilter.
Additionally, much of the reaction between the alkali metal compound and the hydrogen halide occurs on the upstream surface of the (ceramic candle) filter. This is because the residence time between - 5 the point of alkali metal compound in~ection and the filter willtypically be too short for complete reaction. Extension of the pathway to increase the residence time wouLd be uneconomical.
A cake of salt solids builds up on the surface of the (ceramic candle) filter. For the synthesis gas to get through the cake to exit the filter, it must travel 2 convoluted pathway through the solids cake. Thus, the contact time between the hydrogen halide(s) and the alkali metal compound(s) or their thermal decomposition products is increased to provide a longer effective residence time without the uneconomical expense of lengthening the piping.
The synthesis gas recovered from the (ceramic candle) filter h~s r~duced amounts of hydrogen halides, e.g. hydrogen chloride, 2nd is advantageously substantially free of hydrogen halides, e. g.
hydrogen chloride. Advantageously, the synthesis gas is then passed to a third heat recovery ::one, to maximi~e sensible heat recovery before passing the synthesis gas to any wet cleanup units, such as a sulphur removal scrubbing unit.
C. Concentrations of halides, l~atios, and Percent Removal In the reducing atmosphere and elevated temperatures of the gasifier, a halide such as chloride in the coal evolves into 2~ hydrogen chloride. The initial concentrations of hydrogen chloride and other hydrogen halides in the synthesis gas vary widely with the type and source of the feed to the gasifier. Chloride concentrations in coal range from about 0. 01~ by weight chlorine to about O . 3~ by weight chlorine . Other halide concentrations in co~l are typicalLy much lower than chloride concentrations.
At least a stoichiometric amount of alkali metal compounds must be mixed with the synthesis gas with respect to the halide concentration in the synthesis gas. Advantageously, one to three times the stoichiometric ratio 15 used of alkali metal compounds to halides such as chlorides. This assures a high degree of removal of 111~1 1 ~n ~ ~5~
WO95/13340 ~ 63~ - 6-the chlorides. More than about three timea the stoichiometric ratio is wasteful of alkali metal compounds and makes the process uneconomical without any apparent benefit.
From about 959~ by weight to about 999 by welght of the halides ~.
such as chlorides, are removed in the practice of this method. For example, the synthesis gas will initially contaln from about 10 ppm by volume (ppmv) to about 1000 ppmv chloride where the feed is coal.
After gasification and reaction and Jolids removal of the metal halides, the concentration of chloride ln the synthesis gas is from about 0.1 ppmv to about S ppmv.
D. Operating Conditlons _ The gasifier is advAnt~7oo~ y an entrained flow gasifier and is operated at gasifying conditlons. These conditions are known to an expert and may vary from feed to feed. The temperature is a temperature high enough to gasify a substantial portion of the carbonaceous fe~d and to prevent the formation of lln~C~ r~ ' side-products, such as tars and phenols and other aromatics. Typical temperatures in the gasifier are from about 1100C to about 2000C.
Where the feed is coal, the gasifier temperature is advantageously from about 1450C to about 1575C. More in particular, the temperature is from about 1475C to about 1510C. The pressure of the gasifier is from about 14 bar to about 42 bar. AdvAnt~7~ cly, the pressure is from about 21 bar to about 31.5 bar.
At the point of injection of the alkali metal compound the ~ynthesis gas t~ . rAtllre is above the point at which any corrosive ammonium halide compounds, such as ammonium chlorides, will condense. This temperature varies with the type and concentration of halide compound. This is typically at least about 150 C. The temperature at the point of in~ection, however, is adV~ntAg~ cl y not above the condensation point of sodium chloride. This is typically below about 670 C~ This limitation ls necessary since sodium chloride must be a solid to be removed by the (ceramic c~ndle) filter. It is not essential, however, that the temperature at the point of in~ection be above the point of condensation of ~odium chloride, so long as the mixture reaches this temperature ~ WO~5113340 2 17 6 3 ~ 4 PCTIEP9~103699 prior to reaching the upstream surface of the (ceramic c~ndle) filter. Advantageously, the t~, r~t~lre of the synthesis gas stream at the point of alkali metal compound in~ection is from about 180 C
to about 370 C, more in particular from about 230 C to about 260 C.
