CA1096641A - Power generator - Google Patents
Power generatorInfo
- Publication number
- CA1096641A CA1096641A CA287,635A CA287635A CA1096641A CA 1096641 A CA1096641 A CA 1096641A CA 287635 A CA287635 A CA 287635A CA 1096641 A CA1096641 A CA 1096641A
- Authority
- CA
- Canada
- Prior art keywords
- gas
- boiler
- steam
- flue
- dust
- 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
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F02—COMBUSTION ENGINES; HOT-GAS OR COMBUSTION-PRODUCT ENGINE PLANTS
- F02C—GAS-TURBINE PLANTS; AIR INTAKES FOR JET-PROPULSION PLANTS; CONTROLLING FUEL SUPPLY IN AIR-BREATHING JET-PROPULSION PLANTS
- F02C3/00—Gas-turbine plants characterised by the use of combustion products as the working fluid
- F02C3/20—Gas-turbine plants characterised by the use of combustion products as the working fluid using a special fuel, oxidant, or dilution fluid to generate the combustion products
- F02C3/26—Gas-turbine plants characterised by the use of combustion products as the working fluid using a special fuel, oxidant, or dilution fluid to generate the combustion products the fuel or oxidant being solid or pulverulent, e.g. in slurry or suspension
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F01—MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
- F01K—STEAM ENGINE PLANTS; STEAM ACCUMULATORS; ENGINE PLANTS NOT OTHERWISE PROVIDED FOR; ENGINES USING SPECIAL WORKING FLUIDS OR CYCLES
- F01K23/00—Plants characterised by more than one engine delivering power external to the plant, the engines being driven by different fluids
- F01K23/02—Plants characterised by more than one engine delivering power external to the plant, the engines being driven by different fluids the engine cycles being thermally coupled
- F01K23/06—Plants characterised by more than one engine delivering power external to the plant, the engines being driven by different fluids the engine cycles being thermally coupled combustion heat from one cycle heating the fluid in another cycle
- F01K23/067—Plants characterised by more than one engine delivering power external to the plant, the engines being driven by different fluids the engine cycles being thermally coupled combustion heat from one cycle heating the fluid in another cycle the combustion heat coming from a gasification or pyrolysis process, e.g. coal gasification
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E20/00—Combustion technologies with mitigation potential
- Y02E20/16—Combined cycle power plant [CCPP], or combined cycle gas turbine [CCGT]
- Y02E20/18—Integrated gasification combined cycle [IGCC], e.g. combined with carbon capture and storage [CCS]
Landscapes
- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Combustion & Propulsion (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Fluidized-Bed Combustion And Resonant Combustion (AREA)
- Engine Equipment That Uses Special Cycles (AREA)
Abstract
A B S T R A C T
An installation for obtaining energy from solid fossil fuels, especially those high in inerts, more particular-ly bituminous coal, the said installation consisting of at least one block in which the solid fuels are converted into gas and containing a gas turbine and a steam turbine for extracting energy from the gas, the dust and sulphur being removed from the gases, in the block, before the gas turbine, characterized in that a melting-chamber boiler, to which the ground fuel is fed, is equipped with pressure firing, the flue-gases therefrom being adapted to be fed to the desulphurizing unit and to the dust-removal unit before being used in the gas turbine.
An installation for obtaining energy from solid fossil fuels, especially those high in inerts, more particular-ly bituminous coal, the said installation consisting of at least one block in which the solid fuels are converted into gas and containing a gas turbine and a steam turbine for extracting energy from the gas, the dust and sulphur being removed from the gases, in the block, before the gas turbine, characterized in that a melting-chamber boiler, to which the ground fuel is fed, is equipped with pressure firing, the flue-gases therefrom being adapted to be fed to the desulphurizing unit and to the dust-removal unit before being used in the gas turbine.
Description
6~
The invention relates to an installation for obtaining energy from solid fossil fuels, especially those high in inerts, more particularly bituminous coal, the said installation con-sisting o~ at least one ~lock in which the solid fuels are converted into gas and containing a gas turbine and a steam turbine for extracting electrical energy from the gases, the dust and sulphur being removed from the gases, in the block, before the gas turbine.
