• 专利附录
  • 专利说明
  • 权利要求
  • 类似技术
  • 同族专利
  • 引用文献
  • 法律状态
  • 优先权
    • 专利摘要:
    Process and combustion plant in which an oxygen-rich oxidant (43) is preheated by heat exchange with a coolant (23), upstream of the combustion chamber (100), in which an auxiliary gas (21) is heated by heat exchange with a first portion of the hot fumes (11) discharged from the chamber (100), and wherein the coolant (23) comprises a mixture of at least a portion of the heated auxiliary gas (22) with a portion (13) ) hot fumes.
    公开号:FR3015637A1
    申请号:FR1363477
    申请日:2013-12-23
    公开日:2015-06-26
    发明作者:Luc Jarry；Youssef Joumani；Bertrand Leroux；Remi Tsiava
    申请人:Air Liquide SA；LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude；
    IPC主号:
    专利说明:

    [0001] The present invention relates to a method for the combustion of a fuel using as oxidant a preheated gas rich in oxygen. In industry, air remains the oxidant, that is to say the combustion oxidant, the most often used. However, it is known to use oxygen as an oxidizer instead of air, especially to improve the combustion efficiency and thus the energy efficiency of an industrial installation comprising a combustion chamber, to maximize operation. the thermal energy generated in the combustion chamber and to reduce the combustion chamber emissions, such as NOx, If the energy and environmental interest of combustion with oxygen is well known and recognized, the The cost of oxygen relative to that of air continues to limit the use of oxygen as an oxidant in an industrial context. In order to further improve oxycombustion efficiency and thereby reduce the need for fuel and oxygen for a given industrial process, oxygen preheating processes have been developed.
    [0002] In particular, it is known to preheat oxygen in a heat exchanger. In particular, a method is known for the indirect preheating of oxygen with residual heat present in the combustion gases (fumes) at the outlet of the combustion chamber. According to this method, a predominantly inert auxiliary fluid is preheated in an auxiliary exchanger by direct exchange with the hot fumes. The oxygen is then preheated in at least one main heat exchanger by direct exchange with the hot auxiliary fluid from the auxiliary exchanger. If necessary, the fuel is also preheated by direct exchange with the hot auxiliary fluid in an additional heat exchanger. Various embodiments of this method are described in particular in EP-A-0872690 and WO2006 / 054015.
    [0003] Compared with other known methods for preheating oxygen, this method has the important advantage of greater safety. Indeed, in the event of perforation by corrosion or erosion inside the auxiliary exchanger, the hot fumes, likely to contain the residual combustible material, come into contact with the mainly inert auxiliary fluid . Similarly, in the event of a perforation inside a main or additional exchanger, the oxygen or the fuel only comes into contact with the predominantly inert auxiliary fluid.
    [0004] The energy balance of this method is particularly positive. A disadvantage of this method is however the space created by the different heat exchangers and in particular by the auxiliary exchanger, knowing that, to avoid heat loss, said heat exchangers are positioned as close as possible to the outlet of the fumes of the chamber of combustion.
    [0005] Another disadvantage is the price of the different heat exchangers which, given the temperatures and the nature of the fluids flowing in, must be particularly robust. The exchangers are designed and dimensioned for optimal operation at the conditions (temperatures and flow rates of the fluids circulating in the exchangers) which correspond to the nominal conditions of the industrial plant comprising the combustion chamber, that is to say to the operating conditions normal of the industrial installation. However, the industrial installations may be operated outside their nominal conditions, and more particularly with a higher need for heat than during its normal operation, for example because of aging and wear of the installation, or during a pull campaign increased by a melting furnace. In this case, the operation of the preheating method is not optimal because the auxiliary exchanger has a residual heat recovery capacity exhaust fumes too low compared to the need for heat: the residual heat actually recovered is then insufficient for the use or the different uses that one wishes to make of it, such as the preheating of oxygen, the preheating of the fuel and / or other uses. This leads to a higher consumption of energy, including fuel. Consideration could be given to using an auxiliary heat exchanger with a higher heat recovery capacity than that corresponding to the nominal operation of the installation or to installing an additional auxiliary heat exchanger to be used only when the need for heat recovery is higher than that in nominal operation of the installation. However, this would lead to an even larger size and price of the installation. The present invention aims to at least partially overcome the problems described above.
