CN114620694A - Device and method for removing reducing gas - Google Patents
Device and method for removing reducing gas Download PDFInfo
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- CN114620694A CN114620694A CN202011455672.3A CN202011455672A CN114620694A CN 114620694 A CN114620694 A CN 114620694A CN 202011455672 A CN202011455672 A CN 202011455672A CN 114620694 A CN114620694 A CN 114620694A
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- 239000007789 gas Substances 0.000 claims abstract description 145
- 230000003197 catalytic effect Effects 0.000 claims abstract description 83
- 230000008929 regeneration Effects 0.000 claims abstract description 46
- 238000011069 regeneration method Methods 0.000 claims abstract description 46
- 239000003054 catalyst Substances 0.000 claims abstract description 30
- 239000001257 hydrogen Substances 0.000 claims abstract description 19
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 19
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 25
- 239000012495 reaction gas Substances 0.000 claims description 18
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 16
- 229910052757 nitrogen Inorganic materials 0.000 claims description 12
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- 150000003624 transition metals Chemical class 0.000 claims description 7
- 238000010438 heat treatment Methods 0.000 claims description 6
- 229910000314 transition metal oxide Inorganic materials 0.000 claims description 6
- BASFCYQUMIYNBI-UHFFFAOYSA-N platinum Substances [Pt] BASFCYQUMIYNBI-UHFFFAOYSA-N 0.000 claims description 5
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- 229910052748 manganese Inorganic materials 0.000 claims description 3
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- 230000009467 reduction Effects 0.000 claims description 3
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- 239000010970 precious metal Substances 0.000 claims 1
- 125000004435 hydrogen atom Chemical class [H]* 0.000 abstract 1
- SWQJXJOGLNCZEY-UHFFFAOYSA-N helium atom Chemical compound [He] SWQJXJOGLNCZEY-UHFFFAOYSA-N 0.000 description 15
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- 239000000446 fuel Substances 0.000 description 10
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- 238000006356 dehydrogenation reaction Methods 0.000 description 4
- 238000010586 diagram Methods 0.000 description 4
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- 229910052799 carbon Inorganic materials 0.000 description 1
- 229910002091 carbon monoxide Inorganic materials 0.000 description 1
- 238000001514 detection method Methods 0.000 description 1
- 229910001873 dinitrogen Inorganic materials 0.000 description 1
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- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B23/00—Noble gases; Compounds thereof
- C01B23/001—Purification or separation processes of noble gases
- C01B23/0015—Chemical processing only
- C01B23/0026—Chemical processing only by reduction
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
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- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/62—Carbon oxides
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/86—Catalytic processes
- B01D53/8671—Removing components of defined structure not provided for in B01D53/8603 - B01D53/8668
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- B01D2255/1025—Rhodium
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- B01D—SEPARATION
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- B01D2255/20753—Nickel
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Abstract
The invention belongs to the technical field of reducing gas treatment, and discloses a device and a method for removing reducing gas, wherein the device comprises: the system comprises two catalytic reactors with switchable operation modes, wherein one of the two catalytic reactors is in a normal operation mode, the other one of the two catalytic reactors is in a regeneration operation mode, and the two catalytic reactors are respectively a first catalytic reactor and a second catalytic reactor; the two fans are respectively a first fan and a second fan; the two preheaters are respectively a first preheater and a second preheater; a heater; the catalytic reactor is connected with a plurality of pipelines and valves, and realizes the switching between the normal operation mode and the regeneration operation mode of the catalytic reactor through the opening and closing of the valves; the invention realizes the regeneration of the catalyst by periodically switching the reactors, prolongs the service life of the catalyst, effectively realizes the continuous removal of hydrogen, does not introduce other gases and ensures the purity of the gases.
Description
Technical Field
The invention belongs to the technical field of reductive gas treatment, and particularly relates to a device and a method for removing reductive gas.
Background
Helium is widely applied to the fields of aerospace, refrigeration, medical treatment, optical fiber, leak detection, deep sea diving, high-precision welding production and the like due to the properties of low density, low boiling point and inertia of helium. In particular, in the launching engineering of space launch vehicles which adopt liquid hydrogen/liquid oxygen as fuel in the space launch field, the helium is widely used for safe replacement of pipelines, safe replacement of rocket storage tanks, pressurization and gas supplement of rocket storage tanks in the flying process and safe blowing of part of low-temperature components due to the low boiling point and the safety of helium. At present, no other product can replace the helium function. Helium gas is separated and extracted mainly from helium-rich natural gas. The gas of the liquefied natural gas factory contains a large amount of helium resources, the gas is non-condensable gas in the production process of the liquefied natural gas, the gas is generally recycled and re-liquefied, part of the gas can be used as fuel of a factory boiler to be burnt, and the other part of the gas is burnt by a torch and discharged into the atmosphere, wherein the contained rare helium resources are wasted, and the gas is recovered and purified to serve as an important source of helium.
