CA1107963A - Method and apparatus for gasifying coal - Google Patents
Method and apparatus for gasifying coalInfo
- Publication number
- CA1107963A CA1107963A CA288,097A CA288097A CA1107963A CA 1107963 A CA1107963 A CA 1107963A CA 288097 A CA288097 A CA 288097A CA 1107963 A CA1107963 A CA 1107963A
- Authority
- CA
- Canada
- Prior art keywords
- gas
- crude
- tar
- dust
- decant
- 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
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K1/00—Purifying combustible gases containing carbon monoxide
- C10K1/02—Dust removal
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- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Combustion & Propulsion (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Organic Chemistry (AREA)
- Industrial Gases (AREA)
Abstract
A B S T R A C T
A method for gasifying coal under pressure for the purpose of cleaning the crude gas emerging from a reactor, whereby a mixture of dust particles and tar is recovered, from the hot crude gas, in a gas-cleaning unit following the reactor, the said mixture being removed and processed or returned, at least in part, to the reactor, characterized in that liquid tar is distributed to, and vapourized in, the hot crude gas, and in that the tempera-ture of the crude gas is lowered and the tar is condensed, the particles of dust being combined therewith.
A method for gasifying coal under pressure for the purpose of cleaning the crude gas emerging from a reactor, whereby a mixture of dust particles and tar is recovered, from the hot crude gas, in a gas-cleaning unit following the reactor, the said mixture being removed and processed or returned, at least in part, to the reactor, characterized in that liquid tar is distributed to, and vapourized in, the hot crude gas, and in that the tempera-ture of the crude gas is lowered and the tar is condensed, the particles of dust being combined therewith.
Description
:l lt~ 3 The invention relates to a method for gasifying coal under pressure, for the purpose of cleaning the crude gas emerging from a reactor, whereby a mixture of dust particles and tar is recovered, from the hot crude gas, in a gas~cleaning unit following the reactor, the said mixture being removed and processed or returned, at least in part, to the crude gas. The invention also relates to an installation for the execution of this method.
In gasifying coal under pressure, preferably bituminous coal is gasified in a reactor under pressure and at a temperature of about 1000C. The gas-cleaning unit located after the reactor not only separates tar and dust, but also removes hydrogen sulphide, and is thus a considerable ~tep towards the pollution-free generation of electricity. This generation of electricity may be carried out by means of an expansion turbine through which cleaned gas flows, usually under pressure, but is more usually carried out by producing steam in a boiler, under which the gas is burned, and feedi~g the steam to a steam-turbine, or by means of a gas-turbine which processes the combustion gas cooled in the 29 boiler and then release~ it to the atmosphere through a stack.
Although this process makes it possible to eliminate dust and fluorine emissions almost entirely, and to reduce considerably the emission of sulphur and nitric oxide, difficulties still arise in the cleaning stage.
It is known for the gas-cleaning unit to be in the form of a washing cooler to which the crude gas is fed under pressure. Thorough mixing of the washing water takes place in the washing cooler. On the one hand, this results in water being picked by the clean gas, and this gas must therefore be passed through a drip-separator in a subsequent treatment stage~
l~L~7963 On the other hand, the washing water produces a mixture of dust tar and water which must be processed. This is what causes the difficulties mentioned above.
The washing proces~, and the subsequent condensation of the steam rising from the washing water, produces heat losses which impair the overall efficiency. The necessary re-placement of the water thus lost leads to added expense, since only fully desalinized washing water can be used for the process.
Dust-removal efficiency is also poor, generally between 50 and 70~ only. This means additional dust-removal units and there-fore increased expenditure. The mixture produced must be separated into at least tar containing a large amount of dust, which is usually returned to the reactor, and water. The washed-out tar tends to foam, and this makes the process con-siderably more difficult. The dehydrated mixture is generally in the form of a cream-like mass which does not flow and is therefore also very difficult to handle.
It îs the purpose of the invention to eliminate the difficulties caused by the use of washing water by using a novel gas-cleaning unit, in order to improve the cleaning of dust in the gas-cleaning unit and to reduce the processing difficulties hitherto associated with the separated mi~ture.
