• 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 for the combustion of a fuel (32) with a preheated oxidant (43) rich in oxygen, in which an oxygen-rich oxidant (41) is heated in a first heat exchanger (40a) by means of a first part from the residual heat of the generated fumes (11), the heated oxidant is mixed with a predominantly inert gas to obtain the oxygen-rich oxidant (42) and the oxygen-rich oxidant is preheated in a second heat exchanger (40b ) by means of a second part of the residual heat of the fumes (11).
    公开号:FR3015636A1
    申请号:FR1363459
    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 with a preheated oxygen rich gas as oxidant. 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 efficiency of combustion, to maximize the exploitation of the thermal energy generated and to reduce pollutant emissions, such as If the energy and environmental interest of burning with oxygen is well known and recognized, the cost of oxygen in relation to air continues to limit the use of oxygen as a oxidant in an industrial context.
    [0002] 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. In particular, it is known to preheat oxygen in a heat exchanger. In particular, it is known to preheat oxygen with residual heat present in the combustion gases (fumes) at the outlet of the combustion chamber, and this by means of a first heat exchange between the hot fumes and a heat transfer fluid, followed by a second heat exchange between the heat transfer fluid (from the first heat exchange) and oxygen. Such methods are described in particular in EP-A-0872690 and in WO2006 / 054015.
    [0003] The use of heat exchangers for oxygen preheating, however, raises delicate problems of resistance of the materials in contact with the hot oxygen. Indeed, as described in WO2008 / 141939, the materials of the exchanger in contact with the hot oxygen must have a very good resistance to oxidation by this gas and must not be weakened during startup or stop of the exchanger.
    [0004] The most common steels do not meet these requirements and therefore do not allow sufficient safety of the exchanger.
    [0005] The following selection criterion was proposed in WO2008 / 141939 for the selection of materials of the heat exchanger in contact with hot oxygen: a metal alloy of which a sample placed in an oxygen-rich gas atmosphere to circulate in the atmosphere. exchanger and at the highest temperature encountered in the exchanger, does not exhibit a weight gain of more than 0.1 mg / cm 2 of exposed surface after 1000 cycles each comprising maintaining at this highest temperature for one hour each plateau at this temperature being followed by a return to ambient temperature. The aforementioned resistance requirements obviously also apply to any metallic part of the installation that is in contact with the hot oxygen, such as the pipes for transporting the hot oxygen to the burners / lances of the combustion chamber. . In W02008 / 141939, several of these alloys are mentioned, for example / Inconel 600 H, Inconel 600 L and Inconel 800 H, among others. Unfortunately, such alloys and the corresponding assembly processes have a high cost, which, for a large number of industrial installations, is a major obstacle to the implementation of such a technology and to thus benefit from the advantages, including environmental, combustion with preheated oxygen. The present invention aims to remedy at least partially this disadvantage and to allow a more widespread use of combustion with preheated oxygen.
    [0006] The present invention is intended in particular to enable the production of processes and installations for the combustion of a fuel with as oxidant a preheated oxygen rich gas which are robust and reliable while limiting the costs for the production of equipment used for preheating said oxidant. The present invention thus relates to a method for the combustion, in a combustion chamber, of a fuel with a preheated oxygen-rich oxidant. Said combustion generates heat and smoke in said combustion chamber. The fumes generated are removed from the combustion chamber. The temperature of the exhaust fumes being significantly higher than the ambient temperature, typically between 1200 ° C and 1600 ° C, these fumes evacuated contain a significant amount of residual heat.