Various modifications of the present inYention will become apparent to those skilled in the art from the foregoing description.
Such modifications are intended to fall within the scope of the appended claims.
Claims (16)
1. A method for reducing the hydrogen halide(s) content of a synthesis gas stream comprising the steps of:
(a) gasifying a carbonaceous feed material in a gasifier under gasifying conditions thereby producing a gas/solids mixture comprising hydrogen, carbon monoxide, one or more hydrogen halides, and fly slag particles;
(b) passing said gas/solids mixture to a solids removal zone wherein at least a portion of said fly slag particles are removed, thereby producing a gas stream;
(c) admixing with the said gas stream obtained in step (b) at least an alkali metal compound, thereby producing an alkali metal compound/gas mixture; characterized by the step of (d) passing the said alkali metal compound/gas mixture obtained in step (c) to a means for increasing the contact time between the said hydrogen halide(s) and the said alkali metal compound(s) or their thermal decomposition products; step (d) being carried out prior to passing the said synthesis gas stream to downstream processing equipment;
(e) reacting said alkali metal compound(s), or thermal decomposition products thereof, with said hydrogen halide(s) thereby producing solid alkali metal halide(s), wherein a cake of solids builds up on the surface of the said means for increasing the contact time between the said hydrogen halide(s) and the said alkali metal compound(s) or their thermal decomposition products;
(f) periodically removing at least a portion of said cake of solids; and (g) recovering from the said means for increasing the contact time between the said hydrogen halide(s) and the said alkali metal compound(s) or their thermal decomposition products a gas stream substantially free of hydrogen halide(s).
(a) gasifying a carbonaceous feed material in a gasifier under gasifying conditions thereby producing a gas/solids mixture comprising hydrogen, carbon monoxide, one or more hydrogen halides, and fly slag particles;
(b) passing said gas/solids mixture to a solids removal zone wherein at least a portion of said fly slag particles are removed, thereby producing a gas stream;
(c) admixing with the said gas stream obtained in step (b) at least an alkali metal compound, thereby producing an alkali metal compound/gas mixture; characterized by the step of (d) passing the said alkali metal compound/gas mixture obtained in step (c) to a means for increasing the contact time between the said hydrogen halide(s) and the said alkali metal compound(s) or their thermal decomposition products; step (d) being carried out prior to passing the said synthesis gas stream to downstream processing equipment;
(e) reacting said alkali metal compound(s), or thermal decomposition products thereof, with said hydrogen halide(s) thereby producing solid alkali metal halide(s), wherein a cake of solids builds up on the surface of the said means for increasing the contact time between the said hydrogen halide(s) and the said alkali metal compound(s) or their thermal decomposition products;
(f) periodically removing at least a portion of said cake of solids; and (g) recovering from the said means for increasing the contact time between the said hydrogen halide(s) and the said alkali metal compound(s) or their thermal decomposition products a gas stream substantially free of hydrogen halide(s).
2. The method as claimed in claim 1 wherein the carbonaceous feed material is coal or petroleum coke.
3. The method as claimed in claim 2, wherein the carbonaceous feed material is bituminous coal or sub-bituminous coal.
4. The method as claimed in any one of claims 1-3, wherein the amount of alkali metal compound(s) admixed with the effluent of said solids removal zone is at least a stoichiometric amount of alkali metal compounds with respect to the hydrogen halide(s) content of the synthesis gas.
5. The method as claimed in claim 4, wherein the amount of alkali metal compound(s) admixed with the effluent of said solids removal zone is not more than about 3 times the stoichiometric amount of alkali metal compounds with respect to the hydrogen halide(s) content of the synthesis gas.
