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
  • F02C6/00—Plural gas-turbine plants; Combinations of gas-turbine plants with other apparatus; Adaptations of gas-turbine plants for special use
  • F02C6/18—Plural gas-turbine plants; Combinations of gas-turbine plants with other apparatus; Adaptations of gas-turbine plants for special use using the waste heat of gas-turbine plants outside the plants themselves, e.g. gas-turbine power heat plants
• • 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
  • F02C6/00—Plural gas-turbine plants; Combinations of gas-turbine plants with other apparatus; Adaptations of gas-turbine plants for special use
• • 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
  • F02C6/00—Plural gas-turbine plants; Combinations of gas-turbine plants with other apparatus; Adaptations of gas-turbine plants for special use
  • F02C6/003—Gas-turbine plants with heaters between turbine stages
• • 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
  • F02C6/00—Plural gas-turbine plants; Combinations of gas-turbine plants with other apparatus; Adaptations of gas-turbine plants for special use
  • F02C6/006—Open cycle gas-turbine in which the working fluid is expanded to a pressure below the atmospheric pressure and then compressed to atmospheric pressure
• • 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
  • Y02E20/14—Combined heat and power generation [CHP]

Definitions

• the present invention relates to a method and a device for co-generation of work and heat.
• It relates more particularly to a cogeneration process carried out by means of a turbine, in particular a gas turbine.
• the method consists in using the hot combustion gases generated by the gas turbine to exchange heat with an industrial installation in order to carry out, for example, an endothermic reaction.
• Previous cogeneration methods consist in using the hot combustion gases leaving the turbine, which are generally at a pressure close to atmospheric pressure, to generate, for example, pressurized steam by means of a heat exchange carried out in an exchanger crossed by these hot gases and traversed by a fluid, such as water.
• These systems can supply a steam distribution system capable of supplying various industrial installations, such as the heating of reboilers of the distillation columns.
• the disadvantage of such a process lies in the fact that the temperature of the hot gases is not sufficient to heat industrial installations operating at relatively high temperatures, for example above 500 ° C. Furthermore, the direct use of hot gases leaving the gas turbine is difficult, since the pressure drop at the outlet of the gas turbine must remain very low, since these gases exit at a pressure close to atmospheric pressure and that any pressure drop, even relatively small, strongly disrupts the performance of the gas turbine.
• the present invention therefore proposes to remedy the above-mentioned drawbacks by means of a method and a device making it possible to keep the power generated by the gas turbine substantially constant and to obtain a temperature of the hot combustion gases at the inlet of the expansion turbine substantially close to the initial introduction temperature in the absence of heat exchange.
• the present invention relates to a process of cogeneration by turbine, in particular of gas turbine, comprising a compression section, at least one expansion section and a combustion chamber, process in which the following steps are carried out: (a) an oxidizer comprising oxygen is compressed in the compression section; (b) a combustion step is carried out in the combustion chamber under pressure of a mixture of the compressed oxidizer with a fuel;
• step (d) at least one post-combustion stage is carried out of a mixture of the hot gases, resulting from the exchange, with a fuel, so as to obtain hot gases which are sent to the expansion section, under temperature conditions and pressure close to the conditions achieved in the absence of step (c).
• the post-combustion stage can be carried out by introducing a quantity of fuel, which is adjusted so as to obtain a temperature of the hot gases at the inlet of the expansion section substantially close to the initial temperature of introduction in the absence of 'exchange.
• a steam production operation or a charge reforming operation can be carried out by exchange with the external installation.
• the invention also relates to a turbine cogeneration device, in particular a gas turbine, comprising a compression section, at least one expansion section, a combustion chamber and a means exchange between the hot gases from the combustion and a fluid to be heated, characterized in that the device comprises at least one afterburner chamber supplied by the hot gases from the exchange means.
• a turbine cogeneration device in particular a gas turbine, comprising a compression section, at least one expansion section, a combustion chamber and a means exchange between the hot gases from the combustion and a fluid to be heated, characterized in that the device comprises at least one afterburner chamber supplied by the hot gases from the exchange means.
