• 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:
    An oxy-fuel combustion process in which an air stream (21) is heated by means of at least a part of the residual heat present in the flue gases (11) of the combustion chamber (100), at least a part of said flow of hot air (22) is introduced into an oxygen production unit (20) in which a portion of the oxygen present in the hot air stream (22) is extracted by means of one or more MTI, with obtaining a first oxygen flux (50) at a high temperature, said first oxygen flux (50) is mixed with a second oxygen stream (60) so as to obtain a global flow of oxygen (70) at a lower temperature than that of the first oxygen stream (50), at least a portion of the overall oxygen stream (70) being transported to the combustion chamber (100) and used therein as a high-temperature oxidant oxygen.
    公开号:FR3015635A1
    申请号:FR1363503
    申请日:2013-12-23
    公开日:2015-06-26
    发明作者:Luc Jarry；Nicolas Spiegl
    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 an oxycombustion process incorporating the production or generation of oxygen. It is known to extract oxygen from a gas such as air by means of ion transport membranes (ITMs), also known as "solid electrolytes" (in English "Ion Transport Membranes" or IMT). The MTIs are capable of ionizing the oxygen molecules present in the air that comes into contact with a first face of the MTI, selectively transporting the oxygen ions through the MTI and reconstituting oxygen molecules at the same time. from said oxygen ions on the face of the membrane opposite the first face (in the direction of movement of the oxygen ions). It is also known to use oxygen thus produced as an oxidant for the combustion of a fuel and the production of heat. From WO-A-2011/015616, there is known a method of operating a glass melting furnace in which the burners are fed, on the one hand with fuel and, on the other hand, with hot oxygen directly derived from an oxygen extractor at MTI. According to WO-A2011 / 015616, if the oxygen supply of the extractor is not sufficient, an additional supply of oxygen is made directly at the burner. The fumes leaving the melting furnace are passed through a first heat exchanger, called primary exchanger, for heating a heat transfer fluid, especially air. The thus heated air feeds a series of secondary heat exchangers in which circulates compressed air, typically at a pressure of the order of 1.5 to 2.106 Pa. After passing through the secondary exchangers, the compressed air has a temperature of 500 ° C to 550 ° C. This hot compressed air can be further heated in a boiler to reach higher temperatures, for example of the order of 900 ° C. The hot compressed air thus obtained passes over the MTI extractor for the production of oxygen and the oxygen thus extracted from the compressed hot air is directed directly onto a burner. The oxygen-depleted air can be used to activate a turbine for the production of the compressed air introduced into the MTI extractor. As indicated in WO-A-2011/015616, the properties of hot oxygen, as it leaves the extractor at MTI, imposes practical limits on the devices in which the hot oxygen circulates. It is therefore particularly advisable to use the oxygen immediately after its extraction and thus to locate the extractor at MTI near the furnace burners in order to limit the path followed by the oxygen to the burner to limit the risks of degradation. devices in contact with this oxygen. The need, for safety reasons, to locate each extractor near the associated burner greatly limits the interest of the method described in WO-A-2011/015616. Indeed, the immediate vicinity of a glass melting furnace is generally very congested, particularly at the level of the burners, in particular with the oxidizer supply devices and the fuel supply devices of the burners and, if appropriate, devices for preheating the oxidant and / or fuel upstream of the burners. Despite this congestion, it remains necessary to provide easy access to said burners to allow their maintenance and repair. In addition, melting furnaces often have a large number of burners. The realization of oxygen extractors with MTI of small dimensions, unitary for each burner increases the cost considerably the cost of the installations.