The fuel cell is a power generation device which directly converts chemical bond energy stored in fuel and oxidant into electric energy through electrode reaction, and has high energy conversion efficiency and small environmental pollution. The proton exchange membrane fuel cell technology has been developed at a high speed, and is particularly suitable for a mobile power supply, a standby power supply and a decentralized power station, the most ideal raw material of the proton exchange membrane fuel cell is pure hydrogen, during the operation of the proton exchange membrane fuel cell, hydrogen is supplied to an anode, and air or oxygen is supplied to a cathode, and because the hydrogen cannot be completely utilized by 100 percent, a small amount of hydrogen is inevitably discharged out of a proton exchange membrane fuel cell system along with tail gas of the anode. If the hydrogen-containing tail gas is directly discharged, not only great waste of fuel of the proton exchange membrane fuel cell is caused, but also environmental pollution is caused, and dangerous accidents of combustion or explosion can be caused.
Chinese patent CN110844893A discloses a device and method for extracting helium from crude helium containing hydrogen, and provides a device for extracting helium from crude helium containing hydrogen. The device can effectually get rid of the hydrogen in the feed gas through setting up the dehydrogenation subassembly, through setting up membrane separation device, can utilize the membrane separation subassembly among the membrane separation device to effectively separate impurity gas such as methane, nitrogen gas, argon gas in the feed gas after the dehydrogenation, through setting up pressure swing adsorption equipment, can carry out pressure swing adsorption to the gas after membrane separation device separates, further improves helium purity.
Chinese patent CN101543776A discloses a dehydrogenation catalyst for carbon monoxide raw material gas and a preparation and application method thereof, the catalyst which adopts stepwise impregnation preparation and uses alumina as a carrier, palladium or platinum as an active component and alkaline earth metal and transition metal as an auxiliary agent can deeply remove less than 5% of hydrogen in the CO raw material gas, and the dehydrogenation rate is more than 99%.
Therefore, the catalytic oxidation method is generally adopted for removing the reducing gas, and although the method can treat and remove the reducing gas, oxygen or nitrogen can be introduced during the use process to influence the gas purity; and the process is complex, the energy consumption is large, and the stable operation in a long period cannot be realized.
Disclosure of Invention
In view of the above, the present invention aims to provide an apparatus and a method for removing reducing gas; specifically, the regeneration of the catalyst is realized by periodically switching the reactors, and simultaneously, the continuous removal of hydrogen is effectively realized, and other gases are not introduced, so that the gas purity is ensured.
In order to achieve the purpose, the invention provides the following technical scheme:
an apparatus for removing a reducing gas, comprising:
the system comprises two catalytic reactors with switchable operation modes, wherein one of the two catalytic reactors is in a normal operation mode, the other one of the two catalytic reactors is in a regeneration operation mode, and the two catalytic reactors are respectively a first catalytic reactor and a second catalytic reactor;
the two fans are respectively a first fan and a second fan; the first fan is used for introducing a first mixed gas containing reducing gas into one catalytic reactor in a normal operation mode; the second fan is used for introducing a second mixed gas formed by mixing air and nitrogen into the other catalytic reactor in the regeneration operation mode;
the two preheaters are respectively a first preheater and a second preheater; the first preheater is connected between the first fan and the second preheater and is used for realizing preliminary heat exchange between reaction gas generated in one catalytic reactor in the normal operation mode and first mixed gas introduced by the first fan; the second preheater is connected to the gas outlet end of the first preheater and is used for realizing secondary heat exchange between the reaction gas generated in one catalytic reactor in the regeneration operation mode and the first mixed gas after the primary heat exchange;
the heater is connected to the gas outlet end of the second preheater and used for finally heating the first mixed gas after the secondary heat exchange and enabling the heated first mixed gas to enter a catalytic reactor in a normal operation mode;
a plurality of connecting lines and valves; the connecting pipes are used for being in conduction connection with the two catalytic reactors, the two fans, the two preheaters and the heater, the valves are respectively arranged on the corresponding connecting pipelines, and the switching between the normal operation mode and the regeneration operation mode of the catalytic reactors is realized through the opening and closing of the valves.