• the device may include an afterburner chamber supplying the exchange means with hot gases.
• the device can also include a short-circuit pipe making it possible to adjust the temperature of the hot gases at the outlet of the combustion chamber and / or of the afterburner chamber.
• It can also include a hot gas pipe directly connecting the combustion chamber by means of exchange.
• the exchange means can include a heat exchanger and / or a reactor.
• the device may include a first expansion section and a second expansion section and a hot gas pipe connecting the first section to the second.
• Figure 2 is a first variant of the device as illustrated in Figure
• Figure 3 is a variant of the device of Figure 2;
• FIG. 4 is a diagram showing the installation of the device according to the invention in a load reforming installation
• FIG. 5 is another variant configuration of the device according to FIG. 1; and - Figure 6 is another alternative configuration of the device according to the invention.
• FIG. 1 shows a device with a particular type of gas turbine, called a twin-shaft turbine.
• the gas turbine comprises an expansion-compression cell 10 in which a first expansion step makes it possible to compress the combustion air and a expansion cell 12 with a second expansion step making it possible to generate mechanical power and / or electric.
• the expansion-compression cell 10 comprises a compressor 14 linked by a shaft 16 to a first expansion section with an expansion turbine 18 and a combustion chamber 20.
• a fluid containing oxygen generally outside air, is admitted by a line 22 into the compressor 14 from which it emerges in the compressed state by a line 24.
• the combustion chamber 20 is supplied with fuel, such as natural gas, by a line 26 and by an oxidizer which is, in the present case, all or part of the compressed air conveyed by the pipe 24.
• the hot gases originating from the combustion of the mixture of the fuel with the compressed air in the combustion chamber 20 are directed by a pipe 28 into the expansion turbine 18 where they are expanded and then evacuated by a pipe 30.
• part of the compressed air leaving the compressor is sent to the combustion chamber 20 by the pipe 24, the part re stante being directed directly to the hot gas pipe 28 by a short-circuit pipe 32 the operation of which will appear in the following description.
• the device also comprises an exchange means, in particular a heat exchanger means 34, such as a tube and calender heat exchanger, traversed by a fluid to be heated which enters via the intake pipe 36 and leaves this exchanger by a outlet pipe 38.
• This exchanger has an inlet 40 for hot combustion gases conveyed through line 30. These hot gases pass through the exchanger 34 to transmit their calories to the fluid to be heated.
• the hot gases exit the exchanger by an outlet 42 connected by a pipe 44 to an afterburner chamber 46 which is supplied with fuel by a pipe 48, this fuel possibly being the same as that which feeds the combustion chamber 20.
• the afterburner chamber 46 will be referred to in the following description of the downstream afterburner chamber, because it is located downstream of the exchange means 34 and this considering the direction of circulation of the hot gases coming from the combustion chamber 20.
• the hot gases resulting from the post-combustion of the mixture of fuel and hot combustion gases from line 44 are directed by a line 50 in a second expansion section with an expansion turbine 52 which comprises the expansion cell 12, from where they come out, after expansion, through a pipe 54.
• This turbine is connected by a shaft 56 to any means producing mechanical and / or electrical power, such as for example an alternator 58. As shown in FIG.
• the operation of the installation described above is as follows:
• the air admitted via line 22 is compressed in compressor 14, from which it emerges in the compressed state through line 24.
• Part of this air from compression is sent to the combustion chamber 20, in which it is mixed with the fuel arriving via the line 26.
• the combustion in this chamber produces hot combustion gases which are mixed, at the outlet of this combustion chamber 20, with the compressed air from the compressor, which has not been sent to the combustion chamber and which arrives via the short-circuit line 32.
• This makes it possible to adjust the temperature of the hot gases resulting from the combustion to a compatible level with temperature required at the inlet of the first expansion turbine 18, for example between 1000 and 1300 ° C.
• the hot gases leaving the turbine 18 via the pipe 30, at a temperature close to 650 ° C., are then sent to the exchanger 34, in which they are cooled by heating the external fluid, such as water, which enters the exchanger via line 36 and leaves it via line 38 in a desired state, for example in the form of water vapor.