    [0002] Consequently, the current design of the furnaces does not generally allow the implantation of oxygen extractors at MTI immediately upstream of the burners as proposed in WO-A-2011/015616, whereas, as also explained in WO-A- 2011/015616, an implementation of the extractor MTI greater distance from the burner poses a safety problem generally unacceptable for the operator of the furnace related to the transport of oxygen at high temperature. The present invention aims to at least partially overcome the problems described above. The present invention more particularly proposes an oxy-fuel combustion process in which a fuel is burned with an oxygen-rich oxidant in a combustion chamber with generation of heat and smoke in the combustion chamber. The fumes generated are removed from the combustion chamber, said exhaust fumes containing residual heat. According to the invention, a flow of air is heated by means of at least a part of the residual heat present in the evacuated fumes. This produces a hot air flow 30 having a temperature TA1. The temperature TA1 is chosen so as to allow extraction of oxygen from the hot air by MTI. At least a part of the hot air flow is introduced into an oxygen production unit in which a portion of the oxygen present in the at least part of the hot air flow is extracted by means of one or more MTI. In this way, a first flow of oxygen at a temperature TO1 and a stream of oxygen-depleted air having a temperature TA2 are obtained with TA2 <TA1. Downstream of this oxygen production unit, the first oxygen stream is mixed with a second oxygen stream so as to obtain an overall flow of oxygen at a temperature T0 2, with TO 2 <T01. The lower temperature TO2 is generally obtained because the temperature of the second oxygen flow is lower than the temperature TO1 of the first oxygen flow. At least a portion of the overall flow of oxygen is then transported to the combustion chamber and used as oxygen-rich oxidant in the combustion chamber.
    [0003] According to the invention, the said at least part of the overall flow of oxygen is heated directly upstream of the combustion chamber at a temperature TOf, with TOf> T02. By "residual heat, one understands the heat which is evacuated from a combustion chamber with the fumes generated by combustion in the chamber. By oxidant or gas "rich in oxygen" or simply "rich", it includes an oxidizer or gas having an oxygen content greater than 60% vol. According to the invention, the residual heat of the evacuated fumes is thus used in order to heat a flow of air up to a temperature TA1 allowing an extraction of oxygen by MTI at an industrial level. Downstream of the production unit, the first oxygen flow has a high temperature such that the transport of this first oxygen flow would pose a safety problem. By mixing, according to the invention, the first stream with a second stream of oxygen, it is possible to produce an overall flow of oxygen having a lower temperature TO2, which allows the safe transport of the overall flow, without however that the heat energy present in the first oxygen flow at the output of the production unit is lost.
    [0004] Providing a second flow of oxygen from a source other than the production unit also avoids problems due to the limited production capacity of most oxygen-based oxygen production units. MTI. The heating of the air flow by means of residual heat present in the evacuated fumes can be carried out in a recuperator or heat exchanger.
    [0005] According to an advantageous embodiment of the invention, the flow of hot air, at least part or all of which is introduced into the oxygen production unit, has a temperature TA1 of 700 ° C. 1000 ° C, preferably from 750 ° C to 950 ° C and more preferably from 800 ° C to 900 ° C, These temperatures facilitate the extraction of oxygen by MTI.
    [0006] The at least part of the hot air flow preferably has a pressure PA1 of 1 bar ab to 6 bar ab at the inlet of the oxygen production unit, preferably 1 bar ab to 3 bar ab and still more preferably 1 bar ab to 2 bar ab The portion of oxygen extracted from the at least a portion of the hot air flow may correspond to between 10% and 100%, preferably between 20% and 70%, still from preferably between 20% and 50% of the oxygen present in said at least a portion of the hot air flow. Although the most complete extraction of oxygen is desired, partial extraction is often more profitable and therefore preferable in an industrial context. The first flow of oxygen from the production unit may correspond to between 90% and 0% vol, preferably between 90% and 15% vol, still preferably between 80% and 20% vol, or even between 80% and 30% vol, and still preferably between 80% and 50% vol of the overall flow of oxygen. According to the invention, the use of a global stream containing no oxygen from the production unit and therefore consisting entirely of oxygen from another source is exceptional and limited in time (and not during the total duration of the process). However, such an overall flow consisting entirely allows continuous operation of the combustion chamber despite a stop or failure of the oxygen production unit. The second oxygen stream is provided by an air gas separation unit, such as a PSA (i.e., an installation known as "Pressure Swing Adsorption") or a VPSA ( that is to say an installation known under the name "Vacuum Pressure Swing Adsorption", a liquefied oxygen reservoir or a gaseous or liquefied oxygen pipeline The present invention is particularly useful for processes using a rich oxidant In the present context, the term "preheating" refers to 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 at least a part of the overall flow of oxygen is advantageously heated to a temperature TOf between 250 ° C and 620 ° C, preferably between 300 ° C and 600 ° C and more preferably between 350 ° C and 580 ° C dir upstream of the combustion chamber, that is to say directly upstream of burners or lances which is equipped with the combustion chamber and which are used for the injection of oxygen preheated in the combustion chamber.