    [0007] The oxidant is preheated by means of said residual heat in at least one heat exchanger and the preheated oxidant is supplied to the combustion chamber for combustion of the fuel. According to the invention, an oxidant rich in oxygen is heated in a first heat exchanger, more particularly having an oxygen content of from 80% vol to 100% vol, and preferably from 90% vol to 100% vol. by heat exchange with a first coolant containing at least a first part of the residual heat of the exhaust fumes, said oxidant thus being heated from an initial temperature TOi at the inlet of the first exchanger to a final temperature TOf at the outlet of the first exchanger, with TOf> TOi. The heated oxidant from the first heat exchanger is then mixed with a predominantly inert gas, so as to obtain an oxygen-rich oxidant having more particularly an oxygen content of 70% vol to 90% vol, and preferably 75% by weight. % vol 85% vol, with 02 <01. In a second heat exchanger, said oxygen-rich oxidant is preheated by heat exchange with a second heat-transfer fluid containing at least a second part of the residual heat of the evacuated fumes. The oxidant is thus brought from an initial temperature TCi to the inlet of the second heat exchanger to a final temperature TCf at the outlet of the second heat exchanger, with TCf> TCi. At least a portion, and preferably all, of the preheated oxygen rich oxidant from the second heat exchanger is supplied to the combustion chamber as an oxidant for combustion of the fuel. The final temperature TOf of the oxidant at the outlet of the first heat exchanger is advantageously from 200 ° C. to 400 ° C., preferably from 250 ° C. to 400 ° C., and still more preferably from 300 ° C. to 400 ° C. . The final temperature TCf of the oxidant at the outlet of the second heat exchanger is advantageously from 400 ° C. to 850 ° C., preferably from 400 ° C. to 700 ° C., and even more preferably from 500 ° C. to 650 ° C. The invention makes it possible to optimize the preheating of an oxidant rich in oxygen. Indeed, although heated in the first heat exchanger an oxidant particularly rich in oxygen, it is not necessary to use particularly noble and therefore expensive materials (see above) for the elements of the installation which come into contact with the hot oxidant because the temperature of the hot oxidant remains well below the temperature at which the preheated oxidant is supplied to the combustion chamber.
    [0008] On the other hand, although in the second exchanger, the oxidizer is preheated to particularly high temperatures (at least the temperature at which the oxidant is introduced into the combustion chamber), it is not necessary to use particularly noble and therefore expensive materials for the elements of the installation that come into contact with the preheated oxidant, because the oxygen content of the oxidant is lower than the oxygen content of so-called "industrial oxygen" And more particularly not more than 90% vol. Said advantages related to the recovery and exploitation of the residual heat of the fumes discharged for the preheating of the oxidizer more than compensate for the effect of the reduction of the oxygen content of the oxidant (relative to the oxygen content of the oxidant) on the efficiency of combustion. In the present context, the following are understood to mean: a gas "rich in oxygen" or "rich": a gas having a higher oxygen content 70% 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) under the conditions existing in the combustion chamber . A predominantly inert gas therefore necessarily contains less than 50% oxygen; "Heat exchanger": an installation or a heating device in which the heat transfer fluid, which provides heat, and the fluid to be heated circulate in separate enclosures, the heat transfer fluid transmitting heat to the fluid to be heated to through one or more 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 oxidant 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 injecting fuel and oxidant into a combustion zone; - "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. The predominantly inert gas which is mixed with the oxidant heated to obtain the oxidant may be selected from air, steam, CO2, smoke discharged from the combustion chamber or a mixture of minus two of said gases. When it is important to limit the formation of NOx to a minimum, steam, CO2, smoke discharged from the combustion chamber or a mixture of at least two of said gases is preferably used.
    [0009] According to a particular embodiment, a main stream of coolant containing residual heat of the evacuated fumes is provided and said main stream is divided into at least two portions. A first portion constitutes the first heat transfer fluid used in the first heat exchanger and a second portion is used as the second heat transfer fluid in the second heat exchanger. In this case, a third portion of the main coolant flow may advantageously be used for preheating the fuel upstream of the combustion chamber by heat exchange between the third portion and the fuel in an additional heat exchanger. According to an alternative embodiment, at least a first portion of the main heat transfer fluid stream is used as the second heat transfer fluid and said at least a part of the main stream is used as the first heat transfer fluid after passing through the second heat exchanger. It is then advantageous to use at least a second portion of the main stream of coolant for preheating the fuel upstream of the combustion chamber by heat exchange between the third portion and the fuel in an additional heat exchanger. It is possible to use at least a portion of the fumes discharged as first and / or second heat transfer fluids. According to another embodiment, residual heat is recovered from the evacuated fumes by heating an auxiliary fluid by heat exchange with the fumes discharged into an auxiliary heat exchanger.