The advantage of a block installation of this kind is that if the gas-turbine process is correctly combined with the ste~m-turbine process, greater thermal efficiency is obtained than in an installation in which the processes are all carried out separately. The dust-removing operation cleans the gases to such an extent that they can be fed to the gas turbine in spite of the fact that ~he coal used is high in inerts. De-sulphurization is carried out under high pressure and therefore has advantages over the known pressureless flue-gas desulphuri-zation, especially since the desulphurizing units are smaller and since, in adsorptive desulphurizing, the adsorption losses are reduced by the high pressure. This means ~hat installations of this kind also cause particularly little pollution.
So-called pressure-gasification in a solid bed is known. In units of this kind, coal, mostly high in iner~s, is gasified with some of the available combustion air, and with steam, under high pressuxe, i.e. it is partly burned.
; The gasification pressure in known units of this kind is about 20 bars. Gasification is carried out in a reactor produciny lean gas at a temperature of between 500 and 600C which is cooled and is then fed to dust-removal and desulphurizing units.
The clean lean gas is burned, as fuel gas, in a boiler under pressure. ~'he flue-gases are used to operate the gas turbine, ~ ' ~`~
- - . :. ~ . : -.
while ~le steam produced in the boiler drives the steam turbine.
However, coal-gasiEication under pressure produces a series of losses. Some of these are based upon the large proportion of unburned mater:ial in the ash removed from the reactor, hitherlto always amounting to more than 10%. Other losses are the result of so-called casing steam, i.e evaporation of the cooling water ed to ~le pressure-gasifier. Other losses are caused by the evaporation of water during so-called quenching. Finally, the losses are still further increased by the fact that much of the water used in washing the gases is not separated but remains in the fuel gas in the form of a spray which 1therefore has to evaporated in the firing of the boiler.
Other disadvantages of coal-gasification under pressure arise from operating difficulties. For instance, during tha cooling oiE the lean gas, tars condense and are deposited upon the par~icles of dust in the gas, producing a mixture of dust and tar. This easily leads to baked-on deposits and blockages in the different circuits in which it occurs, and these must be removed. If substantial heat losses are to be prevented, the dust-tar mixture must be separated from the washing medium in a tar-separator or some other suitable unit, the said mixture being returned to the gas-producer. This produces special problems, since the dus~y tar is difiEicult to pump and again produces operational problems.
Hitherto-known units for gasifying coal under pressure are also comparatively difficult to cQntrol. For instance, lthere are fluctuations in the gas-outlet temperature, in the calorific value, and in the dust and tar contents, these ' ; , ~ .: ~, - , fluctuations bein~ mainly attributable to the intermittent ~eeding of coal to the gas-producer. Furthermore it is impossible to achieve a rapid load increase if an adequetelY
high calorific value of the fuel gases is required at the same time. These problen-s make it impossible to obtain a sensitive performance control.
Finally, it should be pointed out that, because of their low calorific value, the fuel gases cause problems when they are burned in the boiler, and there are many occasions when comhustion must be supported by additional fuels, usually fuel oil.
There has also been proposed an installation of the kind described at the beginning hereof having a block in which the fuel is burned and desulphurized in a fluidized layer.
To this end, the ground fuel and the desulphurizer are fed to the fluidized bed, the fuel being burned, under pressure, in the suspension. ~Ieat is transferred to the steam process within the fluidized layer, the combustion temperature being thus restricted to about 900C. The flue-gas emerging from the vortex chamber, and containing a considerable amount of solid material (ash, unburned substances, and partly charged desulphurzier) must then be passed to a gas turbine. There has hitherto been no known way of producing a mechanically cle~ gas from these flue-gases.
If a vortex chamber is used to burn the ground fuel, this produces a series of disadvantages, since a considerable amount of unburned substances must also be expected in the ash in the vortex chambsr. Unfortunately, the unburned substances are discharged from the vortex chamber with the 10w of flue-gas and thus inevitably reach the subsequent dust-removal unit. It is extremely difficult to ~eparate the total ash from the fuel and the partly-charged desulphurizer ;, : , . . - : - . .,., ., . -. - :
~Q~
from the flow of flue gas. It is also difEicult to separate the partly-charged desulphurizer from th~ ash for preparing the desulphurizer. In addition to this there are wear problems in connection witn the heating surfaces which have to be arranged within the fluidized layer. This wear is due mainly to the inevitable erosion in the fluidized layer. ~ccurate control of the fluidized-bed temperatures also presents con-: siderable difficulties. If, for instance, the fluidized-bed temperature rises too high, the ash softens and the fluidized bed bakes onto the heating surfaces. On the other hand, if the fluidized-bed temperature is too low, there is a drop in the degree of combustion and ~hus a corresponding increase in fuel losses. Furthermore, low-temperature carbonization sets in, and this causes the tar to condense and the fluidized bed to bake onto the heating surfaces.