According to the invention, this purpose is achieved in that liquid tar is distributed to, and vapourized in, the hot crude gas, and in that the temperature of the crude gas is reduced and the tar with which the dust particles are combined is condensed.
This method makes it possible to dispense completely with the addition of cooling water to the crude gas. As a rule, only a part of the total tar introduced is vapourized by the t~7~63 heat of the crude gas, and this increases the partial pressure of the tar in the crude gas. During the subsequent cooling, therefore, the amount of tar condensed is relatively larger than in known crude-gas cooling processes in which no tar is added.
During condensation of the tar, the particles of dust in the crude gas act as condensation nuclei and support the formation of tar and separation of dust.
The main advantages of the method are therefore, on the one hand, that no washing water is used and, on the other iO hand, that there is a considerable improvement in dust separation.
In additio~ to this, ~n the case of the new method, the crude-gas heat removed by cooling need no longer be wasted but may be utilized in the overall pxocess, as explained in detail hereinafter.
The tar is preferably introduced into the hot crude gas by injecting tar oil through nozzles. This facilitates vapourization of the tar and ensures that when the temperature of the crude gas is reduced, after the tar is introduced, the heavy and hughly viscous hydrocarbons initially separated are diluted, thus improving the ability of the tar-dust suspension to flow. This facilitates the further handling of the separated mixture.
This purpose is also served by a further example of embodiment of the method according to the invention, in which the crude gas is passed along a sloping path along which the condensed tar is caused to flow. In this way a film of tar is forned from the drops of tar initially formed and laden with dust. This film automatically moves by gravity in the direction of ~he flow of gas, the said flow of gas facilitating the flow of tar, thus rendering special transportation means unnecessary.
.1L~7~63 More particularly, with this method the amount of tar separated i~ increased, in the upper stretches of the path followed by the crude gas, by adjusting the amount of tar introduced, as compared with the amounts of mixture separated in the lower stretches of the path. In this connection an excess of tar may be introduced, which causes the film of tar described above to form more rapidly, since it may be formed at least in part from the unvapourized tar introduced.
In the method according to the invention, the mixture ~10 separated from ~he crude gas ispreferably decanted, thus pro-ducing a fraction of the mixture containing more dust which is return~d to the reactor, while another fraction is processed or conditioned. This processing may consist of separating the tar contained in the fraction of the initial mixtures containing less dust, and returning it to the flow of hot crude gas. In ~ -this way, most of the dust is separated and the useful tar fraction is circulated so that the process can sustain itself.
With this process, it is desirable to divide the portion low in dust into a light and a heavY fraction, the light ~20 fraction being injected into the flow of crude gas, while the heavy fraction is returned to the reactor. This ensures that the light fraction contains almost no dust, which means that the difficulties caused by the dust are eliminated, and that high dust-removal efficiency is achieved.
The portion low in dust may be broken down into fractions by expansion vapourization, the heat arising during condensation of the tar vapours being used to preheat the boiler-feedwater used to generate steam. It is possible, with this method, to increase the efficiency of the unit still further, to provide an increase in overall efficiency of 2%.
~Di7963 In addition to this, it ha~ been found that there is a substantial improvement in dust removal, presumably because of the better wetting of the tar in relation to the dust, as compared with the washing water hitherto used. As a result of this, the amount of tar in circulation is about one tenth of the amount of circulation when water is used as the washing agent. As a result of this, the unit for recover-ing tar from the mixture of tar and dust is about one tenth the si~e of units in which the washing water must be separated from the said mixture.
Replacement of the washing water by tar means that there is no need to feed washing fluid to the process from the outside. This also eliminates the difficulties hitherto ~- associated with clarifying the wash~ng water. These difficult- ~ -ies are major, since the washing water is highly contaminated with high-boiling-point hydrocarhons. In additi~n to this, the subsequent installation for removing the fineplrticle~
of dust may be considerably simplified or totally eliminated.
In order to make the invention more easily understood, a unit for the execution of the foregoing method is described hereinafter in greater detail. Since there is no contamination with baked-on dust and ~ar, this unit may be built up with basically conventional components. The drawing attached hereto is a diagrammatic representation of a unit of this kind.