6. The method as claimed in any one of claims 1-5, wherein said admixing step (c) consists essentially of injecting said alkali metal compound into said effluent of said solids removal zone.
7. The method as claimed in any one of claims 1-6, wherein in admixing step (c) the said alkali metal compound is dry at the point of admixture.
8. The method as claimed in any one of claims 1-7, wherein at least a portion of the sensible heat of the gas/solids mixture is recovered prior to adding the alkali metal compound.
9. The method as claimed in claim 8, wherein the gas/solids mixture is passed through a first heat recovery zone, a solids removal zone, then a second heat recovery zone, and then the alkali metal compound is injected into the gas stream recovered from the second heat recovery zone.
10. The method according to any one of claims 1-9, wherein the temperature in the gasifier is from about 1100°C to about 2000°C.
11. The method according to any one of claims 1-10, wherein the pressure in the gasifier is from about 14 bar to about 42 bar.
12. The method as claimed in any one of claims 1-11, wherein the said means for increasing the contact time is a filter.
13. The method as claimed in claim 12, wherein the filter is a ceramic candle filter.
14. The method as claimed in any one of claims 1-13, wherein the alkali metal compound comprises at least one oxide, hydroxide, bicarbonate or carbonate of an alkali metal.
15. The method as claimed in any one of claims 1-14, wherein the alkali metal is sodium or potassium.
16. The method as claimed in any one of claims 1-15, wherein the substantially hydrogen-halide-free gas stream is passed to a third heat recovery zone wherein a portion of the sensible heat of the said substantially hydrogen-halide-free gas stream is recovered.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US08/153,591 USH1539H (en) | 1993-11-12 | 1993-11-12 | Method of reducing hydrogen chloride in synthesis gas |
| US153591 | 1993-11-12 |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CA2176354A1 true CA2176354A1 (en) | 1995-05-18 |
Family
ID=22547849
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA002176354A Abandoned CA2176354A1 (en) | 1993-11-12 | 1994-11-08 | A method of reducing hydrogen halide(s) content in synthesis gas |
Country Status (9)
| Country | Link |
|---|---|
| US (1) | USH1539H (en) |
| EP (1) | EP0728172A1 (en) |
| JP (1) | JPH09504822A (en) |
| KR (1) | KR960705903A (en) |
| CN (1) | CN1135233A (en) |
| AU (1) | AU8141494A (en) |
| CA (1) | CA2176354A1 (en) |
| WO (1) | WO1995013340A1 (en) |
| ZA (1) | ZA948905B (en) |
Families Citing this family (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP3615878B2 (en) * | 1996-09-20 | 2005-02-02 | 三菱重工業株式会社 | Gasification combined power generation facility |
| US6080301A (en) | 1998-09-04 | 2000-06-27 | Exxonmobil Research And Engineering Company | Premium synthetic lubricant base stock having at least 95% non-cyclic isoparaffins |
| US6475960B1 (en) | 1998-09-04 | 2002-11-05 | Exxonmobil Research And Engineering Co. | Premium synthetic lubricants |
| US7056487B2 (en) * | 2003-06-06 | 2006-06-06 | Siemens Power Generation, Inc. | Gas cleaning system and method |
| JP5366147B2 (en) * | 2008-02-05 | 2013-12-11 | 一般財団法人電力中央研究所 | Fuel gas purification equipment, power generation system and fuel synthesis system |
| BRPI0919624A2 (en) * | 2008-10-22 | 2015-12-01 | Southern Res Inst | synthesis gas decontamination process. |