It is the purpose of the invention to reduce the losses and operating problems in installations of the kind described at the beginning hereof, and to design an installation that can be used as a peak-load power station.
According to the invention, this purpose i3 achieved in that a melting-chamber boiler, to which the ground fuel is fed, is pressure fired, and in that the flue-gases pass to - desulphurizing and dust-removal units before they reach the gas turbine.
Since combustion takes place in one part of the installation (partial combustion and post-combustion), the two processes can be jointly controlled as required for a peak-load power station~ In other words, the output can be increased and reduced relatively quickly, and may thus be adapted to the power taken off, without heat loss and without supporting the combustion process with oil or other additional _ ~ _ -.~, .
.:
- : :-fuels. Since the fuel is burned in a melting-chan~er boiler (kettle, vessel), no tar occurs, no equipment is re~uired to deal with it, and the corresponding difficulties are eliminated.
Ihe pressure in ~e flue-gas side of the melting-chamber boiler may be 10 bars, for example, and this corresponds approximately ~o t~e gas-turbine pressure.
The main advantage~s of the new installation is that there is a negligeable amount of unburned substance in the melting-chamher slag, so little that it cannot be measured.
The thermal efficiency is considerably higher, since there are no losses by evaporation outside the steam circuit, such as have hitherto been unavoidable in the gasification of a fuel. The low water content in the flue-gas also assists in improving the thermal efficiency. This is the reason for the low dew-point and the relatively small waste-gas loss.
Another advangtage is that most of the ash is removed from the melting-chamber boiler in the form of granules and does not reach the turbine gas. The granular material thus removed may be further processed and used for other purposes.
Accordiny to another characteristic of the invention the flue-gases may be removed from bahind the radiating portion of the boiler. Moreover, heat-exchanger surfaces are provided, outside the boiler, for the flue-gases thus removed, and may be used to adjust the flue-gas temperature before the gas turbine. These heat-exchanger surfaces are used to produce the steam which is fed to the steam-power process. It is also desirable to burn the fuel directly under pressure in a cyclone since, as compared with the gasification technique, this saves a number of additional units (gas producers) and requires, for the combustion process, a unit substantially smaller tham that used in the fluidized-bed technique. It is also possible to locate ~e heat--exchanger surfaces, used to adjust the flue-gas temperature before the gas turbine, in the flue-gas desulphurizer. The said heat-exchanger surfaces may also follow the desulphurizer~
The actual desulphuriziny may be carried out with metal car~onates or oxides, using a solid bed in which the de-sulphurizer is in the form of pellets or briquettes. On the other hand, a fluidized becl may be used, or the desulphuriæer may be injected into the desulphurizing chamber in the form of a dry dust.
On the flue-gas side, a dry flue-gas dust-removal unit, operating at the existin~ high pressure, may be inserted after the said heat-exchanger surfaces~ l~his dust-removal unit may operate with ceramic candle filters or with separator nozzles, a hot cyclone bPing used, if necessary, as a pre-separator before the actual dust-removal process.
~ s regards subsequent equipment, the invention has the advantage that the heat-exchanger surfaces after the radiating portion of the boiler are substantially smaller as compared wi~h those in the proposed fluidized bed, and this reduces erosion. Furthermore, the desulphurizer is more easily separated from the ash, since there is considerably less ash than in the fluidized-bed process. This is also quite an advantage.
The details, further characteristics, and other - advantages of the invention may ~e gathered from the following descriptions of three examples of embodiment o~ the installation according to the invention, as illustrated in the drawing attached hereto, wherein :
Fig. 1 is a first example of embodiment of the installation according to the invention, in which the flue-gases are desulphurized in a fluidized bed;
-- , .