    [0006] It is intended in particular to allow an increase in the efficiency of heat exchanges without increasing the cost of implementing the process, or even reducing this cost. According to the invention, this is achieved by a direct supply of heat by the introduction of hot fumes in a coolant used for preheating. The present invention more particularly relates to a first improved method for the combustion of a fuel with a preheated oxidant rich in oxygen in a combustion chamber. This combustion generates heat and hot smoke in said combustion chamber. The hot fumes, which contain residual heat, are removed from the combustion chamber. Residual heat is then recovered from the evacuated fumes by heating a gas, said auxiliary gas, by heat exchange with at least a portion of the hot fumes discharged into a first heat exchanger, said auxiliary heat exchanger. This gives a hot auxiliary gas and temperate smoke. At least a first portion of the hot auxiliary gas thus obtained is introduced into a second exchanger, said main heat exchanger, wherein the oxidant is preheated by heat exchange with a heat transfer gas comprising said at least a first portion of the hot auxiliary gas. This gives a preheated oxidizer and a tempered heat transfer gas. The preheated oxidant is supplied to the combustion chamber for combustion of the fuel. According to the invention, it is possible to increase the thermal energy content of the heat transfer gas by mixing a portion of the exhausted hot fumes, which is not introduced into the auxiliary exchanger, with the at least a first portion of the auxiliary gas. hot before said at least a portion of the hot auxiliary gas is introduced into the main heat exchanger for preheating the oxidant. Due to this higher thermal energy content of the heat transfer gas, the present invention makes it possible to meet a higher need for thermal energy in the combustion chamber, for example a higher need for thermal energy than the nominal requirement of the installation.
    [0007] The invention also makes it possible to compensate for a reduction in the efficiency of one or more of the heat exchangers due, for example, to an aging of the installation. In the present context, the following are understood to mean: an "oxygen-rich" or "rich" gas: a gas having an oxygen content greater than or equal to 70% vol, preferably greater than or equal to 90% vol, or even greater or equal to 95% vol (ie 95% vol to 100% vol); - a "predominantly inert" gas: a gas consisting of more than 50% by volume of one or more substances which do not participate in the combustion (neither as a fuel nor as an oxidant) to the existing conditions in the combustion chamber. A predominantly inert gas therefore necessarily contains less than 50 vol% oxygen; - "heat exchanger": an installation or a heating device in which the first fluid (gas), which provides heat, and the fluid (gas), to heat circulate in separate enclosures, the first fluid transmitting the heat to the fluid to be heated through one or walls separating the two enclosures; "Burner": a device or a set of devices for bringing at least one fuel into contact with at least one oxidizer in order to allow the combustion of the at least one fuel by means of the at least one oxidant. A burner typically comprises injectors and / or lances for the injection of fuel and oxidant into a combustion zone. A burner may also include other elements, such as an igniter, a flame detector, etc ... - "residual heat": the heat that is removed from the combustion chamber with the fumes generated by the combustion; "Preheating": the heating of a product, such as a fuel, an oxidizer or a charge to be heated or melted, before its introduction into the combustion chamber; In the present context, two elements or devices are "fluidically connected" when these two elements are connected by at least one pipe or at least one pipe so as to allow the transport of a fluid through the at least one pipe or through said at least one conduit from one of the two elements to the other of the two elements. According to the invention, the auxiliary gas is preferably a predominantly inert auxiliary gas.
    [0008] The auxiliary gas may in particular be chosen from air, steam and CO2, or a mixture of at least two of said gases, the auxiliary gas being preferably air. As indicated above, the recovery of residual heat by means of a predominantly inert auxiliary gas has the advantage of a high degree of safety.
    [0009] Insofar as, according to the present invention, the content of hot fumes in the heat-transfer gas remains rather low, this security is maintained. Thus, it will advantageously maintain the content of hot fumes discharged from the heat transfer gas is less than or equal to 30% vol, and preferably less than or equal to 20% vol. In order to increase the thermal energy content of the heat transfer fluid significantly, the content of hot fumes discharged from the heat transfer gas is preferably at least 10% vol. The volumetric ratio between, on the one hand, hot exhaust fumes and, on the other hand, hot auxiliary gas in the coolant gas is preferably less than or equal to 43% vol, preferably less than or equal to 25% vol, and preferably at least 11% vol. As indicated above, the auxiliary heat exchanger and the main heat exchanger are typically designed and dimensioned for optimum operation at the rated conditions of the industrial plant including the combustion chamber. In this case, the heat energy content of the first part of the hot auxiliary gas is sufficient for the preheating of the oxidant to the normal operating conditions of the industrial installation and it is not necessary to increase the thermal energy content. heat transfer gas under these normal conditions, but only when the process requires a higher recovery of the residual heat of the evacuated fumes. The present invention thus also relates to a second flexible method for the combustion, in a combustion chamber, of a fuel with a preheated oxidant rich in oxygen with generation of heat and hot fumes within said combustion chamber. As already described above in connection with a first method according to the invention, the hot fumes, which contain residual heat, are removed from the combustion chamber. Residual heat is recovered from said exhaust fumes by heating an auxiliary gas by heat exchange, in an auxiliary heat exchanger, with at least a portion of the hot fumes discharged. This gives warm auxiliary gas and temperate smoke. At least a portion of the hot auxiliary gas is then introduced into a main heat exchanger in which the oxygen-rich oxidant is preheated by heat exchange with a heat-transfer gas, said heat-transfer gas comprising said at least a portion of the hot auxiliary gas. This gives preheated oxidant and tempered heat transfer gas. The preheated oxidant rich in oxygen is then supplied to the combustion chamber for combustion of the fuel.