The crude gas emerging ~rom a reactor, not shown, passes through line 1 into a crude-gas cooler marked 2 as a whole. This cooler comprises an inlet chamber 3 at the top and an outlet chamber 4 at the bottom. Between these chambers lies a group of pipes 5 constituting the heating surface, the pipes in this group having an inside diameter of about 50 mm, - 5 ~
1~7963 not more than 90 mm. The crude gas flows through the pipes which are cooled externally with a cooling fluid. This fluid is supplied from a steam drum 6 through a line 7 and flows, through line 8, into crude-gas cooler 2, leaving the cooler through line 9 and returning to steam drum 6. The steam drum, in turn, is connected to boiler feedwater line 10, from which an amount of fluid, corresponding substantially to the amount of steam is replaced, the said steam being removed through line 11 and being passed, for example, to a steam-turbine process, not shown, for the purpose of generating electrical power.
In the design illustrated, the cooling water circulates naturally and returns, at least some of it in the form of steam, through the said line 9, to steam drum 6.
With this arrangement, the cooled and cleaned crude gas emerges at 12 as fuel gas, still at a temperature of between 260 and 300C. This ~uel gas is passed on for further processing, not shown in the drawing.
The mixture removed through line 13 consists of condensed tar and dust par~icles. The said mixture passes to a decanting marked 15 as a whole where it is divided, the example of embodiment illustrated, into one fraction high in dust and one fraction low in dust. By means of a pump 14, the tar low in dust i5 returned, through a line ~, to the top of crude-gas cooler 2. The tar high in dust is returned, through a line 17, to the reactor, not shown.
As shown, the crude gas entering cooler 2 is cooled, at the same time liquid tar is injected through nozzles into the crude gas. This causes the tar to condense and combines the dust contained in the crude gas into the mixture. Since tar is present in excess, the mixture remains fluid, so that ~379~3 cooler 2 does not become contaminated and the unit requires almost no maintenance. According to variant of this example of embodim~t, an expansion-distilling unit may be connected to decanting system 15, so that the mixture fraction high in dust can also be processed.
In gasifying coal under pressure, preferably bituminous coal is gasified in a reactor under pressure and at a temperature of about 1000C. The gas-cleaning unit located after the reactor not only separates tar and dust, but also removes hydrogen sulphide, and is thus a considerable ~tep towards the pollution-free generation of electricity. This generation of electricity may be carried out by means of an expansion turbine through which cleaned gas flows, usually under pressure, but is more usually carried out by producing steam in a boiler, under which the gas is burned, and feedi~g the steam to a steam-turbine, or by means of a gas-turbine which processes the combustion gas cooled in the 29 boiler and then release~ it to the atmosphere through a stack.
Although this process makes it possible to eliminate dust and fluorine emissions almost entirely, and to reduce considerably the emission of sulphur and nitric oxide, difficulties still arise in the cleaning stage.
It is known for the gas-cleaning unit to be in the form of a washing cooler to which the crude gas is fed under pressure. Thorough mixing of the washing water takes place in the washing cooler. On the one hand, this results in water being picked by the clean gas, and this gas must therefore be passed through a drip-separator in a subsequent treatment stage~
l~L~7963 On the other hand, the washing water produces a mixture of dust tar and water which must be processed. This is what causes the difficulties mentioned above.
The washing proces~, and the subsequent condensation of the steam rising from the washing water, produces heat losses which impair the overall efficiency. The necessary re-placement of the water thus lost leads to added expense, since only fully desalinized washing water can be used for the process.
Dust-removal efficiency is also poor, generally between 50 and 70~ only. This means additional dust-removal units and there-fore increased expenditure. The mixture produced must be separated into at least tar containing a large amount of dust, which is usually returned to the reactor, and water. The washed-out tar tends to foam, and this makes the process con-siderably more difficult. The dehydrated mixture is generally in the form of a cream-like mass which does not flow and is therefore also very difficult to handle.
It îs the purpose of the invention to eliminate the difficulties caused by the use of washing water by using a novel gas-cleaning unit, in order to improve the cleaning of dust in the gas-cleaning unit and to reduce the processing difficulties hitherto associated with the separated mi~ture.
According to the invention, this purpose is achieved in that liquid tar is distributed to, and vapourized in, the hot crude gas, and in that the temperature of the crude gas is reduced and the tar with which the dust particles are combined is condensed.