Fig. 2 is an e~ample oE en~odiment using a modified (injection) desulphuriæing unit;
Eig. 3 is an example of embodiment of the installa-tion accordiny to the invention using a solid-bed desulphuri-zing unit.
In the figures, similar parts of the installation bear the same reference numerals.
Coal containing inerts is fed rom a bunker 1 to a grindin~ unit 2 which passes thP grouncl fuel, througll a gate 3, to a line 4 running to the cyclone-firing unit of a melting-chamber boiler (kettle, vessel) marked 5 as a whole.
Id~ntification of the media in the lines corresponds to German Industrial Standard 2481.
'rhe flue-gases are removed at 7 and pass, in ~he installation according to Fiy. l to a fluidized-bed desulphuri zer 8. The desulphurizing agent used may be limestone, for example, which is fed, through a gate unit 9, to the desul-phurizing unit at lO and ll. The desulphurizing flue-gases leave the fluidized bed at 12 and pass to a cyclone which removas any coarse solids. These solids ara removed at 14 and are passed to a grading unit 15 consisting of several screens, fore~mpls. The overflow from the screens is passed on, through a line 16, for further processiny or use. l`he material passing through the screens is removed at 17 and passes, in the example of embodiment illustrated, to a gate 18 to which fine dust is fed through a line 20. The fine-dust separator ~a separator nozzle or filter) is shown at 21, and the flue gases from which the coarse solids have been removed are fed ther.eto.
The flue-gases leave fine separa-tor 21 at a tempera-ture of bet~leen 800 and 900C, fsr example, and pass, through . :
a line 22, to a gas turbine 23 which is followed by a waste-heat boiler 24. The flue-gases are th~n released to the atmosphere at 25.
Provision is made, in the example of embodiment illustrated, for the separated fine dust to be returned, through gate unit 18, pneumatically ~rough a line 26, to line 4, so that this part of the dust is returned to melting-chamber boiler 5.
Dust and ash is removed in the form of a liquid from boiler ~, and this passes to a hydraulic ash-removal unit and a crusher for granular material, this portion of the ins-talla-tion being marked 27. The granular material from the melting-chamber ash is separated from the transpor~ing water, and is removed, at a gate 28.
Boiler-feed water, which has been fed at 30 to waste-heat boiler 24, flows through a line 32 having a branch 34 running the radiating portion of melting-chamber boiler 5.
Steam leaves the boiIer at 35 and, as shown in the example ~ -of embodiment, it is passed through a heat-exchanger 36 arranged in ~idized-bed desulphurizer 8. This st~am then passes ~hrough a line 37 to a steam-turbine unit 38 with in~ermediate superheating 38a, followed by a condenser 39.
As indicated, the fossil fuels, in the form of coal, are fed directly to the ~ombination block described. This is also the case in the installations shown in Figs. 2 and 3.
The example of embodiment in Fig. 2 difers from that in Fig. 1 mainly in the type of desulphurizer to which the flue-ga~ses pass from line 7. The desulphurizing device i~ Fig. 2 is marked 40. It uses a dry desulphurizer in the form of a dust which is injected into desulphurizing vessel 41, at several locations, through nozzles marked 42-44. Again, -- 8 ~
.~
:
the desulphurizer is passed, with the aid of air from air-supply line ~7, shown in dotted lines, through a gate unit .~. 45, to the ~bove-mentioned nozzles.
The sulphur associated with the desulphurizer leaves vessel 41, in the form of a ~iolid, ~lrouyh a line 48 and is therefore passed to a gradiny unit 15 which has an overflow at lS. Part of the desulphurizer is returned to the gate through a line 49, and part is removed at 16a for processing or further . use. The amount removed is xeplaced at 16b by the addition of fresh desulphuxizer.
In the example of embodiment according to Fig. 3, solid-bed desulphuring is carried in a reaction vessel S0. In this case, the desulphurizer may be in the form of pellets or briquettes and may be fed continuously or intermittently through a gate 51. If any desulphurizer, and the sulphur associated therewith, is removed from vessel 50, this product returns at 51 to the screen overflow of grading unit 15, and so to line 16, fxom which the processed desulphurizer can be returned to the pxocess at 53.
.
_ g _ .
: "
.. : . - .
