METHOD FOR OPERATING A FIRED FURNACE AND ARRANGEMENT COMPRISING SUCH A FURNACE

Abstract

The invention concerns a process for operating a fired furnace which is heated using a fuel gas stream and forming a combustion product stream, wherein heat of at least part of the combustion product stream is used in forming a steam stream. It is provided that at least a part of the steam stream is subjected to a high-temperature electrolysis to form a hydrogen-containing and an oxygen-containing material stream, and that at least a part of the hydrogen-containing material stream is used as the fuel gas stream. A corresponding arrangement is also the subject of the invention.

Claims

1-13. (canceled)

14. A method for operating a fired furnace which is heated using a fuel gas stream and forming a combustion product stream, wherein heat of at least a part of the combustion product stream is used in forming a steam stream, wherein at least a part of the steam stream is subjected to a high temperature electrolysis to form a hydrogen-containing and an oxygen-containing substance stream, and that at least a part of the hydrogen-containing substance stream is used as the fuel gas stream, wherein the formation of the steam stream comprises a plurality of heat exchange steps to which the combustion product stream or a part thereof is subjected, wherein water used to form the steam stream and/or steam used to form the steam stream is heated in the heat exchange steps and wherein the heat exchange steps comprise a first heat exchange step in which the combustion product stream or a portion thereof is cooled from a temperature level of 1400 to 1600° C. to a temperature level of 900 to 1100° C., and in which saturated steam used to form the steam stream is superheated from a temperature level of 100 to 120° C. to a temperature level of 700 to 900° C.

15. The method according to claim 14 in which, in addition, at least a part of the oxygen-containing substance stream is used together with the fuel gas stream to heat the furnace.

16. The method according to claim 14, wherein the formation of the steam stream comprises a plurality of heat exchange steps to which the combustion product stream or a part thereof is subjected, wherein water used to form the steam stream and/or steam used to form the steam stream is heated in the heat exchange steps.

17. The method according to claim 14, in which the formation of the steam stream comprises a combined heat exchange step to which the combustion product stream or part thereof is subjected, wherein water used to form the steam stream and/or steam used to form the steam stream is heated in the combined heat exchange step.

18. The method according to claim 14, wherein the heat exchange steps comprise a second heat exchange step in which the combustion product stream or a portion thereof is cooled from a temperature level of 900 to 1100° C. to a temperature level of 100 to 200° C., and in which water used to form the vapor stream is evaporated to form saturated vapor.

19. The method according to claim 14, wherein the heat exchange steps comprise a first heat exchange step in which the combustion product stream or a portion thereof is cooled from a temperature level of 1400 to 1600° C. to a temperature level of 600 to 700° C., and in which water used to form the vapor stream is evaporated to form saturated vapor.

20. The method according to claim 19, wherein the heat exchange steps comprise a second heat exchange step in which the combustion product stream or a portion thereof is cooled from a temperature level of 600 to 700° C. to a temperature level of 100 to 200° C., and in which saturated steam used to form the steam stream is superheated from a temperature level of 100 to 120° C. to a temperature level of 700 to 900° C.

21. The method according to claim 19, wherein the heat exchange steps comprise a second heat exchange step in which the combustion product stream or part thereof is cooled from a temperature level of 600 to 700° C. to a temperature level of 300 to 400° C., and in which the hydrogen-containing and/or oxygen-containing substance stream formed in the high temperature electrolysis is heated.

22. The method according to claim 18, wherein the heat exchange steps comprise a third heat exchange step in which the combustion product stream or a part thereof is cooled from a temperature level of 100 to 200° C. to a lower temperature level and is thereby partially condensed, and in which water used to form the steam stream is preheated.

23. The method according to claim 22 in which the flue gas or at least its part subjected to the second and third cooling steps is compressed between the second and third cooling steps or after the third cooling step.

24. The process according to claim 17 in which a heater operated by a separate heat source is also used to evaporate the water.

25. The method according to claim 14 in which the hydrogen-containing and oxygen-containing substance streams formed in the high temperature electrolysis are cooled against steam supplied to the high temperature electrolysis.

26. The method according to claim 14 in which the furnace is partially electrically heated.

Description

SHORT DESCRIPTION OF THE DRAWINGS

[0064] FIG. 1 illustrates an arrangement according to an embodiment of the invention.

[0065] FIG. 2 illustrates an arrangement according to an embodiment of the invention.

[0066] FIG. 3 illustrates an arrangement according to an embodiment of the invention.