• These hot gases are under pressure, for example at a pressure close to 4 bars.
• the hot gases are at a temperature substantially lower than that of their inlet, the temperature difference with respect to the inlet 40 being for example greater than 100 ° C. These hot gases are then sent to the downstream afterburner chamber 46. Since the amount of air entering the compressor 14 through line 22 is much greater than the amount of stoichiometric air required for combustion of the fuel arriving through the line 48, post-combustion can be carried out in the chamber of 46 by using, as the oxidant, a fraction of the hot gases leaving the exchanger 34, the remaining fraction passing through the short-circuit line 60 so as to adjust the temperature of the mixture of hot gases resulting from afterburning to a level compatible with the temperature required at the inlet of the second expansion turbine 52.
• the quantity of fuel used to carry out this afterburning and arriving via line 48 is also adjusted, in combination with the quantity hot gas flowing in the short-circuit line 60, so as to obtain the inlet of the second expansion turbine 52, a temperature close to that which is required in the absence of the exchange operated in the exchanger 34, for example between 1000 and 1300 ° C.
• the hot post-combustion gases thus obtained are expanded in the expansion turbine 52, producing a mechanical power close to that which is obtained in the absence of the exchange carried out in the exchanger 34. This mechanical power is used, in the 'example described, to drive the alternator 58.
• the hot gases are evacuated to a pressure close to atmospheric pressure via line 54.
• FIG 2 shows an alternative embodiment of Figure 1 and includes the same references for this.
• This preliminary step is carried out in an afterburner chamber 62 which makes it possible to heat the hot gases leaving the first expansion turbine 18 and before they enter the exchanger 34.
• This afterburner chamber is called the upstream afterburner chamber because it is located upstream of the exchange means 34 and this always considering the direction of circulation of the hot gases coming from the combustion chamber 20.
• this upstream afterburning chamber is supplied with fuel, such as gas natural, by a pipe 64 and in hot gases by the pipe 30 connecting the expansion turbine 18 to this chamber.
• the hot gases leaving the afterburner chamber 62 are directed through a pipe 66 to the inlet 40 of the heat exchanger 34.
• a short circuit pipe is provided.
• a first post-combustion stage is carried out in the combustion chamber 62 with the combustion of the fuel arriving via the line 64 and a fraction of the hot gases leaving the expansion turbine 18 via the line 30, the remaining fraction of the hot gases passing through the short-circuit pipe 68 to adjust the temperature of the hot gases leaving this chamber before they enter the exchanger 34.
• a second post-combustion stage is carried out in the post-combustion chamber 46, with the hot gases leaving the exchanger 34 and the fuel arriving via the line 48, the quantity of which is adjusted so as to obtain the temperature required at the inlet of the expansion turbine 52.
• the example of arrangement shown in FIG. 2 is particularly well suited for carrying out the heating of an endothermic reaction occurring at relatively high temperature, such as for example a steam reforming reaction to produce hydrogen from '' a gas-based filler, in particular natural gas.
• Such an endothermic reaction can also be used in combination with other fillers, such as petroleum fractions, alcohols, such as methanol, or possibly other fillers.
• other fillers such as petroleum fractions, alcohols, such as methanol, or possibly other fillers.
• FIG. 3 Such an application case is illustrated by the diagram of the installation in FIG. 3 for a steam reforming reaction to produce hydrogen from a gas-based charge.
• This installation comprises a device which essentially has the same elements as those in FIG. 2 and, for this, will bear the same references.
• the exchange means is a reactor 70 of the reactor-exchanger type which includes a gas inlet pipe 72, preferably natural gas, and an inlet pipe for a fluid 74, such as water vapor. These two fluids mix at the junction of the two pipes and are sent via a pipe 76 to the inlet of the reactor.
• the synthesis gas obtained leaves through a pipe 78 by which it is sent to any known treatment device.
• This reactor also includes an inlet for hot gases 80 brought from the upstream afterburner chamber 62 through line 66 and an outlet for hot gases 82 to downstream afterburner chamber 46 through line 44.
• natural gas arrives through line 72. It has been preheated by means of heat exchangers, not shown.