This method makes it possible to dispense completely with the addition of cooling water to the crude gas. As a rule, only a part of the total tar introduced is vapourized by the t~7~63 heat of the crude gas, and this increases the partial pressure of the tar in the crude gas. During the subsequent cooling, therefore, the amount of tar condensed is relatively larger than in known crude-gas cooling processes in which no tar is added.
During condensation of the tar, the particles of dust in the crude gas act as condensation nuclei and support the formation of tar and separation of dust.
The main advantages of the method are therefore, on the one hand, that no washing water is used and, on the other iO hand, that there is a considerable improvement in dust separation.
In additio~ to this, ~n the case of the new method, the crude-gas heat removed by cooling need no longer be wasted but may be utilized in the overall pxocess, as explained in detail hereinafter.
The tar is preferably introduced into the hot crude gas by injecting tar oil through nozzles. This facilitates vapourization of the tar and ensures that when the temperature of the crude gas is reduced, after the tar is introduced, the heavy and hughly viscous hydrocarbons initially separated are diluted, thus improving the ability of the tar-dust suspension to flow. This facilitates the further handling of the separated mixture.
This purpose is also served by a further example of embodiment of the method according to the invention, in which the crude gas is passed along a sloping path along which the condensed tar is caused to flow. In this way a film of tar is forned from the drops of tar initially formed and laden with dust. This film automatically moves by gravity in the direction of ~he flow of gas, the said flow of gas facilitating the flow of tar, thus rendering special transportation means unnecessary.
.1L~7~63 More particularly, with this method the amount of tar separated i~ increased, in the upper stretches of the path followed by the crude gas, by adjusting the amount of tar introduced, as compared with the amounts of mixture separated in the lower stretches of the path. In this connection an excess of tar may be introduced, which causes the film of tar described above to form more rapidly, since it may be formed at least in part from the unvapourized tar introduced.
In the method according to the invention, the mixture ~10 separated from ~he crude gas ispreferably decanted, thus pro-ducing a fraction of the mixture containing more dust which is return~d to the reactor, while another fraction is processed or conditioned. This processing may consist of separating the tar contained in the fraction of the initial mixtures containing less dust, and returning it to the flow of hot crude gas. In ~ -this way, most of the dust is separated and the useful tar fraction is circulated so that the process can sustain itself.
With this process, it is desirable to divide the portion low in dust into a light and a heavY fraction, the light ~20 fraction being injected into the flow of crude gas, while the heavy fraction is returned to the reactor. This ensures that the light fraction contains almost no dust, which means that the difficulties caused by the dust are eliminated, and that high dust-removal efficiency is achieved.
The portion low in dust may be broken down into fractions by expansion vapourization, the heat arising during condensation of the tar vapours being used to preheat the boiler-feedwater used to generate steam. It is possible, with this method, to increase the efficiency of the unit still further, to provide an increase in overall efficiency of 2%.
~Di7963 In addition to this, it ha~ been found that there is a substantial improvement in dust removal, presumably because of the better wetting of the tar in relation to the dust, as compared with the washing water hitherto used. As a result of this, the amount of tar in circulation is about one tenth of the amount of circulation when water is used as the washing agent. As a result of this, the unit for recover-ing tar from the mixture of tar and dust is about one tenth the si~e of units in which the washing water must be separated from the said mixture.
Replacement of the washing water by tar means that there is no need to feed washing fluid to the process from the outside. This also eliminates the difficulties hitherto ~- associated with clarifying the wash~ng water. These difficult- ~ -ies are major, since the washing water is highly contaminated with high-boiling-point hydrocarhons. In additi~n to this, the subsequent installation for removing the fineplrticle~
of dust may be considerably simplified or totally eliminated.
In order to make the invention more easily understood, a unit for the execution of the foregoing method is described hereinafter in greater detail. Since there is no contamination with baked-on dust and ~ar, this unit may be built up with basically conventional components. The drawing attached hereto is a diagrammatic representation of a unit of this kind.