DETAILED DESCRIPTION OF THE DRAWINGS

[0067] FIG. 1 illustrates an arrangement in accordance with an embodiment of the present invention designated 100. Further embodiments are illustrated in FIGS. 2 and 3, where they are designated 200 and 300 respectively. The arrangement 100 in FIG. 1 corresponds at least in part to the first embodiment of the invention described above, the arrangement 200 in FIG. 2 corresponds at least in part to the second embodiment described above and the arrangement 300 in FIG. 3 corresponds at least in part to the third embodiment of the invention described above.

[0068] All arrangements 100 to 300 have in common a glass melting furnace 1 and an electrolysis device 2 with a cathode side 21 and an anode side 22, all arrangements 100 to 300 also provide water (boiler feed water) (W) and ultimately use it to form two steam streams 111 and 112 which are supplied to the cathode side 21 and the anode side 22, respectively, of the electrolysis device 2. The formation of these steam streams 111 and 112 is explained separately for the individual embodiments below.

[0069] Using the electrolysis device, a hydrogen-containing 121 and an oxygen-containing 122 gas stream are also formed in all embodiments. In addition to hydrogen and oxygen, both gas streams 121 and 122 also contain water in the form of superheated steam. They are fed to the glass melting furnace 1 and burned there. An external oxygen feed 3 can be provided to cover any additional oxygen demand that may be required. In all the forms of the present invention, a combustion product stream 131 is extracted from the glass melting furnace 1. The embodiments of the present invention, which are illustrated using arrangements 100 to 300, differ in particular in the sequence or specific embodiment of heat recovery from the combustion product stream 131, which is explained in detail below.

[0070] In the arrangement 100 as shown in FIG. 1, the combustion product stream 131 is first fed to a heat exchanger X1 in which saturated steam 103 is superheated and superheated steam 104 is formed. The superheated steam is divided into steam streams 111 and 112. After cooling down in the heat exchanger X1, the combustion product stream F is fed to a heat exchanger X2, in which preheated water is evaporated to saturated steam. The preheated water is supplied in the form of a water stream 102 and passed through the heat exchanger X2 in the form of a partial stream 102a. Another partial current 102b is evaporated in an electric heater E1. The evaporated partial streams 102a and 102b are combined after the evaporation to a saturated steam stream 103.

[0071] After cooling in the heat exchanger X2, the combustion product stream 131 is subjected to compression in a compressor or blower C1 and then passed through another heat exchanger X3, which serves to preheat the water stream 101. The water contained in the combustion product stream 131 condenses at least partially in the heat exchanger X3.

[0072] Further elements shown in FIG. 1 are further electric heaters E2 and E3, which use steam streams 111 and 112 respectively in cases where there is no or too little waste heat from the combustion product stream 131.

[0073] In the arrangement 200 illustrated in FIG. 2, the combustion product stream 131 first streams through the heat exchanger X1 and is cooled accordingly. In heat exchanger X1, preheated water (boiler feed water) 102 is evaporated to saturated steam 103. As explained above, in this arrangement the formation of the partial currents 102a and 102b and the use of electric heater E1 can be dispensed with. After cooling in heat exchanger X1, combustion product stream 131 is passed through heat exchanger X2, where superheated steam 104 is generated. The further arrangement here essentially corresponds to that shown in FIG. 1, although the electric heaters E2 and E3 are permanently operated here due to the lower degree of overheating in the heat exchanger X2.

[0074] FIG. 3 illustrates an arrangement according to a further development of the present invention and is marked with a total of 300. This in turn differs in the use of heat exchangers and the type of waste heat recovery.

[0075] The combustion product stream 131 is passed through heat exchangers X2a and X2b downstream of heat exchanger X1, the use of which basically corresponds to that of FIG. 2 and arrangement 200, and is thus used to heat the hydrogen-containing substance stream 121 and the oxygen-containing substance stream 122. These substance streams 121 and 122 are compressed in compressors C2 and C3, which, as mentioned above, is possible due to a previous cooling of the gas streams 121 and 122. This cooling in turn takes place in heat exchangers X3a and X3b in counterflow to steam streams 111 and 112, which are initially provided here in an unheated or only slightly overheated state and, after overheating in heat exchangers X3a and X3b, are fed to electrolysis unit 2. A further cooling of the combustion product stream 131 takes place in the heat exchanger X4 by overheating the steam stream 103. As also illustrated here, a (particularly adjustable) partial stream 121a of the substance stream 121 is returned to the high-temperature electrolysis 1, as explained above.