    [0010] At least a portion of said auxiliary fluid heated in the auxiliary heat exchanger is then used as first and / or second heat transfer fluid, preferably as first and second heat transfer fluids. In this case, the auxiliary fluid is preferably a predominantly inert fluid, preferably selected from air, steam, CO2 and mixtures of at least two of said gases, more preferably air. The temperature of the auxiliary fluid at the outlet of the auxiliary exchanger is conveniently from 600 ° C to 900 ° C, preferably from 650 ° C to 800 ° C, and more preferably from 650 ° C to 700 ° C. It is then possible, particularly advantageously, to obtain the oxygen-rich oxidant 10 by mixing the heated oxidant with a portion of: (i) heated auxiliary fluid from the auxiliary heat exchanger, (ii) fluid auxiliary from the first heat exchanger after its use as a first heat transfer fluid, or (iii) auxiliary fluid from the second heat exchanger after use as a second heat transfer fluid. In this way, the recovery of the residual heat of the evacuated fumes is optimized. It should be noted that the various heat exchangers, and in particular the first and second heat exchangers, may be in the form of separate apparatus, each having its own outer shell. However, said heat exchangers can also be integrated in the same device, that is to say be surrounded by the same outer envelope. The combustion chamber may be a melting chamber, a refining chamber, a melting-refining chamber or a melt distributor (preferably a feeder), preferably a glass or metal melting chamber. , a glass or metal refining chamber, a melting-refining chamber of glass or metal or a distributor of molten glass or molten metal. The combustion process is then part of a melting process, a refining process, a melting-refining process, a melt distribution process, especially for melting / refining / distribution. glass or metal.
    [0011] The present invention and its advantages are further illustrated in the following description of examples of the present invention, with reference being made to Figures 1 to 4 which are schematic representations of facilities for implementing different forms of performing the method according to the invention.
    [0012] In the various figures, the same reference numerals designate elements corresponding to the different embodiments. I. Examples 1 and 2: recovery of the residual heat by means of an intermediate fluid and use of the heated intermediate fluid as the first and second heat transfer fluid and substantially inert dilution gas. I.1: Example 1 (Figure 1): As illustrated in Figure 1, heat is generated inside the combustion chamber 1 by combustion, for example, to heat and / or melt a charge in the chamber (such as steam, metals, vitrifiable material, etc.). The fumes generated 11 are discharged from the chamber 1 by means of a flue gas outlet. The evacuated fumes 11 contain residual heat. According to the invention, this residual heat is recovered, in particular for the preheating of the oxidant and preferably of the oxidant and the fuel, upstream of the combustion chamber 1. For this purpose, the evacuated fumes 11 (or at least a part thereof) said fumes) are introduced into an auxiliary heat exchanger 10. In this auxiliary heat exchanger 10, an auxiliary fluid 21 is heated by heat exchange with the exhaust fumes. In the case illustrated, the auxiliary fluid to be heated 21 is ambient air. At the outlet of the auxiliary exchanger 10, the cooled fumes 12 are fed to a chimney, where appropriate after a cleaning treatment (not shown) to remove dust or other pollutants. The heated auxiliary fluid 22 has a temperature of the order of 700 ° C. and constitutes a main stream of coolant. Said main flow 22 is divided into several portions (23, 24, 25). A first portion 24 of heat transfer fluid is introduced into a first heat exchanger 40a for heating an oxidant 41 with a high oxygen content.
    [0013] In the illustrated case, the oxidant 41 has an oxygen content of approximately 100% vol, typically of the order of 99% vol. The oxidant source (not shown) may for example be an oxidant pipeline, an oxidant tank, or an installation for the production of a high oxygen gas, such as a gas separation unit. air. The cool heat transfer fluid 44 of this first portion 24 is recovered at the outlet of the first exchanger 40a. The heated oxidant exits the first exchanger 40a at a temperature of about 400 ° C. It is mixed with heat transfer fluid (auxiliary fluid) heated 26 in proportion to 12 parts (vol) of heat transfer fluid 26 over 100 parts (vol) of heated oxidant. Thus, an oxygen-rich oxidant 42 with an oxygen content of 91.5 vol% and a temperature of the order of 402 ° C., which is introduced into a second exchanger 40b (see Table 1). 02 100 N / h 4% 300 N / h 237 N / h N2 63 Nm3 / h 02 Air 102.52 N / h 02 9.48 Nm3 / h N2 112 Total 91.5%% purity 288 Ne / h Air Table 1 In the illustrated installation in FIG. 1, the heated oxidant and heat transfer fluid mixture is produced at the outlet of the heated oxidizer of the first heat exchanger 40a, by means of a pipe connecting, on the one hand, the line bringing the first portion 24 coolant fluid to the first heat exchanger 40a, on the other hand, the line connecting the heated oxidant outlet of the first heat exchanger 40a to the rich oxidizer inlet of the second heat exchanger 40b.