    [0007] Advantageously, the oxygen-depleted air stream is used for preheating the at least part of the overall flow of oxygen, for example by heat exchange between the depleted air and the at least part of the overall flow in a heat exchanger. heat. Indeed, as a function of the temperature TA1 of the air at the inlet of the oxygen production unit, the depleted air flow at the outlet of this oxygen production unit may have a temperature TA2 of 400 ° C to 750 ° C, preferably 450 ° C to 700 ° C and more preferably 500 ° C and 650 ° C. This oxygen-depleted airflow therefore has a thermal energy which can be usefully used to increase the energy efficiency of the process.
    [0008] Thus, according to one embodiment, the at least part of the overall flow of oxygen is heated directly upstream of the combustion chamber by heat exchange with the stream of oxygen depleted air from the production unit of oxygen. It is also advantageous to preheat at least a portion of the burned fuel in the combustion chamber. In this case, it is preferable that at least a portion of the fuel burned in the combustion chamber is preheated upstream of the combustion chamber by heat exchange with the oxygen depleted air stream from the production unit. oxygen, typically in a heat exchanger. By "heat exchanger" or "exchanger" is meant an installation or device in which two fluids of different temperatures circulate in separate enclosures and transmit heat from one of the two fluids (the hottest fluid) to the other of the two fluids (the least hot fluid) through one or walls separating the two enclosures. However, this does not exclude the use of other heat sources for the preheating of oxygen and / or fuel, alone or, preferably, in combination with a heat exchange with the oxygen-depleted air stream. The process according to the invention is useful and advantageous for any high temperature combustion chamber. The combustion chamber may thus be a melting chamber, such as a metal melting chamber or, preferably, a vitrifiable material melting chamber. An example of such a melting chamber is a "float" type glass melting chamber. The chamber may also be a calcination chamber, for example for the calcination of cement or a reheating chamber, such as steel heating chambers. It is noted that the term "combustion chamber" is not limited to static combustion chambers, but also covers rotary combustion chambers.
    [0009] The invention and its advantages will be better understood in the light of the following example of a method according to the invention and an installation adapted for the implementation of such a method, reference being made to FIG. 1 which is a schematic representation of such an installation for glass melting suitable for implementing the method according to the invention.
    [0010] Said installation comprises a combustion chamber 100, more particularly a melting or melting / glass refining chamber, provided with one or more burners 200 adapted for the combustion of a fuel rich in oxygen and preheated. The plant also comprises an oxygen-rich oxidizer distribution network for supplying said burners 200 with oxidant, as well as a fuel distribution network for supplying said burners 200 with fuel (for example, natural gas). . Although only one burner is shown in the figure, the combustion chamber typically comprises several or even a large number of burners, for example in the case of a "float" type melting furnace.
    [0011] The fumes generated by the combustion are discharged from the combustion chamber 100 and sent into a flue gas evacuation circuit 11. One or more heat exchangers 10, called primary exchangers, are placed on the flue gas evacuation circuit 11. downstream of the combustion chamber 100. In the primary heat exchanger 10, part of the residual heat of the flue gases discharged is transferred to an air stream 21, on the one hand obtaining a flow of hot air 22 and, on the other hand, a flow of fumes vented temperate 12. The hot air reaches a temperature of about 700 ° C and up to 900 ° C, or up to 950 ° C output of a primary heat exchanger 10. The hot air flow 22 is thus raised to a temperature level at which the extraction of oxygen on an MTI can be carried out on an industrial scale. It is at a pressure close to atmospheric. This flow of hot air 22 is introduced into an oxygen production unit by extraction using ceramic MTI 20 with a capacity of 1 to 100 tons of oxygen per day.
    [0012] At these pressures and with a suitable membrane surface, the extraction yield is, for example, of the order of 50%. There is thus obtained at the output of the production unit 20 a first flow of oxygen 50 and a flow of air depleted of oxygen 23.