    [0010] The second method according to the invention is flexible in that it has several modes of operation: a first mode of operation in which the heat transfer gas does not comprise fumes evacuated, this first mode of operation being used for example during the nominal operation of the industrial installation, and - a second mode of operation in which the thermal energy content of the heat-transfer gas is increased by adding a part of the hot exhaust fumes which has not been introduced into the exchanger auxiliary and whose residual heat was not recovered to heat the auxiliary gas. Said second mode of operation therefore corresponds to the first method according to the invention, of which various embodiments have been described above. In the first mode of operation of the second method, the heat transfer gas consists of hot auxiliary gas. The processes according to the invention advantageously also include a step in which the fuel is also preheated in a heat exchanger called a fuel exchanger 20 by heat exchange with a second heat transfer gas. When the second heat transfer gas corresponds to the first heat transfer gas, the preheating of the oxidant and the fuel are in series. When the second heat transfer gas used for the preheating of the fuel comprises a second portion of the hot auxiliary gas distinct from the at least a first portion of the hot auxiliary gas of the first heat transfer gas, the preheating of the oxidant and the preheating of the fuel are carried out. series. The present invention thus makes it possible to recover a portion of the residual heat from the hot fumes evacuated which is greater than that which can only be recovered with the auxiliary exchanger. In other words, the present invention allows an optimal recovery of the residual heat of the fumes discharged by means of the auxiliary heat exchanger during the nominal operation of the installation (first mode of operation), but it also makes it possible to respond a greater need for thermal energy from the installation by recovering a larger part of the industrial heat (second mode of operation): a first part of the residual heat being recovered by heat exchange between hot fumes discharged and the auxiliary gas in the auxiliary exchanger; a second part of the residual heat being recovered by direct mixing of hot fumes discharged with the hot auxiliary gas. The combustion processes according to the invention are advantageous for a large number of applications. The combustion chamber can thus be a melting chamber, a refining chamber or a melting / refining chamber, for example for melting glass (including enamel) or for melting metals. The melting chamber can also be a combustion chamber of a boiler. The invention is particularly useful in the case where the combustion chamber is a glass melting chamber, a glass refining chamber or a glass melting / refining chamber, such as, for example, the melting / refining chamber. a "float" type glass furnace for making flat glass. The present invention also relates to an installation adapted for the implementation of a combustion method according to the invention. Such an installation comprises a combustion chamber, a first heat exchanger, called auxiliary exchanger, and a second heat exchanger, said main exchanger. The combustion chamber is provided with injectors for injecting fuel and for injecting an oxidant into the combustion chamber and a flue gas outlet. The auxiliary exchanger comprises, on the one hand, a hot flue gas inlet and a tempered smoke outlet and, on the other hand, an auxiliary gas inlet to be heated and a hot auxiliary gas outlet. The hot flue outlet of the combustion chamber is fluidly connected to the hot flue gas inlet of the auxiliary heat exchanger.
    [0011] The main exchanger comprises, on the one hand, a hot heat-transfer gas inlet and a tempered heat-transfer gas outlet and, on the other hand, an oxidizer inlet to be preheated and a preheated oxidizer outlet. The auxiliary hot gas outlet of the auxiliary exchanger is fluidly connected to the hot heat transfer gas inlet of the main exchanger. The preheated oxidant outlet is fluidly connected to at least one of the injectors in the combustion chamber. According to the invention, the installation also comprises a pipe connecting fluidically or capable of fluidically connecting the hot flue outlet with the heat transfer gas inlet of the main exchanger in parallel with the auxiliary heat exchanger. This pipe allows in this way to allow the flow of a controlled portion of the hot smoke from the smoke outlet to the hot heat transfer gas inlet of the main heat exchanger.
    [0012] The plant according to the invention may also comprise a fuel exchanger for preheating fuel by means of a second fuel gas upstream of the combustion chamber. As described above with respect to the processes according to the invention, this fuel exchanger can operate in series or in parallel with the main exchanger which preheats the oxidizer.