    [0014] A valve mounted on the first line regulates the flow of heat transfer fluid and directed to the second line via the pipe connecting them. In the second exchanger 40b, the oxygen-rich oxidant 42 thus obtained is in turn heated by heat exchange with a second portion 23 of the heat-transfer fluid heated to a preheating temperature of 650 ° C. The heat transfer fluid 45 of this second portion is removed from the second heat exchanger 40b and the preheated oxygen rich oxidant 43 is supplied to one or more burners 2 of the combustion chamber 1 for the combustion of fuel in said chamber 1, with generation of heat and smoke. Since the temperature of the oxidant 41 in the first exchanger 40a remains relatively low, it is possible to produce this first exchanger 40a without having to resort to particularly expensive materials known for their particularly high resistance to approximately pure oxygen. at high temperature, while ensuring a high durability and reliability of said first exchanger 40a. Since the oxygen content of the oxygen-rich oxidant 42 is lower than the oxygen content of the oxidant 41, it is possible, similarly, despite the high temperature of the oxidant 42, 43 in the second heat exchanger 40b, realize this second exchanger 40b without having to use such expensive materials, while ensuring a high durability and reliability of the second exchanger 40b. According to the illustrated embodiment, a third portion 25 of the heated coolant 22 is used in an additional heat exchanger 30 for preheating the fuel 31. For a gaseous fuel such as natural gas, the fuel is typically heated. up to a preheating temperature of 400 ° C to 600 ° C.
    [0015] The heat transfer fluid 33 of this third portion 25 is removed from the additional exchanger 30 and the preheated fuel 32 from the additional exchanger 30 is supplied to the (x) burner (s) 2 to be burned in the chamber 1 with the Preheated oxidant 43. 1.2: Example 2 (Figure 2): The embodiment illustrated in Figure 2 differs from that illustrated in Figure 1 mainly in that a single portion 23 of heated coolant 22 is used for respectively the heating the oxidant 41 and preheating the oxidant 42. Said portion 23 of the heated coolant 22 is first used for preheating the oxygen-rich oxidant 42 in the second heat exchanger 40b and the partially tempered heat transfer fluid 45 of this portion is removed from the second exchanger 40b and introduced into the first exchanger 40a for heating the oxidant 41.
    [0016] The oxygen-rich oxidant 42, which is introduced into the second exchanger 40b, is obtained by mixing heated oxidant from the first exchanger 40a with a portion 27 of the coolant (auxiliary (cool) fluid) 44 obtained from said first exchanger 40a in proportion to 12 parts (vol) of coolant on 100 parts (vol) of heated oxidant.
    [0017] The mixture of heated oxidant and heated heat transfer fluid is produced at the outlet of the heated oxidizer of the first heat exchanger 40a, by means of a pipe connecting, on the one hand, the tempered coolant outlet 44 of the first heat exchanger 40a. on the other hand, the line connecting the heated oxidant outlet of the first exchanger 40a to the rich oxidant inlet of the second exchanger 40b. The flow of cool heat transfer fluid directed to the second line is again adjusted by a valve 27 '. After being used as heat transfer fluid in the various exchangers 40a, 40b, 30, the auxiliary fluid or the auxiliary fluid portions 44, 45, 33 can (i) recirculate, (ii) be sent to the atmosphere (if the nature of the auxiliary fluid permits) or (iii) be used for other purposes on the site.
    [0018] II Examples 3 and 4: use of fumes discharged from the combustion chamber as first and second heat transfer fluid. II.1: Example 3 (Figure 3): The embodiment of Figure 3 differs from that of Figure 1 mainly in that at least a portion of the fumes 11 discharged from the chamber 1 directly as heat transfer fluid 22. Residual heat is therefore transferred directly from the fumes discharged 22 respectively to the oxidant 41 in the first heat exchanger 40a, to the oxidant 42 in the second heat exchanger 40b and to the fuel 31 in the heat exchanger. additional heat 30 (without intermediate transfer to an auxiliary fluid used as heat transfer fluid in an auxiliary exchanger 10). The costs of the installation and the losses of thermal energy are thus reduced. However, the prolonged use of this option of the process according to the invention is generally limited to heating processes producing relatively clean fumes, that is to say fumes with a low content of dust and condensable materials.