    [0013] The first oxygen stream 50 produced from MTI is hot, with a TOI temperature of the order of 900 ° C. This hot oxygen 50 is directly injected into an oxygen distribution network where it is mixed with colder oxygen 60 from another source of oxygen (such as a US gas separation unit). air, in English: ASU (air separation unit), a VSA (vacuum swing adsorption = adsorption with vacuum), a reservoir of LOX (liquid oxygen) or oxygen gas circuit). oxygen 70 containing 20 to 25% vol (and up to 50% vol) of oxygen from the oxygen production unit at MTI and from 75 to 80% vol (and up to 50% vol) of oxygen from the other source of oxygen.
    [0014] The hot oxygen produced from MTI is thus cooled without loss of energy for the installation and can safely be transported in the oxygen distribution network whose materials do not have to withstand the very aggressive conditions of the environment. oxygen at very high temperature. The oxygen mixture of different sources thus obtained is then used as oxygen-rich oxidant to generate combustion of the fuel in the combustion / fusion chamber 30. According to the invention, it is possible to optimize the configuration of the installation melting glass by positioning the oxygen production unit (s) 20 at the most appropriate location, even if it is at a distance from the burners 200 of the combustion chamber 100 and it is not necessary to to use generally oxygen intensive high temperature oxygen-carrying materials 70. In the illustrated embodiment, oxygen production by MTI is integrated with a preheating technology. oxygen and fuel, for example natural gas, for supplying the oxy-fuel burners 200 of the combustion chamber 100 of the glass fusion plant. A similar oxygen preheating technology is in particular known from US-A-6071116. The oxygen depleted air 21 from the oxygen production unit 20, which has a temperature TA2 of the order of 450 ° C, is channeled to secondary heat exchangers 31 and 32. In the first secondary exchanger 31, part of the oxygen-depleted air 23 is used for preheating the fuel 25, for example natural gas, upstream of the burners 200 of the combustion chamber 100. A preheated fuel stream 26 is obtained which is supplied to the burners 200 and a first temperate flow of oxygen-depleted air 27.
    [0015] Similarly, in the second secondary exchanger 32, part of the oxygen-depleted air 23 is used for preheating at least part of the overall flow of oxygen 70 upstream of said burners 200. preheated oxygen 71 which is supplied to the burners 200 and a second tempered stream of oxygen depleted air 28.
    [0016] A single first secondary exchanger 31 and a single second secondary exchanger 32 are shown in FIG. 1. However, the installation may comprise several first secondary exchangers 31 and several second secondary exchangers 32. In particular, when the combustion chamber comprises a large number of 200, the installation may comprise a number of first secondary heat exchangers 31 and a number of second secondary heat exchangers 32, each heat exchanger 31 and 32 supplying a limited number of burners 200, or even a single burner (200). This allows in particular to limit the pipes for transporting preheated fuel, respectively preheated oxygen. Although, according to the invention, the oxygen produced from MTI is cooled by mixing it with oxygen from another source, the invention nevertheless makes it possible to have a temperature of oxygen (mixture of oxygen or oxygen stream) at the inlet of the secondary heat exchanger 32, typically at a temperature of about 300 ° C, and thus to reduce the size and cost of the secondary heat exchanger (s) 31 for the preheating of the heat exchanger. 'oxygen.
    [0017] The present invention thus makes it possible to use the residual heat of the fumes discharged from the combustion chamber 100 for the production of oxygen and for the preheating of the fuel and an oxygen-rich oxidant, to optimize the configuration of the installation. and limit the use of materials that must withstand hot oxygen.
    权利要求:
    Claims (11)
    [0001]
    CLAIMS1) oxyfuel combustion process in which: - a fuel is burned with oxygen-rich oxidant in a combustion chamber (100) with generation of heat and smoke in the combustion chamber - the fumes generated (11) are removed of the combustion chamber (100), said evacuated smoke containing residual heat, - an air flow (21) is heated by means of at least a part of the residual heat present in the evacuated fumes, with obtaining of a flow of hot air (22) at a temperature TA1, - at least a portion of the hot air flow (22) is introduced into an oxygen production unit (20) in which a portion of the oxygen present in said at least a portion of the hot air flow (20) by means of one or more MTIs, obtaining a first oxygen flow (50) at a temperature TOI and an air flow depleted in oxygen (23) at a temperature TA2, with TA2 <TA1, - in downstream of the oxygen generating unit (20), the first oxygen stream (50) is mixed with a second oxygen stream (60) so as to obtain an overall oxygen flow (70) to a temperature T02, with TO2 <T01, - at least a part of the overall flow of oxygen (70) is transported to the combustion chamber (100) and used as oxygen-rich oxidant in the combustion chamber (100), said at least a portion of the overall oxygen stream (70) being heated to a temperature TOf directly upstream of the combustion chamber (100), with TOf> T02.