Preferably, the preheater adopts a shell-and-tube heat exchanger or a plate heat exchanger.
Preferably, the heater is an electric heater or a combustion heater.
Preferably, the first preheater preliminarily preheats the first mixed gas to 40-500 ℃, the second preheater preheats the first mixed gas to 80-500 ℃ again, and the heater finally heats the first mixed gas to 100-500 ℃.
Preferably, the first mixed gas contains hydrogen and/or CO, and the ratio of the hydrogen and/or CO is 0.01 vol.% to 10 vol.%.
Preferably, the catalyst is a particle or regular structure catalyst.
Preferably, the active component of the catalyst is one or a combination of several of transition metal oxides; or an alloy of a transition metal and a noble metal; or a noble metal supported on a transition metal oxide;
the transition metal comprises one or a combination of more of Co, Mn, Cu, Cr, Mo and Fe, and the noble metal comprises one or a combination of more of Pt, Pd and Rh.
Preferably, in the catalytic reactor, the space velocity of the reactor is 1000--1The reaction temperature is 20-800 ℃.
Preferably, when any one catalytic reactor is in a regeneration operation mode, the regeneration gas is mixed gas of air and nitrogen; the regeneration temperature of the catalyst is 20-800 ℃, and the regeneration time is 1-24 h.
In order to achieve the above purpose, the invention also provides the following technical scheme:
a method for removing reducing gas comprises the following steps:
introducing a first mixed gas containing reducing gas into a first preheater for preliminary preheating;
introducing the primarily preheated first mixed gas into a second preheater for secondary preheating;
introducing the preheated first mixed gas into a heater for heating;
introducing the heated first mixed gas into a catalytic reactor which normally operates to perform a reduction catalytic reaction;
and introducing a second mixed gas formed by mixing air and nitrogen into the catalytic reactor in the regeneration operation to perform the oxidation regeneration reaction of the catalyst.
Specifically, the method comprises the following steps:
when the first catalytic reactor or the second catalytic reactor normally operates, the reacted reaction gas is introduced into the first preheater to provide a heat source for primary preheating of the first mixed gas in the first preheater;
when the second catalytic reactor or the first catalytic reactor is in regeneration operation, the reacted reaction gas is introduced into the second preheater to provide a heat source for the second preheating of the first mixed gas in the second preheater.
Compared with the prior art, the invention has the following beneficial effects:
(1) the method for removing the reducing gas provided by the invention not only can realize the removal of the reducing gas, but also can realize the oxidation regeneration of the catalyst and prolong the service life of the catalyst.
(2) The method for removing the reducing gas provided by the invention has the advantages of flexible operation, low operation cost, high efficiency and high economy.
(3) In the device for removing the reducing gas, the adopted purifying catalyst has good activity and stability, long service life and small system pressure drop.
Drawings
FIG. 1 is a schematic structural diagram of a device for removing reducing gas according to the present invention;
FIG. 2 is a schematic diagram illustrating the operation of an apparatus for removing reducing gases in the first embodiment of the present invention;
fig. 3 is an operation schematic diagram of a device for removing reducing gas in the second embodiment of the present invention.
Detailed Description
The technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only a part of the embodiments of the present invention, and not all of the embodiments. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.
Specifically, referring to fig. 1, a schematic structural diagram of an apparatus for removing reducing gas according to the present invention is shown, and it can be seen that the apparatus includes:
the system comprises two catalytic reactors with switchable operation modes, wherein one of the two catalytic reactors is in a normal operation mode, the other one of the two catalytic reactors is in a regeneration operation mode, and the two catalytic reactors are respectively a first catalytic reactor 1 and a second catalytic reactor 2;
the two fans are respectively a first fan 3 and a second fan 4; and the first fan 3 is used for introducing a first mixed gas containing a reducing gas into one catalytic reactor in a normal operation mode; the second fan 4 is used for introducing a second mixed gas formed by mixing air and nitrogen into the other catalytic reactor in the regeneration operation mode;
two preheaters, namely a first preheater 5 and a second preheater 6; the first preheater 5 is connected between the first fan 3 and the second preheater 6 and is used for realizing preliminary heat exchange between the reaction gas generated in one catalytic reactor in the normal operation mode and the first mixed gas introduced by the first fan 3; the second preheater 6 is connected to the gas outlet end of the first preheater 5 and is used for realizing the secondary heat exchange between the reaction gas generated in one catalytic reactor in the regeneration operation mode and the first mixed gas after the primary heat exchange;
a heater 7 connected to the outlet end of the second preheater 6 for finally heating the reheated first mixed gas and making the heated first mixed gas enter a catalytic reactor in a normal operation mode;
a plurality of connecting lines and valves; and the plurality of connecting pipes are used for conducting and connecting the two catalytic reactors, the two fans, the two preheaters and the heater 7, the plurality of valves are respectively arranged on the corresponding connecting pipes, and the switching between the normal operation mode and the regeneration operation mode of the catalytic reactors is realized through the opening and closing of the plurality of valves. Specifically, as can be seen from fig. 1, the valves include a valve a, a valve B, a valve C, a valve D, a valve E, a valve F, a valve G, and a valve H.