• the water vapor arrives through line 74 and is mixed with natural gas at the junction point between the two lines.
• the molar ratio of the amount of water introduced through line 74 to the amount of natural gas through line 72 is between 2 and 4.
• the resulting mixture is introduced through line 76 into the reactor 70.
• the endothermic reforming reaction which is operated in reactor 70, makes it possible to produce a mixture of carbon monoxide CO and hydrogen H 2 .
• the gas mixture operates in tubes, in the presence of a catalyst, which can for example be based on either nickel deposited on calcium or magnesium silico-aluminate doped with potassium hydroxide, or nickel on an alumina support.
• the temperature reached at the outlet from the reaction zone is between 850 and 940 ° C.
• the reaction is carried out at a pressure between 20 and 40 bars.
• the heating of the reactor is ensured by the hot gases arriving via line 66, at a pressure for example close to 4 bars and circulating in the shell, generally against the current. It is also possible to carry out co-current heating, so as to limit the wall temperature of the tubes.
• the mixture of carbon monoxide and hydrogen obtained is discharged through line 78.
• the carbon dioxide can be separated by the various methods known to those skilled in the art, for example by washing with a solvent.
• the hydrogen produced can then be purified by adsorption or by membranes, separating unconverted hydrocarbons, which can be recycled to the inlet of natural gas.
• the hydrogen thus produced can be used at least in part to supply the gas turbine as fuel, so as to generate electricity by the alternator, greatly reducing carbon dioxide emissions.
• the method as described above comprises the following steps:
• a pressurized combustion step is carried out with a mixture of a fuel and of the compressed oxidizer
• step (d) at least one post-combustion stage is carried out of a mixture of the hot gases from the exchange with a fuel, so as to obtain hot gases which are sent to the turbine 52, under close temperature and pressure conditions conditions achieved in the absence of step (c).
• the method makes it possible to use hot pressurized gases generated during the mechanical energy production process while preserving the performance of the gas turbine.
• This process can be used with a reforming installation, as illustrated, by way of example, in the diagram in FIG. 4.
• the turbine used is a GE Frame 7 type gas turbine, using the terminology of the manufacturer, General Electric. Such a machine is capable of producing mechanical power of up to 80 MW under iso conditions.
• the axial compressor 14 draws, via line 22, approximately 958 t / h of compressed ambient air up to a pressure of approximately 18 bars.
• the air thus compressed circulating in line 24 is mixed, in combustion chamber 20, with approximately 7 t / h of a hydrogen-rich fuel arriving through line 26 and the mixture obtained is burned in combustion chamber 20 At the outlet of the combustion chamber 20, a mixture of hot gases is obtained at a temperature of approximately 1200 ° C.
• the hot gases are then sent, via line 28, to the first expansion turbine 18, from which they exit, via line 30, at a pressure of approximately 4 bars and a temperature of approximately 750 ° C. They are then mixed, in the upstream afterburning chamber 62, with an additional quantity of approximately 4 t / h of hydrogen-rich fuel arriving via line 64. A mixture is thus obtained, at the outlet of the afterburning chamber 62 hot gases at a temperature of about 1150 ° C., which are used, via line 66, to heat the reactor 70, of the reactor-exchanger type.
• the hot gases leaving the reactor-exchanger 70 via line 44 are mixed, in the downstream afterburner chamber 46, with a third fuel fraction representing approximately 1 t / h of hydrogen-rich fuel arriving through line 48.
• the hot gases circulating in the pipe 50 are again at a temperature of around 750 ° C. They are then expanded in the second expansion turbine 52 from which they exit through line 54 at a pressure of approximately 1.3 bars and a temperature of approximately 565 ° C.
• the power generated in the expansion turbine is 55 MW.
• the hydrogen-rich fuel is produced by reforming approximately 50 t / h of natural gas arriving via line 72 in the presence of approximately 170 t / h of water vapor arriving via line 74. This water vapor is generated in a recovery boiler 84 by heat recovery from the hot gases leaving the second expansion turbine 52 via the pipe 54.
• the water vapor is generated from demineralized water arriving via a pipe 86 and recirculating in the loop exchange 88.