The invention relates to an installation for obtaining energy from solid fossil fuels, especially those high in inerts, more particularly bituminous coal, the said installation con-sisting o~ at least one ~lock in which the solid fuels are converted into gas and containing a gas turbine and a steam turbine for extracting electrical energy from the gases, the dust and sulphur being removed from the gases, in the block, before the gas turbine.
The advantage of a block installation of this kind is that if the gas-turbine process is correctly combined with the ste~m-turbine process, greater thermal efficiency is obtained than in an installation in which the processes are all carried out separately. The dust-removing operation cleans the gases to such an extent that they can be fed to the gas turbine in spite of the fact that ~he coal used is high in inerts. De-sulphurization is carried out under high pressure and therefore has advantages over the known pressureless flue-gas desulphuri-zation, especially since the desulphurizing units are smaller and since, in adsorptive desulphurizing, the adsorption losses are reduced by the high pressure. This means ~hat installations of this kind also cause particularly little pollution.
So-called pressure-gasification in a solid bed is known. In units of this kind, coal, mostly high in iner~s, is gasified with some of the available combustion air, and with steam, under high pressuxe, i.e. it is partly burned.
; The gasification pressure in known units of this kind is about 20 bars. Gasification is carried out in a reactor produciny lean gas at a temperature of between 500 and 600C which is cooled and is then fed to dust-removal and desulphurizing units.
The clean lean gas is burned, as fuel gas, in a boiler under pressure. ~'he flue-gases are used to operate the gas turbine, ~ ' ~`~
- - . :. ~ . : -.
while ~le steam produced in the boiler drives the steam turbine.
However, coal-gasiEication under pressure produces a series of losses. Some of these are based upon the large proportion of unburned mater:ial in the ash removed from the reactor, hitherlto always amounting to more than 10%. Other losses are the result of so-called casing steam, i.e evaporation of the cooling water ed to ~le pressure-gasifier. Other losses are caused by the evaporation of water during so-called quenching. Finally, the losses are still further increased by the fact that much of the water used in washing the gases is not separated but remains in the fuel gas in the form of a spray which 1therefore has to evaporated in the firing of the boiler.
Other disadvantages of coal-gasification under pressure arise from operating difficulties. For instance, during tha cooling oiE the lean gas, tars condense and are deposited upon the par~icles of dust in the gas, producing a mixture of dust and tar. This easily leads to baked-on deposits and blockages in the different circuits in which it occurs, and these must be removed. If substantial heat losses are to be prevented, the dust-tar mixture must be separated from the washing medium in a tar-separator or some other suitable unit, the said mixture being returned to the gas-producer. This produces special problems, since the dus~y tar is difiEicult to pump and again produces operational problems.
Hitherto-known units for gasifying coal under pressure are also comparatively difficult to cQntrol. For instance, lthere are fluctuations in the gas-outlet temperature, in the calorific value, and in the dust and tar contents, these ' ; , ~ .: ~, - , fluctuations bein~ mainly attributable to the intermittent ~eeding of coal to the gas-producer. Furthermore it is impossible to achieve a rapid load increase if an adequetelY
high calorific value of the fuel gases is required at the same time. These problen-s make it impossible to obtain a sensitive performance control.
Finally, it should be pointed out that, because of their low calorific value, the fuel gases cause problems when they are burned in the boiler, and there are many occasions when comhustion must be supported by additional fuels, usually fuel oil.
There has also been proposed an installation of the kind described at the beginning hereof having a block in which the fuel is burned and desulphurized in a fluidized layer.
To this end, the ground fuel and the desulphurizer are fed to the fluidized bed, the fuel being burned, under pressure, in the suspension. ~Ieat is transferred to the steam process within the fluidized layer, the combustion temperature being thus restricted to about 900C. The flue-gas emerging from the vortex chamber, and containing a considerable amount of solid material (ash, unburned substances, and partly charged desulphurzier) must then be passed to a gas turbine. There has hitherto been no known way of producing a mechanically cle~ gas from these flue-gases.