    [0002]
    2) A method of heating according to claim 1, wherein the hot air stream (22) has a temperature TA1 of 700 ° C to 1000 ° C, preferably 750 ° C to 950 ° C and more preferably 800 ° C at 900 ° C. 30
    [0003]
    3) Process according to any one of the preceding claims, wherein the hot air stream (22) has a pressure PA1 of 1 bar ab to 6 bar ab at the inlet of the oxygen production unit, preferably from 1 bar ab to 3 bar ab and preferably from 1 bar ab to 2 bar ab
    [0004]
    4) Process according to any preceding claim, wherein the portion of oxygen extracted from the at least a portion of the hot air stream (22) corresponds to between% and 100%, preferably between 20% and 70% still more preferably between 20% and 50% of the oxygen present in said at least a portion of the hot air stream.
    [0005]
    5. A process as claimed in any one of the preceding claims, wherein the temperature TA2 of the oxygen-depleted air stream (23) from 400 ° C to 750 ° C, preferably from 450 ° C to 700 ° C, and preferably 500 ° C and 650 ° C
    [0006]
    6) Process according to any one of the preceding claims, wherein the first oxygen flux (50) corresponds to between 90% and 0% vol, preferably between 90% and 15% vol, more preferably between 80% and 20% vol, even between 80% and 30% vol, and even more preferably between 80% and 50% vol of the overall flow of oxygen (70).
    [0007]
    A process as claimed in any one of the preceding claims, wherein the second oxygen stream (60) is provided by an air gas separation unit, a VSA, a liquefied oxygen reservoir or a gas line. oxygen gas.
    [0008]
    Process according to any one of the preceding claims, wherein the at least a part of the overall flow of oxygen (70) is heated to a temperature TOf between 250 ° C and 620 ° C, preferably between 300 ° C and 600 ° C and more preferably between 350 ° C and 580 ° C directly upstream of the combustion chamber (100).
    [0009]
    9) Process according to any one of the preceding claims, wherein the at least a portion of the overall flow of oxygen (70) is heated directly upstream of the combustion chamber (100) by heat exchange with the air flow depleted oxygen (23) from the oxygen production unit (20).
    [0010]
    A method according to any one of the preceding claims, wherein at least a portion of the fuel (25) burned in the combustion chamber (100) is preheated upstream of the combustion chamber (100) by heat exchange with the flow of oxygen-depleted air (23) from the oxygen production unit (20).
    [0011]
    11) A method according to any one of the preceding claims wherein the combustion chamber (100) is a melting chamber, preferably a vitrifiable material melting chamber, a calcining chamber or a steel heating chamber.
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    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
    FR1363503A|FR3015635B1|2013-12-23|2013-12-23|INTEGRATED PROCESS FOR OXYCOMBUSTION AND OXYGEN PRODUCTION|
    FR1363503|2013-12-23|FR1363503A| FR3015635B1|2013-12-23|2013-12-23|INTEGRATED PROCESS FOR OXYCOMBUSTION AND OXYGEN PRODUCTION|
    KR1020167018986A| KR20160111380A|2013-12-23|2014-12-19|Integrated process for oxy-fuel combustion and production of oxygen|
    PCT/FR2014/053478| WO2015097389A1|2013-12-23|2014-12-19|Integrated process for oxy-fuel combustion and production of oxygen|
    MX2016008291A| MX2016008291A|2013-12-23|2014-12-19|Integrated process for oxy-fuel combustion and production of oxygen.|
    EP14830993.3A| EP3087319A1|2013-12-23|2014-12-19|Integrated process for oxy-fuel combustion and production of oxygen|
    CN201480074698.XA| CN105980776A|2013-12-23|2014-12-19|Integrated process for oxy-fuel combustion and production of oxygen|
    JP2016541125A| JP2017502245A|2013-12-23|2014-12-19|Integrated process of oxyfuel combustion and oxygen generation|
    US15/107,542| US10197274B2|2013-12-23|2014-12-19|Integrated process for oxy-fuel combustion and production of oxygen|
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