    [0013] The fuel exchanger and the main exchanger may be surrounded by separate enclosures or envelopes or may be wrapped in the same enclosure. Injectors for fuel and oxidant injection are generally incorporated into burners and / or injection lances. As indicated above, the combustion chamber can thus be a melting chamber, a refining chamber or a melting / refining chamber, for example for melting glass (including enamel) or for melting. of metals. The melting chamber can also be a combustion chamber of a boiler. The invention is particularly useful in the case where the combustion chamber is a glass melting chamber, a glass refining chamber or a glass melting / refining chamber, such as, for example, the melting / refining chamber. 'a float type glass furnace. As already indicated, it is possible that the necessity or the interest of operating an industrial installation outside its nominal conditions, and more particularly with a higher need for heat than during its normal operation, is only manifested by some time after the start of the installation, for example because of the aging and wear of the installation and the combustion chamber and / or several of the heat exchangers. The interest of the present invention can then become manifest a certain time after the construction of the installation. One can then take advantage of a temporary stop of the installation, for example between two campaigns, to proceed to the adaptation of the installation for the implementation of a method according to the invention.
    [0014] The present invention thus also relates to a method of modifying an installation comprising a combustion chamber, a first heat exchanger, said auxiliary exchanger, and a second heat exchanger, said main heat exchanger, in which: - the combustion chamber is provided with injectors for the injection of a fuel and for the injection of an oxidant into the combustion chamber and a smoke outlet, the auxiliary exchanger comprises, on the one hand, an inlet of hot fumes and a tempered smoke outlet and, secondly, an auxiliary gas inlet to be heated and a hot auxiliary gas outlet, the hot flue outlet of the combustion chamber being fluidly connected to the inlet of hot fumes of the auxiliary exchanger, and - the main heat exchanger comprises, on the one hand, a hot heat-transfer gas inlet and a tempered heat-transfer gas outlet and, on the other hand, a preheat oxidant inlet. ffer and a preheated oxidant outlet, the auxiliary auxiliary gas outlet of the auxiliary exchanger being fluidly connected to the hot heat transfer gas inlet of the main exchanger, the preheated oxidant outlet being fluidly connected to at least one of the injectors of the combustion chamber. According to the modification method according to the invention, there is added to said installation a duct capable of fluidically connecting the hot flue outlet with the heat transfer gas inlet of the main exchanger in parallel with the auxiliary exchanger, so as to allow the flow of a controlled portion of the hot fumes from the flue gas outlet to the hot heat transfer gas inlet of the main exchanger. As already indicated, the combustion chamber is a melting chamber, a refining chamber, a melting / refining chamber or a combustion chamber of a boiler, preferably a glass melting chamber, a refining chamber of glass, a melting chamber / glass refining. The present invention is illustrated by the example below, reference being made to Figure 1 which is a schematic representation of an installation adapted for the implementation of a combustion process according to the invention. In the present example, the process according to the invention is more particularly combined with the method described in the unpublished co-existing patent application No. FR 1363459 of the applicant.
    [0015] Said method makes it possible to limit the costs of the equipment used for the preheating of oxidant by the use of a first exchanger for heating an oxidant rich in oxygen, followed by a second exchanger for preheating the oxidant, said oxidant being obtained by mixing the oxidant heated in the first exchanger with a predominantly inert gas upstream of the second exchanger. The installation comprises a melting chamber, for example a glass melting chamber 100, equipped with burners 200 for the combustion of a fuel, such as natural gas with an oxidant rich in oxygen. Although only one burner is shown in FIG. 1, such a melting chamber generally comprises several burners. This combustion generates heat and smoke inside the chamber 100. The heat generated by this combustion is used for the melting of vitrifiable material in the chamber 100. The fumes are removed from the chamber by a fumes outlet 300 The evacuated fumes are hot (typically of the order of 1200 ° C to 1600 ° C) and contain a non-negligible amount of residual heat.
    [0016] The present invention allows optimized recovery and exploitation of residual heat. At least a portion of the exhausted hot fumes are introduced into an auxiliary exchanger 10 in which circulates air used as auxiliary gas 21 (hereinafter referred to as "auxiliary air"). As only part of the hot fumes is introduced into the auxiliary exchanger 10, this part advantageously corresponds to at least 70% vol, preferably at least 75% vol and more preferably at least 80% vol flue gases. In the auxiliary exchanger 10, the auxiliary air is heated by heat exchange with the hot fumes. Hot auxiliary air 22 is thus obtained, typically at a temperature of 600 ° C. to 900 ° C. and tempered fumes. The hot auxiliary air is introduced into a main exchanger 40b in which the oxygen-rich oxidant circulates. typically a gas consisting of at least 90% oxygen, preferably at least 95% vol. Inside the main exchanger 40a, 40b, the oxidant is preheated by heat exchange with a hot peddler gas 23 which comprises at least a part of the hot auxiliary air 22. This gives hot oxidant 43 and gas coolant coolant 45.