    [0019] The oxygen-rich oxidant 42 is obtained by mixing the heated oxidant from the first heat exchanger 40a with a predominantly inert gas 28 such as ambient air, steam, N2 or CO2. 11.2: Example 4 (FIG. 4): The embodiment of FIG. 4 differs in a similar manner from that of FIG. 2 in that at least a portion of the fumes 11 discharged from the chamber are used as hot heat transfer fluid. 1. The oxygen-rich oxidant 42 is obtained by mixing the heated oxidant from the first heat exchanger 40a with a predominantly inert gas 28 such as ambient air, steam, N2 or CO2. After serving as heat transfer fluid, the temperate fumes 44 ', 45', 33 'are sent to the chimney, as well as the portion 12' of exhaust fumes that have not been used as heat transfer fluid.
    权利要求:
    Claims (11)
    [0001]
    CLAIMS1) A method for the combustion, in a combustion chamber (1), of a fuel (32) with a preheated oxidant (43) rich in oxygen with generation of heat and smoke (11) in said combustion chamber (1) ), in which process: - the fumes (11) are discharged from the combustion chamber (1), said exhaust fumes (11) containing residual heat; the oxidant (42) is preheated by means of said residual heat in at least one heat exchanger (40a, 40b); and - the preheated oxidant (43) is supplied to the combustion chamber (1) for the combustion of the fuel, characterized in that: - in a first heat exchanger (40a) is heated, by heat exchange with a first fluid coolant (24, 45) containing at least a first part of the residual heat of the fumes discharged, an oxidant (41) having an oxygen content of from 80% vol to 100% vol, and preferably from 90% to 100% vol flight, from an initial temperature TOi at the inlet of the first exchanger (40a) to a final temperature TOf at the outlet of the first exchanger (40a), with TOf> T0i,; the heated oxidant from the first heat exchanger (40a) is mixed with a predominantly inert gas, so as to obtain an oxygen-rich oxidant (42) having an oxygen content of 70% vol to 90% vol, and preferably from 75% vol to 85% vol, with 02 <01; - In a second heat exchanger (40b) is preheated, by heat exchange with a second heat transfer fluid (23, 46) containing at least a second part of the residual heat of the evacuated fumes, oxygen-rich oxidant (42) d an initial temperature TCi at the inlet of the second heat exchanger (40b) to a final temperature TCf at the outlet of the second heat exchanger (40b), with TCf> TCi; and providing at least a portion of the preheated oxygen rich oxidant (43) from the second heat exchanger (40b) to the combustion chamber (1) for fuel combustion.
    [0002]
    2) Process according to claim 1, wherein the final temperature TOf of the oxidant at the outlet of the first heat exchanger (40a) is 200 ° C to 400 ° C, preferably 250C to 400C, and still preferably from 300 ° C to 400 ° C.
    [0003]
    3) Process according to one of claims 1 and 2, wherein the final temperature TCf 10 of the oxidant at the outlet of the second heat exchanger (40b) is 400 ° C to 850 ° C, preferably 400 ° C to 700 ° C, and more preferably from 500 ° C to 650 ° C.
    [0004]
    4) Process according to any one of the preceding claims, wherein the predominantly inert gas (28) is selected from air, steam, CO2, smoke discharged from the combustion chamber or a mixture at least two of said gases.
    [0005]
    5) Process according to any one of the preceding claims, wherein a main stream of coolant containing residual heat of the evacuated fumes (11) is provided and said main stream (22) is divided into at least two portions: a first portion (24) constituting the first heat transfer fluid, and - a second portion (23) constituting the second heat transfer fluid, and - preferably also a third portion (25), said third portion (25) being used for the preheating of the fuel (31) upstream of the combustion chamber (1) by heat exchange between the third portion (25) and the fuel (31) in an additional heat exchanger (30).
    [0006]
    6) Process according to any one of claims 1 to 4, wherein: - a main stream of heat transfer fluid (22) containing residual heat evacuated fumes (11) is provided, - at least a first part is used; (23) of said main stream (22) as a second heat transfer fluid, - said at least a first heat transfer fluid is used at least a portion of the main flow (46) after passing through the second heat exchanger (40b), and - it is used preferably at least a second portion (25) of the main flow (22) of the coolant for preheating the fuel (31) upstream of the combustion chamber (1) by heat exchange between the second portion (25) and the fuel (31) in an additional heat exchanger (30).
    [0007]
    7) Process according to any one of the preceding claims, wherein the evacuated smoke (11) of the combustion chamber (1) is used as first and / or second heat transfer fluid, preferably as first and second heat transfer fluids.