• the synthesis gas obtained and circulating in line 78 goes through a second conversion step, called "shift-conversion" by specialists in the field, during which it reacts in the presence of steam of water to produce an additional quantity of hydrogen, while converting part of the CO produced into carbon dioxide.
• shift-conversion a second conversion step, called "shift-conversion" by specialists in the field, during which it reacts in the presence of steam of water to produce an additional quantity of hydrogen, while converting part of the CO produced into carbon dioxide.
• a flow of 56 t / h of water is supplied via a pipe 90, which is consumed by the “shift-conversion” reaction in a reactor 92.
• This “shift-conversion” reaction must be carried out at a temperature lower than that which is required to carry out the main reforming reaction. The temperature is maintained at around 400 ° C, generating 46 t / h of steam.
• the steam generated in the recovery loop 88 represents 164 t / h, of which 124 t / h are used for the production of synthesis gas.
• the flow rate of 40 t / h not used to generate the synthesis gas, can be either exported or used in a condensation cycle.
• the synthesis gas leaving the reactor 92, via line 94, is then sent to a section for washing and purifying the hydrogen (not shown).
• FIG. 5 is a variant of FIG. 3 and in which the hot gases resulting from combustion in the combustion chamber 20 are evacuated via a pipe 96 directly to the inlet 80 of the reactor 70, at a pressure which can for example be between 10 and 40 bars. In this case, it may be advantageous to operate the reaction which is carried out in the reactor 70 at a pressure at least slightly higher, so as to avoid any risk of passage of a gas containing oxygen towards the reactants.
• the hot gases leaving the reactor 70 via line 44 are then sent to the downstream afterburner chamber 46.
• the quantity of fuel supplied by line 48 is adjusted so as to obtain gases at the inlet of the first expansion turbine 18 hot, conveyed by a pipe 98 connecting the downstream afterburner chamber and the first expansion turbine 18, at the temperature required to obtain a mechanical power close to the maximum power that can be delivered by the turbine.
• the hot gases leaving this expansion turbine 18 are then sent, via a line 100 to the second expansion turbine 52 driving the alternator 58.
• a single turbine 102 is connected by the same shaft 16, on the one hand, to the compressor 14 and, on the other hand, to the alternator 58.
• the hot gases leaving the downstream combustion chamber 46 are sent via line 98 to the expansion turbine 102, which not only drives the compressor 14, but also the alternator 58.
• the reactor-exchanger can be produced using tubes of ceramic material, selectively permeable to oxygen.
• the reactor-exchanger can be produced using tubes of ceramic material, selectively permeable to oxygen.
• the reactor-exchanger can be produced using tubes which are selectively permeable to hydrogen, for example tubes comprising a selective layer of palladium.
• the hydrogen can thus be directly separated and mixed with the oxidizer, in order to carry out the post-combustion step.

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• Engineering & Computer Science (AREA)
• Chemical & Material Sciences (AREA)
• Combustion & Propulsion (AREA)
• Mechanical Engineering (AREA)
• General Engineering & Computer Science (AREA)
• Engine Equipment That Uses Special Cycles (AREA)
• Hydrogen, Water And Hydrids (AREA)
• Incineration Of Waste (AREA)
• Filling Or Discharging Of Gas Storage Vessels (AREA)

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• 2003
  • 2003-03-13 FR FR0303141A patent/FR2852358B1/fr not_active Expired - Fee Related
• 2004
  • 2004-03-11 EP EP04719501A patent/EP1608858A2/de not_active Withdrawn
  • 2004-03-11 JP JP2006505720A patent/JP4842801B2/ja not_active Expired - Fee Related
  • 2004-03-11 RU RU2005131619/06A patent/RU2309275C2/ru not_active IP Right Cessation
  • 2004-03-11 CA CA002518460A patent/CA2518460A1/fr not_active Abandoned
  • 2004-03-11 WO PCT/FR2004/000600 patent/WO2004083729A2/fr active Application Filing
  • 2004-03-11 US US10/548,738 patent/US7703271B2/en not_active Expired - Fee Related

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