    [0017] The hot oxidant is supplied to at least one of the burners 200 of the combustion chamber 100, and preferably to all of the burners 200 of the chamber 100. In Fig. 1, a single heat exchanger 40b is shown. However, the installation may comprise several main exchangers 40a and 40b, and in particular several examples of the exchanger 40b which is connected to the (x) burner (s) 200. In this case, each main exchanger 40b preferably feeds a number limited burners 200 in hot oxidizer. For example, a main heat exchanger 40b may be associated with each of the burners 200 of the chamber 100 using oxygen-rich oxidant. According to the present invention, it is possible to increase the heat supplied to the main heat exchanger 40a and 40b by replacing hot auxiliary air as coolant 23 with a mixture of hot auxiliary air with hot exhaust gases. To this end, a portion 13 of the hot exhaust fumes is not introduced into the auxiliary exchanger 10 for heating the auxiliary gas. This portion 13 of the hot fumes is instead mixed with the hot auxiliary air 22 (or only with the part of the hot auxiliary air which is introduced into the main heat exchanger 40a and 40b for the preheating of the oxidant 42). In this way, it is possible to preheat the oxidant to a higher temperature and / or to preheat a larger flow of the oxidant. It is possible to preheat the oxidant in a single step by introducing cold oxidizer, for example at room temperature, into exchanger 40b and heating said oxidant to its final temperature in main exchanger 40b before supplying it. the burner (s) 200. In the example illustrated in Figure 1, however, the preheating of the oxidant is carried out in two steps. An oxygen-rich gas 41 is first introduced into an additional exchanger 40a of the main exchanger in which said rich gas 41 is heated by heat exchange with a portion 24 of the hot auxiliary air to a first temperature. Thus, a partially heated rich gas and a tempered auxiliary air stream 44 are obtained. The partially heated rich gas 42 is then introduced as the oxidant 42 into the main heat exchanger 40b.
    [0018] It is also possible to further increase the thermal energy of the rich oxidant 42 before it is introduced into the main exchanger 40b by mixing a limited amount of the hot auxiliary air with the partially heated rich gas, which mixture is then introduced. as a rich oxidant at 42 in the main heat exchanger 40b. The disadvantage of this option is a slight reduction in the oxygen content of the 42, 43 rich oxidant. This method and its advantages are described in more detail in the aforementioned coexisting patent application. Part of the hot auxiliary air is also used for preheating the fuel 3, for example natural gas, in a heat exchanger 30 called fuel exchanger. Preheated fuel 32 is thus obtained, which is then supplied to the burner (s) 200 of the combustion chamber 100, and a third tempered auxiliary air flow 33.
    权利要求:
    Claims (15)
    [0001]
    CLAIMS1) A method for the combustion, in a combustion chamber (100), of a fuel (32) with a preheated oxidant (43) rich in oxygen with generation of heat and hot fumes (11) within said combustion chamber (100), wherein: - the hot fumes (11) are removed from the combustion chamber (100), said exhaust fumes (11) containing residual heat; - Residual heat is recovered by heating an auxiliary gas (21) by heat exchange with at least a portion of the hot exhaust fumes (11) in an auxiliary heat exchanger (10), obtaining a hot auxiliary gas (22). ) and temperate fumes (12), at least a first portion of the hot auxiliary gas is introduced into a main heat exchanger (40b) in which oxygen-rich oxidant is preheated by heat exchange with a first heat-carrying gas (23) comprising said at least a first portion of the hot auxiliary gas, obtaining a preheated oxidant (43) and a tempered heat transfer gas (45); and the preheated oxidant rich in oxygen is supplied to the combustion chamber for the combustion of the fuel, characterized in that: a portion (13) of the exhausted hot fumes (11) is not introduced into the auxiliary exchanger ( 10) and is mixed with said at least a first portion of the hot auxiliary gas (22) prior to introduction into the main heat exchanger (40b) to increase the heat energy content of the heat transfer gas (23).
    [0002]
    2) A method according to claim 1, wherein the first heat transfer gas (23) consists of a mixture of hot auxiliary gas (22) and the portion (13) of the exhaust fumes (11).
    [0003]
    3) Process according to any of the preceding claims, wherein the auxiliary gas (21) is a predominantly inert gas.
    [0004]
    4) Process according to claim 3, wherein the auxiliary gas (21) is selected from air, steam, CO2, or a mixture of at least two of said gases, the auxiliary gas preferably being the air.
    [0005]
    5) Process according to any one of the preceding claims wherein the content of hot flue gases (11) discharged from the first heat-transfer gas (23) is less than or equal to 30% vol, and preferably less than or equal to 20% vol.