    [0008]
    8) Process according to any one of claims 1 to 6, wherein: - the waste heat is recovered from the evacuated fumes (11) by heating an auxiliary fluid (21) by heat exchange with the evacuated fumes (11) in a auxiliary heat exchanger (10), and - auxiliary fluid heated in the auxiliary heat exchanger (10) is used as first and / or second heat transfer fluids (23, 24, 46), preferably as first and second heat transfer fluid .
    [0009]
    9) The method of claim 8, wherein the auxiliary fluid (21) is a predominantly inert fluid, preferably selected from air, steam, CO2 and mixtures of at least two of said gases, further preference of air.
    [0010]
    The process according to claim 9, wherein the oxygen-rich oxidant is obtained by mixing the heated oxidant with a portion of: (i) heated auxiliary fluid from the auxiliary heat exchanger (10), (ii) auxiliary fluid from the first heat exchanger (40a) after its use as a first heat transfer fluid or (iii) auxiliary fluid from the second heat exchanger (40b) after its use as a second heat transfer fluid.
    [0011]
    Process according to any of the preceding claims, wherein the combustion chamber (1) is a melting chamber, a refining chamber, a melting-refining chamber or a melt distributor, preferably a chamber. melting glass or metal, a glass or metal refining chamber, a glass or metal melting-refining chamber or a molten glass or molten metal dispenser.
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    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    EP0137059A1|1983-10-07|1985-04-17|Sorg GmbH &amp; Co. KG|Method of melting glass using glass batch preheating, and glass melting furnace used therefor|
    US6126440A|1996-05-09|2000-10-03|Frazier-Simplex, Inc.|Synthetic air assembly for oxy-fuel fired furnaces|WO2017017382A1|2015-07-30|2017-02-02|L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude|Method and facility for manufacturing a fiberglass material|
    FR3039536A1|2015-07-31|2017-02-03|Air Liquide|PROCESS FOR MANUFACTURING FIBER GLASS PRODUCTS COMPRISING STACKING AND DESENSING STAGES AND APPARATUS ADAPTED FOR ITS IMPLEMENTATION|
    FR3039535A1|2015-07-30|2017-02-03|Air Liquide|PROCESS AND INSTALLATION FOR MANUFACTURING FIBER GLASS RETICULATED PRODUCTS|
    US10208952B2|2013-12-23|2019-02-19|L'air Liquide Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude|Combustion method and installation with optimized energy recuperation|BE794409A|1972-01-24|1973-07-23|Morgan Construction Co|APPLIANCE FOR TREATING OXIDIZING AIR AND BURNT GAS FROM A REGENERATION OVEN|
    US5807418A|1996-05-21|1998-09-15|Praxair Technology, Inc.|Energy recovery in oxygen-fired glass melting furnaces|
    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|
    BRPI0520661A2|2005-10-28|2009-05-19|Air Liquide|low-oxide combustion process and apparatus|
    EP1995543A1|2007-05-10|2008-11-26|AGC Flat Glass Europe SA|Heat exchanger for oxygen|
    KR20140066699A|2011-07-15|2014-06-02|레르 리키드 쏘시에떼 아노님 뿌르 레？드에렉스뿔라따시옹 데 프로세데 조르즈 클로드|Glass-melting equipment and process|
    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|
    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 |
    2018-12-19| PLFP| Fee payment|Year of fee payment: 6 |
    2020-10-16| ST| Notification of lapse|Effective date: 20200905 |
    优先权:
    申请号 | 申请日 | 专利标题
    FR1363459|2013-12-23|
    FR1363459A|FR3015636B1|2013-12-23|2013-12-23|COMBUSTION WITH IMPROVED HEAT RECOVERY|FR1363459A| FR3015636B1|2013-12-23|2013-12-23|COMBUSTION WITH IMPROVED HEAT RECOVERY|
    ES14835481T| ES2717976T3|2013-12-23|2014-12-19|Combustion with improved heat recovery|
    TR2019/04502T| TR201904502T4|2013-12-23|2014-12-19|Combustion with improved heat recovery.|
    PCT/FR2014/053474| WO2015097386A1|2013-12-23|2014-12-19|Combustion with improved heat recovery|
    CN201480074700.3A| CN106061909B|2013-12-23|2014-12-19|Burning with improved recuperation of heat|
    EP14835481.4A| EP3087041B1|2013-12-23|2014-12-19|Combustion with improved heat recovery|
    JP2016541502A| JP6585055B2|2013-12-23|2014-12-19|Combustion with improved heat recovery|
    PL14835481T| PL3087041T3|2013-12-23|2014-12-19|Combustion with improved heat recovery|
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