The crude gas emerging ~rom a reactor, not shown, passes through line 1 into a crude-gas cooler marked 2 as a whole. This cooler comprises an inlet chamber 3 at the top and an outlet chamber 4 at the bottom. Between these chambers lies a group of pipes 5 constituting the heating surface, the pipes in this group having an inside diameter of about 50 mm, - 5 ~
1~7963 not more than 90 mm. The crude gas flows through the pipes which are cooled externally with a cooling fluid. This fluid is supplied from a steam drum 6 through a line 7 and flows, through line 8, into crude-gas cooler 2, leaving the cooler through line 9 and returning to steam drum 6. The steam drum, in turn, is connected to boiler feedwater line 10, from which an amount of fluid, corresponding substantially to the amount of steam is replaced, the said steam being removed through line 11 and being passed, for example, to a steam-turbine process, not shown, for the purpose of generating electrical power.
In the design illustrated, the cooling water circulates naturally and returns, at least some of it in the form of steam, through the said line 9, to steam drum 6.
With this arrangement, the cooled and cleaned crude gas emerges at 12 as fuel gas, still at a temperature of between 260 and 300C. This ~uel gas is passed on for further processing, not shown in the drawing.
The mixture removed through line 13 consists of condensed tar and dust par~icles. The said mixture passes to a decanting marked 15 as a whole where it is divided, the example of embodiment illustrated, into one fraction high in dust and one fraction low in dust. By means of a pump 14, the tar low in dust i5 returned, through a line ~, to the top of crude-gas cooler 2. The tar high in dust is returned, through a line 17, to the reactor, not shown.
As shown, the crude gas entering cooler 2 is cooled, at the same time liquid tar is injected through nozzles into the crude gas. This causes the tar to condense and combines the dust contained in the crude gas into the mixture. Since tar is present in excess, the mixture remains fluid, so that ~379~3 cooler 2 does not become contaminated and the unit requires almost no maintenance. According to variant of this example of embodim~t, an expansion-distilling unit may be connected to decanting system 15, so that the mixture fraction high in dust can also be processed.
Claims (12)
1. A method for gasifying coal under pressure for the purpose of cleaning the crude gas emerging from a reactor, whereby a mixture of dust particles and tar is recovered, from the hot crude gas, in a gas-cleaning unit following the reactor, the said mixture being removed and processed or returned, at least in part, to the reactor, characterized in that liquid tar is distributed to, and vapourized in, the hot crude gas, and in that the temperature of the crude gas is lowered and the tar is condensed, the particles of dust being combined therewith.
2. A method according to claim 1, characterized in that tar is introduced into the hot crude gas by injecting tar oil through nozzles.
3. A method according to Claim 1, characterized in that the crude gas is returned along a sloping path, along which the condensed tar is caused to flow.
4. A method according to claim 1, 2 or 3, characterized in that the amount of separated tar is increased in comparison with the amounts of the mixture separated in the lower sections of the path along which the crude gas flows in the higher sections of the said path, by adjusting the amount of tar introduced.
5. A method according to claim 1, characterized in that the mixture is decanted, a portion of the mixture high in dust being returned, while at least a part of the tar contained in the remaining portion of the mixture, which is low in dust, is introduced into the flow of hot gas.
6. A method according to Claim 1, characterized in that the portion low in dust is divided into a light and a heavy fraction, the light fraction being sprayed into the flow of crude-gas, while the heavy fraction is returned to the reactor.
7. A method according to Claim 5 or 6 characterized in that the portion low in dust is broken down into fractions by expansion vapourization, the heat produced by condensation of the tar vapours being used for preheating the boiler-feedwater used for generating steam.
8. A gas cleaner for use in cleaning the crude-gas output of a coal gasification reactor comprising:
(a) a heat exchanger having a crude-gas chamber and a cooling fluid chamber arranged in the heat exchange relation-ship, said crude-gas chamber having an input end and an output end, (b) a first input passage opening into said input end of said crude-gas chamber for admitting crude-gase, (c) a second input passage opening into said input end of said crude-gas chamber for admitting tar, (d) a first outlet passage opening from said output end of said crude-gas chamber for discharging clean gas, (e)a second outlet passage opening from said output end of said crude-gas chamber for discharging tar and dust, (f) decant means for separating high dust content tar for low dust content tar, said decant means having a decant inlet communicating with said second outlet passage to receive tar and dust from said crude-gas chamber, (g) first decant outlet means opening from said decant means and arranged to permit discharge of high dust content tar from said decant means, (h) second decant outlet means opening from said decant means arranged to communicate with said first input passage of said crude-gas chamber for directing low dust content tar to said input end of said crude-gas chamber, and (i) means for circulating cooling fluid through said cooling fluid chamber.