    [0006]
    6) Process according to any one of the preceding claims, wherein the volumetric ratio between, on the one hand, hot exhaust fumes and, on the other hand, the first hot auxiliary gas in the heat transfer gas is less than or equal to 45% flight and preferably less than or equal to 25% vol.
    [0007]
    7) A method according to any one of the preceding claims, wherein the combustion chamber (100) is a melting chamber, a refining chamber, a melting / refining chamber or a combustion chamber of a boiler.
    [0008]
    The method of claim 7, wherein the combustion chamber (100) is a glass melting chamber, a glass refining chamber or a glass melting / refining chamber.
    [0009]
    9) Process for the combustion, in a combustion chamber, of a fuel with a preheated oxidant (43) rich in oxygen with generation of heat and hot fumes (11) inside said combustion chamber, method in which: - the hot fumes are removed from the combustion chamber (100), said exhaust fumes (11) containing residual heat; - residual heat is recovered by heating an auxiliary gas (21) by heat exchange with at least a portion of the exhausted hot fumes (11) in an auxiliary heat exchanger (10), to obtain a hot auxiliary gas (22) and temperate fumes (12), at least a first portion of the hot auxiliary gas (22) is introduced into a main heat exchanger (40b) in which oxygen-rich oxidant (42) is preheated by heat exchange with a first heat-transfer gas (23) comprising said at least a first portion of the hot auxiliary gas (22); and - the oxygen-rich preheated oxidant (43) is supplied to the combustion chamber (100) for combustion of the fuel (32), characterized in that the method includes: - a first mode of operation in which the heat-transfer gas (23) does not include hot exhaust fumes (13), and - a second mode of operation corresponding to the method according to any one of the preceding claims.
    [0010]
    10) The method of claim 9, wherein in the first mode of operation, the coolant gas (13) consists of hot auxiliary gas (22).
    [0011]
    11) Installation comprising a combustion chamber (100), a first heat exchanger, said auxiliary exchanger (10), and a second heat exchanger, said main exchanger (40b), - the combustion chamber (100) being provided with injectors for injecting a fuel (22) and for injecting an oxidant (43) into the combustion chamber (100) and a flue gas outlet (300), - the auxiliary exchanger ( 10) comprising, on the one hand, a hot flue gas inlet (11) and a tempered flue outlet (12) and, on the other hand, an auxiliary gas inlet to be heated (21) and a hot auxiliary gas outlet (22), the hot flue outlet (300) of the combustion chamber (100) being fluidically connected to the hot flue gas inlet (11) of the auxiliary heat exchanger (10), - the main heat exchanger (40b) comprising, on the one hand, a hot heat-transfer gas inlet (23) and a tempered heat-transfer gas outlet (45) and, on the other hand, a combustion chamber inlet preheating (42) and a preheated oxidant outlet (43), the hot auxiliary gas outlet (22) of the auxiliary heat exchanger (10) being fluidly connected to the hot gas inlet (23) of the heat exchanger main outlet (40b), the preheated oxidant outlet being fluidly connected to at least one of the combustion chamber injectors (100), characterized in that the installation also comprises a pipe capable of fluidically connecting the hot flue outlet with the heat transfer gas inlet of the main heat exchanger (40b) in parallel with the auxiliary heat exchanger (10), so as to allow the flow of a controlled portion of the hot fumes (11) from the flue gas outlet (300) ) to the hot heat transfer gas inlet (23) of the main heat exchanger (40b).
    [0012]
    12) Installation according to claim 11, wherein the injectors for fuel injection (32) and oxidizer (43) are integrated in burners (200) and / or injection lances.
    [0013]
    13) Installation according to one of claims 11 and 12, wherein the combustion chamber (100) is a melting chamber, a refining chamber, a melting / refining chamber or the combustion chamber of a boiler, preferably a glass melting chamber, a glass refining chamber, a glass melting / refining chamber.