If a vortex chamber is used to burn the ground fuel, this produces a series of disadvantages, since a considerable amount of unburned substances must also be expected in the ash in the vortex chambsr. Unfortunately, the unburned substances are discharged from the vortex chamber with the 10w of flue-gas and thus inevitably reach the subsequent dust-removal unit. It is extremely difficult to ~eparate the total ash from the fuel and the partly-charged desulphurizer ;, : , . . - : - . .,., ., . -. - :
~Q~
from the flow of flue gas. It is also difEicult to separate the partly-charged desulphurizer from th~ ash for preparing the desulphurizer. In addition to this there are wear problems in connection witn the heating surfaces which have to be arranged within the fluidized layer. This wear is due mainly to the inevitable erosion in the fluidized layer. ~ccurate control of the fluidized-bed temperatures also presents con-: siderable difficulties. If, for instance, the fluidized-bed temperature rises too high, the ash softens and the fluidized bed bakes onto the heating surfaces. On the other hand, if the fluidized-bed temperature is too low, there is a drop in the degree of combustion and ~hus a corresponding increase in fuel losses. Furthermore, low-temperature carbonization sets in, and this causes the tar to condense and the fluidized bed to bake onto the heating surfaces.
It is the purpose of the invention to reduce the losses and operating problems in installations of the kind described at the beginning hereof, and to design an installation that can be used as a peak-load power station.
According to the invention, this purpose i3 achieved in that a melting-chamber boiler, to which the ground fuel is fed, is pressure fired, and in that the flue-gases pass to - desulphurizing and dust-removal units before they reach the gas turbine.
Since combustion takes place in one part of the installation (partial combustion and post-combustion), the two processes can be jointly controlled as required for a peak-load power station~ In other words, the output can be increased and reduced relatively quickly, and may thus be adapted to the power taken off, without heat loss and without supporting the combustion process with oil or other additional _ ~ _ -.~, .
.:
- : :-fuels. Since the fuel is burned in a melting-chan~er boiler (kettle, vessel), no tar occurs, no equipment is re~uired to deal with it, and the corresponding difficulties are eliminated.
Ihe pressure in ~e flue-gas side of the melting-chamber boiler may be 10 bars, for example, and this corresponds approximately ~o t~e gas-turbine pressure.
The main advantage~s of the new installation is that there is a negligeable amount of unburned substance in the melting-chamher slag, so little that it cannot be measured.
The thermal efficiency is considerably higher, since there are no losses by evaporation outside the steam circuit, such as have hitherto been unavoidable in the gasification of a fuel. The low water content in the flue-gas also assists in improving the thermal efficiency. This is the reason for the low dew-point and the relatively small waste-gas loss.
Another advangtage is that most of the ash is removed from the melting-chamber boiler in the form of granules and does not reach the turbine gas. The granular material thus removed may be further processed and used for other purposes.
Accordiny to another characteristic of the invention the flue-gases may be removed from bahind the radiating portion of the boiler. Moreover, heat-exchanger surfaces are provided, outside the boiler, for the flue-gases thus removed, and may be used to adjust the flue-gas temperature before the gas turbine. These heat-exchanger surfaces are used to produce the steam which is fed to the steam-power process. It is also desirable to burn the fuel directly under pressure in a cyclone since, as compared with the gasification technique, this saves a number of additional units (gas producers) and requires, for the combustion process, a unit substantially smaller tham that used in the fluidized-bed technique. It is also possible to locate ~e heat--exchanger surfaces, used to adjust the flue-gas temperature before the gas turbine, in the flue-gas desulphurizer. The said heat-exchanger surfaces may also follow the desulphurizer~
The actual desulphuriziny may be carried out with metal car~onates or oxides, using a solid bed in which the de-sulphurizer is in the form of pellets or briquettes. On the other hand, a fluidized becl may be used, or the desulphuriæer may be injected into the desulphurizing chamber in the form of a dry dust.
On the flue-gas side, a dry flue-gas dust-removal unit, operating at the existin~ high pressure, may be inserted after the said heat-exchanger surfaces~ l~his dust-removal unit may operate with ceramic candle filters or with separator nozzles, a hot cyclone bPing used, if necessary, as a pre-separator before the actual dust-removal process.
~ s regards subsequent equipment, the invention has the advantage that the heat-exchanger surfaces after the radiating portion of the boiler are substantially smaller as compared wi~h those in the proposed fluidized bed, and this reduces erosion. Furthermore, the desulphurizer is more easily separated from the ash, since there is considerably less ash than in the fluidized-bed process. This is also quite an advantage.