(a) a heat exchanger having a crude-gas chamber and a cooling fluid chamber arranged in the heat exchange relation-ship, said crude-gas chamber having an input end and an output end, (b) a first input passage opening into said input end of said crude-gas chamber for admitting crude-gase, (c) a second input passage opening into said input end of said crude-gas chamber for admitting tar, (d) a first outlet passage opening from said output end of said crude-gas chamber for discharging clean gas, (e)a second outlet passage opening from said output end of said crude-gas chamber for discharging tar and dust, (f) decant means for separating high dust content tar for low dust content tar, said decant means having a decant inlet communicating with said second outlet passage to receive tar and dust from said crude-gas chamber, (g) first decant outlet means opening from said decant means and arranged to permit discharge of high dust content tar from said decant means, (h) second decant outlet means opening from said decant means arranged to communicate with said first input passage of said crude-gas chamber for directing low dust content tar to said input end of said crude-gas chamber, and (i) means for circulating cooling fluid through said cooling fluid chamber.
9. A gas cleaner as claimed in Claim 8 further comprising an expansion-distilling unit communicating with said first decant outlet means for distilling said high dust content tar.
10. A gas cleaner as claimed in Claim 8 wherein said crude-gas chamber of said heat exchanger comprises a plurality of vertically oriented heat exchanger tubes through which said crude-gas is directed when passing from said input end to said output end of said crude-gas chamber, said first and second input passages of said crude-gas chamber being located above said heat exchanger tubes and said first and second outlet passages being located below said heat exchanger tubes.
11. A gas cleaner as claimed in Claim 8 wherein said means for circulating cooling fluid through said cooling fluid chamber comprises cooling fluid inlet and outlet pas-sages communicating with said cooling fluid chamber , a steam-drum arranged to communicate with a feedwater line of a boiler, first conduit means arranged to convey cooling water from said steam-drum to said inlet of said cooling fluid chamber and second conduit means arranged to convey the output from said cooling fluid chamber to said steam-drum.
12. A gas cleaner as claimed in Claim 9 further comprising pump means for pumping the low dust content tar from said decant outlet to said second input passage of said crude-gas chamber.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| DE19762646568 DE2646568B2 (en) | 1976-10-15 | 1976-10-15 | Process for purifying the raw gas emerging from a reactor for pressurized coal gasification |
| DEP2646568.9 | 1976-10-15 |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CA1107963A true CA1107963A (en) | 1981-09-01 |
Family
ID=5990524
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA288,097A Expired CA1107963A (en) | 1976-10-15 | 1977-10-04 | Method and apparatus for gasifying coal |
Country Status (2)
| Country | Link |
|---|---|
| CA (1) | CA1107963A (en) |
| DE (1) | DE2646568B2 (en) |
Families Citing this family (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE3421393A1 (en) * | 1984-06-08 | 1985-12-12 | Krupp Koppers GmbH, 4300 Essen | METHOD FOR PROCESSING SMOKE GAS FROM WASTE PYROLYSIS |
| DE102004030370B3 (en) * | 2004-06-23 | 2005-12-15 | Kirchner, Hans Walter, Dipl.-Ing. | Cooling and cleaning system for biogas plant has two heat exchangers connected in series to cool hot gas and condense out tar before gas goes to cooled metallic fabric filter |
-
1976
- 1976-10-15 DE DE19762646568 patent/DE2646568B2/en not_active Withdrawn
-
1977
- 1977-10-04 CA CA288,097A patent/CA1107963A/en not_active Expired
Also Published As
| Publication number | Publication date |
|---|---|
| DE2646568B2 (en) | 1981-01-29 |
| DE2646568A1 (en) | 1978-04-20 |
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| Date | Code | Title | Description |
|---|---|---|---|
| MKEX | Expiry |