    [0014]
    14) Method of modifying an installation comprising a combustion chamber (100), a first heat exchanger (10), said auxiliary exchanger, and a second heat exchanger (40b), said main exchanger, - the combustion chamber (100) being provided with injectors for injecting a fuel (32) and for injecting an oxidant (43) into the combustion chamber (100) and a flue gas outlet (300), the auxiliary heat exchanger (10) comprising, on the one hand, a hot flue gas inlet (11) and a tempered flue outlet (12) and, on the other hand, an auxiliary gas inlet to be heated (21) and a hot auxiliary gas outlet (22), the hot flue outlet (300) of the combustion chamber (100) being fluidly connected to the hot flue gas inlet (11) of the auxiliary heat exchanger (10), - main heat exchanger (40b) comprising, on the one hand, a hot heat-transfer gas inlet (23) and a tempered heat-transfer gas outlet (45) and, on the other hand, an oxidizer inlet to be preheated (42) and a preheated oxidant outlet (43), the hot auxiliary gas outlet (22) of the auxiliary heat exchanger (10) being fluidly connected to the hot gas inlet ( 23) of the main exchanger, the preheated oxidant outlet being fluidly connected to at least one of the injectors of the combustion chamber (100), the method being characterized by adding to said installation a duct capable of fluidically connecting the hot flue gas outlet (300) with the heat transfer gas inlet (23) of the main heat exchanger (40b) in parallel with the auxiliary heat exchanger, so as to allow the flow of a controlled portion of the hot fumes ( 11) from the flue gas outlet (300) to the hot heat transfer gas inlet (23) of the main heat exchanger (40b).
    [0015]
    The process according to claim 14, wherein the combustion chamber (100) is a melting chamber, a refining chamber, a melting / refining chamber or a combustion chamber of a boiler, preferably a chamber. glass melting, a glass refining chamber, a glass melting / refining chamber. 15
    类似技术:
    公开号 | 公开日 | 专利标题
    EP3087040B1|2018-08-29|Combustion method and installation with optimized energy recuperation
    EP2736854B1|2019-11-20|Hybrid plant and method for melting glass
    EP2091872B1|2019-04-03|Combustion method for glass melting
    EP2731918B1|2019-09-18|Glass-melting equipment and process
    EP2462055B1|2016-08-03|Glass melting process
    EP2935132B1|2017-03-01|Energy recovery from fumes from a melting furnace with a gas turbine and heat exchangers
    EP3087041B1|2019-02-27|Combustion with improved heat recovery
    FR2918657A1|2009-01-16|FURNACE AND OXY-COMBUSTIBLE PROCESS FOR FUSION OF VITRIFIABLE MATERIALS
    BE1009707A6|1997-07-01|Gas turbine thermal energy system with a catalytic partial fuel oxidation
    EP2935133B1|2017-05-10|Energy recovery from fumes from a melting furnace using a gas turbine and heat exchangers
    EP3087319A1|2016-11-02|Integrated process for oxy-fuel combustion and production of oxygen
    EP2546204A1|2013-01-16|Method and installation for melting glass
    EP2281785A1|2011-02-09|Glass melting furnace
    FR2895490A1|2007-06-29|Fuel combustion method, involves injecting fuel jet and oxygen gas jets in combustion chamber, introducing primary gas jet through hole of specific diameter, where diameter and distance of emerging fuel jet ratio is at preset range
    FR3037131B1|2019-09-13|METHOD AND INTALLATION OF COMBUSTION
    EP2956416B1|2018-09-12|Installation with a furnace with an external heat recovery exchanger and combustion method using such an installation
    FR2969267A1|2012-06-22|DISCONTINUOUS LOAD FUSION PROCESS
    FR2937329A1|2010-04-23|METHOD AND DEVICE FOR CONTROLLING THE TEMPERATURE OF COMBUSTION FUMEES OF A THERMOLYSIS PROCESS
    同族专利:
    公开号 | 公开日
    US10208952B2|2019-02-19|
    JP2017501956A|2017-01-19|
    MX2016008292A|2016-09-09|
    JP6449300B2|2019-01-09|
    KR20160108343A|2016-09-19|
    WO2015097385A1|2015-07-02|
    US20160320057A1|2016-11-03|
    CN106061908B|2019-03-15|
    TR201815201T4|2018-11-21|
    EP3087040A1|2016-11-02|
    EP3087040B1|2018-08-29|
    ES2691969T3|2018-11-29|
    FR3015637B1|2016-01-22|
    CN106061908A|2016-10-26|
    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    EP1338848A2|2002-02-25|2003-08-27|L'Air Liquide S. A. à Directoire et Conseil de Surveillance pour l'Etude et l'Exploitation des Procédés Georges Claude|Method and apparatus for integrated air separation and heat recovery in a furnace|