The details, further characteristics, and other - advantages of the invention may ~e gathered from the following descriptions of three examples of embodiment o~ the installation according to the invention, as illustrated in the drawing attached hereto, wherein :
Fig. 1 is a first example of embodiment of the installation according to the invention, in which the flue-gases are desulphurized in a fluidized bed;
-- , .
Fig. 2 is an e~ample oE en~odiment using a modified (injection) desulphuriæing unit;
Eig. 3 is an example of embodiment of the installa-tion accordiny to the invention using a solid-bed desulphuri-zing unit.
In the figures, similar parts of the installation bear the same reference numerals.
Coal containing inerts is fed rom a bunker 1 to a grindin~ unit 2 which passes thP grouncl fuel, througll a gate 3, to a line 4 running to the cyclone-firing unit of a melting-chamber boiler (kettle, vessel) marked 5 as a whole.
Id~ntification of the media in the lines corresponds to German Industrial Standard 2481.
'rhe flue-gases are removed at 7 and pass, in ~he installation according to Fiy. l to a fluidized-bed desulphuri zer 8. The desulphurizing agent used may be limestone, for example, which is fed, through a gate unit 9, to the desul-phurizing unit at lO and ll. The desulphurizing flue-gases leave the fluidized bed at 12 and pass to a cyclone which removas any coarse solids. These solids ara removed at 14 and are passed to a grading unit 15 consisting of several screens, fore~mpls. The overflow from the screens is passed on, through a line 16, for further processiny or use. l`he material passing through the screens is removed at 17 and passes, in the example of embodiment illustrated, to a gate 18 to which fine dust is fed through a line 20. The fine-dust separator ~a separator nozzle or filter) is shown at 21, and the flue gases from which the coarse solids have been removed are fed ther.eto.
The flue-gases leave fine separa-tor 21 at a tempera-ture of bet~leen 800 and 900C, fsr example, and pass, through . :
a line 22, to a gas turbine 23 which is followed by a waste-heat boiler 24. The flue-gases are th~n released to the atmosphere at 25.
Provision is made, in the example of embodiment illustrated, for the separated fine dust to be returned, through gate unit 18, pneumatically ~rough a line 26, to line 4, so that this part of the dust is returned to melting-chamber boiler 5.
Dust and ash is removed in the form of a liquid from boiler ~, and this passes to a hydraulic ash-removal unit and a crusher for granular material, this portion of the ins-talla-tion being marked 27. The granular material from the melting-chamber ash is separated from the transpor~ing water, and is removed, at a gate 28.
Boiler-feed water, which has been fed at 30 to waste-heat boiler 24, flows through a line 32 having a branch 34 running the radiating portion of melting-chamber boiler 5.
Steam leaves the boiIer at 35 and, as shown in the example ~ -of embodiment, it is passed through a heat-exchanger 36 arranged in ~idized-bed desulphurizer 8. This st~am then passes ~hrough a line 37 to a steam-turbine unit 38 with in~ermediate superheating 38a, followed by a condenser 39.
As indicated, the fossil fuels, in the form of coal, are fed directly to the ~ombination block described. This is also the case in the installations shown in Figs. 2 and 3.
The example of embodiment in Fig. 2 difers from that in Fig. 1 mainly in the type of desulphurizer to which the flue-ga~ses pass from line 7. The desulphurizing device i~ Fig. 2 is marked 40. It uses a dry desulphurizer in the form of a dust which is injected into desulphurizing vessel 41, at several locations, through nozzles marked 42-44. Again, -- 8 ~
.~
:
the desulphurizer is passed, with the aid of air from air-supply line ~7, shown in dotted lines, through a gate unit .~. 45, to the ~bove-mentioned nozzles.
The sulphur associated with the desulphurizer leaves vessel 41, in the form of a ~iolid, ~lrouyh a line 48 and is therefore passed to a gradiny unit 15 which has an overflow at lS. Part of the desulphurizer is returned to the gate through a line 49, and part is removed at 16a for processing or further . use. The amount removed is xeplaced at 16b by the addition of fresh desulphuxizer.