| CN110075823B (en) * | 2019-05-30 | 2022-04-12 | 新奥科技发展有限公司 | Preparation method, preparation device and application method of catalyst for DEC synthesis |
Family Cites Families (14)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4062926A (en) * | 1975-03-19 | 1977-12-13 | The Superior Oil Company | Sulfur dioxide removal using thermally crushed nahcolite |
| US4018868A (en) * | 1975-03-19 | 1977-04-19 | The Superior Oil Company | Thermal crushing of alkali compounds in the removal of sulfur dioxides from a flue gas |
| US4343631A (en) * | 1981-01-30 | 1982-08-10 | Westinghouse Electric Corp. | Hot gas particulate removal |
| DE3137812A1 (en) * | 1981-09-23 | 1983-03-31 | Vereinigte Elektrizitätswerke Westfalen AG, 4600 Dortmund | "METHOD FOR SEPARATING CHLORINE, FLUOR AND SULFUR FROM COMBUSTION AND SMOKE GASES" |
| US4468376A (en) * | 1982-05-03 | 1984-08-28 | Texaco Development Corporation | Disposal process for halogenated organic material |
| EP0190416A3 (en) * | 1984-11-30 | 1988-07-27 | Waagner-Biro Aktiengesellschaft | Process for separating pollutants from combustion gases |
| AT382089B (en) * | 1985-04-05 | 1987-01-12 | Waagner Biro Ag | METHOD AND DEVICE FOR THE PURIFICATION OF EXHAUST GASES POLLUTED WITH DUST AND POLLUTANT GAS |
| US4681045A (en) * | 1986-07-21 | 1987-07-21 | William F. Cosulich Associates, P.C. | Treatment of flue gas containing noxious gases |
| US4793981A (en) * | 1986-11-19 | 1988-12-27 | The Babcock & Wilcox Company | Integrated injection and bag filter house system for SOx -NOx -particulate control with reagent/catalyst regeneration |
| DE3644102A1 (en) * | 1986-12-23 | 1988-07-07 | Metallgesellschaft Ag | EXHAUST GAS PURIFICATION PROCESS |
| US4857285A (en) * | 1987-06-04 | 1989-08-15 | General Electric Environmental Services, Inc. | Method and system for removal of sulfur compounds from gases and for regenerating spent sorbents |
| US4865627A (en) * | 1987-10-30 | 1989-09-12 | Shell Oil Company | Method and apparatus for separating fine particulates from a mixture of fine particulates and gas |
| US5118480A (en) * | 1990-06-25 | 1992-06-02 | General Electric Environmental Services, Incorporated | Method for removing hcl and hf from coal derived fuel gas |
| GB9211551D0 (en) * | 1992-05-30 | 1992-07-15 | Foseco Int | Filtration of gases |
-
1993
- 1993-11-12 US US08/153,591 patent/USH1539H/en not_active Abandoned
-
1994
- 1994-11-08 KR KR1019960702546A patent/KR960705903A/en not_active Application Discontinuation
- 1994-11-08 JP JP7513593A patent/JPH09504822A/en active Pending
- 1994-11-08 EP EP95900688A patent/EP0728172A1/en not_active Withdrawn
- 1994-11-08 AU AU81414/94A patent/AU8141494A/en not_active Abandoned
- 1994-11-08 CN CN94194120A patent/CN1135233A/en active Pending
- 1994-11-08 WO PCT/EP1994/003699 patent/WO1995013340A1/en not_active Application Discontinuation
- 1994-11-08 CA CA002176354A patent/CA2176354A1/en not_active Abandoned
- 1994-11-10 ZA ZA948905A patent/ZA948905B/en unknown
Also Published As
| Publication number | Publication date |
|---|---|
| WO1995013340A1 (en) | 1995-05-18 |
| CN1135233A (en) | 1996-11-06 |
| KR960705903A (en) | 1996-11-08 |
| AU8141494A (en) | 1995-05-29 |
| EP0728172A1 (en) | 1996-08-28 |
| USH1539H (en) | 1996-06-04 |
| JPH09504822A (en) | 1997-05-13 |
| ZA948905B (en) | 1995-06-13 |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| FZDE | Discontinued |