    EP2546204A1|2011-07-15|2013-01-16|L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude|Method and installation for melting glass|FR3039535A1|2015-07-30|2017-02-03|Air Liquide|PROCESS AND INSTALLATION FOR MANUFACTURING FIBER GLASS RETICULATED PRODUCTS|
    US10781137B2|2015-07-31|2020-09-22|L'air Liquide Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude|Fiberglass material manufacture method comprising steps of sizing and desizing, and facility suitable for implementing said method|
    US11066319B2|2015-07-30|2021-07-20|L'air Liquide Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude|Method and facility for manufacturing a fiberglass material|FR1363459A|1962-05-11|1964-06-12|Basf Ag|Process and device for the polymerization of monoolefins|
    US6071116A|1997-04-15|2000-06-06|American Air Liquide, Inc.|Heat recovery apparatus and methods of use|
    ZA200304880B|2003-02-24|2004-05-04|Air Liquide|Integrated heat recovery systems and methods for increasing the efficiency of an oxygen-fired furnace.|
    FR2878318B1|2004-11-22|2007-03-30|Air Liquide|INDIRECT HEAT EXCHANGER|
    FR2890155B1|2005-08-25|2007-11-23|Air Liquide|PREHEATING FUEL AND OXYBRUSTER FUEL FROM COMBUSTION AIR PREHEATING|
    BRPI0520661A2|2005-10-28|2009-05-19|Air Liquide|low-oxide combustion process and apparatus|
    US20090293782A1|2008-05-30|2009-12-03|Foster Wheeler Energia Oy|Method of and system for generating power by oxyfuel combustion|
    US20100081103A1|2008-09-26|2010-04-01|Hisashi Kobayashi|Furnace with multiple heat recovery systems|
    US20110041740A1|2009-08-20|2011-02-24|Reilly Timothy J|Recuperative combustion system|
    EP2456204A1|2010-11-18|2012-05-23|Koninklijke Philips Electronics N.V.|Method and apparatus for encoding or generating an image|
    JP5724695B2|2011-07-07|2015-05-27|株式会社Ihi|Hot air fired boiler system|
    EP2551243A1|2011-07-26|2013-01-30|L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude|Hybrid facility and method for melting glass|
    EP2827058B1|2012-03-14|2017-07-26|IHI Corporation|Oxygen combustion boiler system|
    FR3015637B1|2013-12-23|2016-01-22|Air Liquide|COMBUSTION METHOD AND INSTALLATION WITH OPTIMIZED ENERGY RECOVERY|
    FR3015636B1|2013-12-23|2019-05-31|L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude|COMBUSTION WITH IMPROVED HEAT RECOVERY|FR3015637B1|2013-12-23|2016-01-22|Air Liquide|COMBUSTION METHOD AND INSTALLATION WITH OPTIMIZED ENERGY RECOVERY|
    FR3015635B1|2013-12-23|2019-05-31|L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude|INTEGRATED PROCESS FOR OXYCOMBUSTION AND OXYGEN PRODUCTION|
    CN106509966A|2016-11-29|2017-03-22|黄俊柳|Flue-cured tobacco stove utilizing water vapor combustion and secondary combustion|
    法律状态:
    2015-12-21| PLFP| Fee payment|Year of fee payment: 3 |
    2016-12-22| PLFP| Fee payment|Year of fee payment: 4 |
    2017-12-21| PLFP| Fee payment|Year of fee payment: 5 |
    2019-12-19| PLFP| Fee payment|Year of fee payment: 7 |
    2020-12-23| PLFP| Fee payment|Year of fee payment: 8 |
    2021-12-24| PLFP| Fee payment|Year of fee payment: 9 |
    优先权:
    申请号 | 申请日 | 专利标题
    FR1363477A|FR3015637B1|2013-12-23|2013-12-23|COMBUSTION METHOD AND INSTALLATION WITH OPTIMIZED ENERGY RECOVERY|FR1363477A| FR3015637B1|2013-12-23|2013-12-23|COMBUSTION METHOD AND INSTALLATION WITH OPTIMIZED ENERGY RECOVERY|
    KR1020167018980A| KR20160108343A|2013-12-23|2014-12-19|Combustion method and installation with optimized energy recuperation|
    EP14835480.6A| EP3087040B1|2013-12-23|2014-12-19|Combustion method and installation with optimized energy recuperation|
    JP2016541388A| JP6449300B2|2013-12-23|2014-12-19|Combustion method and equipment with optimized energy recovery|
    TR2018/15201T| TR201815201T4|2013-12-23|2014-12-19|Combustion method and mechanism with optimized energy recovery.|
    MX2016008292A| MX2016008292A|2013-12-23|2014-12-19|Combustion method and installation with optimized energy recuperation.|
    CN201480074699.4A| CN106061908B|2013-12-23|2014-12-19|The combustion method and facility of energy regenerating with optimization|
    PCT/FR2014/053472| WO2015097385A1|2013-12-23|2014-12-19|Combustion method and installation with optimized energy recuperation|
    US15/107,538| US10208952B2|2013-12-23|2014-12-19|Combustion method and installation with optimized energy recuperation|
    ES14835480.6T| ES2691969T3|2013-12-23|2014-12-19|Procedure and installation of combustion with optimized energy recovery|
    [返回顶部]