In the example of embodiment according to Fig. 3, solid-bed desulphuring is carried in a reaction vessel S0. In this case, the desulphurizer may be in the form of pellets or briquettes and may be fed continuously or intermittently through a gate 51. If any desulphurizer, and the sulphur associated therewith, is removed from vessel 50, this product returns at 51 to the screen overflow of grading unit 15, and so to line 16, fxom which the processed desulphurizer can be returned to the pxocess at 53.
.
_ g _ .
: "
.. : . - .
Claims
1. An installation for recovering energy from solid fossil fuels, more particularly, fuels high in inerts, and particularly bituminous coal, said installation comprising:
at least one steam generating wet bottom boiler pressure fired with ground fuel for converting the solid fuel to combustible flue gas;
gas turbine means operable by the flue gas for driving electrical generation means;
steam turbine means operable by the steam from said boiler for driving electrical generation means;
desulfurizing means interposed between said boiler and said gas turbine, said desulfurizing means having a heat exchanger means located therein for transferring heat between said flue gas and the steam from said boiler; and dust removing means interposed between said boiler and said gas turbine.
at least one steam generating wet bottom boiler pressure fired with ground fuel for converting the solid fuel to combustible flue gas;
gas turbine means operable by the flue gas for driving electrical generation means;
steam turbine means operable by the steam from said boiler for driving electrical generation means;
desulfurizing means interposed between said boiler and said gas turbine, said desulfurizing means having a heat exchanger means located therein for transferring heat between said flue gas and the steam from said boiler; and dust removing means interposed between said boiler and said gas turbine.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| DEP2650491.6 | 1976-11-04 | ||
| DE19762650491 DE2650491C2 (en) | 1976-11-04 | 1976-11-04 | Gas-steam turbine system for generating electrical energy |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CA1096641A true CA1096641A (en) | 1981-03-03 |
Family
ID=5992409
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA287,635A Expired CA1096641A (en) | 1976-11-04 | 1977-09-27 | Power generator |
Country Status (2)
| Country | Link |
|---|---|
| CA (1) | CA1096641A (en) |
| DE (1) | DE2650491C2 (en) |
Families Citing this family (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE2931427A1 (en) * | 1978-11-17 | 1981-02-19 | Steag Ag | PLANT FOR ENERGY FROM SOLID FOSSIL FUELS, IN PARTICULAR CHARCOAL |
| DE2850005A1 (en) * | 1978-11-17 | 1980-05-29 | Steag Ag | Pulverised coal pressure fired power plant - has steam turbine and uses cleaned gas from dry combustion to drive gas turbine |
| DE2924245C2 (en) * | 1979-06-15 | 1982-11-25 | Rheinische Braunkohlenwerke AG, 5000 Köln | Process for covering peaks in demand in the generation of electrical energy in a power plant using gas turbines |
| EP0044094A1 (en) * | 1980-07-09 | 1982-01-20 | BBC Aktiengesellschaft Brown, Boveri & Cie. | Method for desulfurization with a fluidized bed in a power plant burning pulverized coal, and power plant working according to this method |
| DE3124832A1 (en) * | 1981-06-24 | 1983-01-13 | Kraftwerk Union AG, 4330 Mülheim | HOT GAS SYSTEM |
| SE436248B (en) * | 1983-04-15 | 1984-11-26 | Asea Atom Ab | PRESSURE REDUCTION VALVE FOR EXPOSURE OF DUST FROM A PRESSURE CONTAINER EXAMPLE A CYCLON WHICH THE VALVE CONTAINS FLUIDIZABLE PARTICLES |
| DE3416181A1 (en) * | 1984-02-28 | 1985-09-12 | Ruhrkohle Ag, 4300 Essen | Energy generating system |
Family Cites Families (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE890009C (en) * | 1944-08-01 | 1953-09-14 | Basf Ag | Combustion chamber operated with coal dust for the operation of gas turbines |
| DE1240338B (en) * | 1961-07-12 | 1967-05-11 | Ladislav Michalicka | Gas turbine plant with a pressure combustion chamber for solid fuel |
-
1976
- 1976-11-04 DE DE19762650491 patent/DE2650491C2/en not_active Expired
-
1977
- 1977-09-27 CA CA287,635A patent/CA1096641A/en not_active Expired
Also Published As
| Publication number | Publication date |
|---|---|
| DE2650491C2 (en) | 1982-10-07 |
| DE2650491A1 (en) | 1978-05-18 |
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