In conclusion, the two catalytic reactors can be alternately subjected to regeneration operation and normal operation by switching the connecting pipeline and the valve, so that the whole device can be continuously catalyzed, and the catalytic reactors can be ensured to be subjected to catalyst regeneration at regular time, so that the service life of the catalyst is effectively prolonged; and the whole structure is simple, the adopted purifying catalyst has good activity and stability, the service life is long, and the pressure drop of the system is small.
Further, in the embodiment of the invention, the preheater adopts a shell-and-tube heat exchanger or a plate heat exchanger. The heater adopts an electric heater or a combustion type heater.
In the embodiment of the present invention, the first mixed gas contains hydrogen and/or CO in an amount of 0.01 vol.% to 10 vol.%.
In the embodiment of the invention, the catalyst is a granular or regular structure catalyst. The active component of the catalyst can be one or a combination of more of transition metal oxides; or an alloy of a transition metal and a noble metal; can also be a noble metal supported by a transition metal oxide; the embodiment of the present invention is not particularly limited to the form of the active component of the catalyst.
Specifically, the transition metal comprises one or a combination of more of Co, Mn, Cu, Cr, Mo and Fe, and the noble metal comprises one or a combination of more of Pt, Pd and Rh.
In the embodiment of the invention, the space velocity of the reactor is 1000--1The reaction temperature is 20-800 ℃.
When any catalytic reactor is in a regeneration operation mode, the regeneration gas adopts mixed gas of air and nitrogen; the regeneration temperature of the catalyst is 20-800 ℃, and the regeneration time is 1-24 h.
The valve in the embodiment of the invention adopts a pneumatic or electric ball valve and a butterfly valve;
in the embodiment of the invention, the first preheater preheats the first mixed gas to 40-500 ℃ initially, the second preheater preheats the first mixed gas to 80-500 ℃ again, and the heater finally heats the first mixed gas to 100-500 ℃.
Based on the device for removing the reducing gas disclosed above, the invention also provides a method for removing the reducing gas, which specifically comprises the following steps:
introducing a first mixed gas containing reducing gas into a first preheater 5 for preliminary preheating;
introducing the primarily preheated first mixed gas into a second preheater 6 for secondary preheating;
introducing the preheated first mixed gas into a heater 7 for heating;
introducing the heated first mixed gas into a catalytic reactor which normally operates to perform a reduction catalytic reaction;
and introducing a second mixed gas formed by mixing air and nitrogen into the catalytic reactor in the regeneration operation to perform the oxidation regeneration reaction of the catalyst.
When the first catalytic reactor or the second catalytic reactor normally operates, the reacted reaction gas is introduced into the first preheater to provide a heat source for primary preheating of the first mixed gas in the first preheater;
when the second catalytic reactor or the first catalytic reactor is in regeneration operation, the reacted reaction gas is introduced into the second preheater to provide a heat source for the second preheating of the first mixed gas in the second preheater.
Specifically, according to the operation steps of the above method, the following operation examples are provided:
example one
In the present embodiment the first catalytic reactor 1 is in normal operation mode and the second catalytic reactor 2 is in regeneration operation mode.
Specifically, please refer to fig. 2, in which the valves in the circular dashed boxes are shown in a closed state, and the valves B, C, F, and G are closed in the embodiment.
As can be seen from the above, in this embodiment, the method for removing reducing gas based on the apparatus for removing reducing gas provided by the present invention includes:
a first mixed gas which is at normal temperature and contains 2% vol of hydrogen is pressurized to 8kPag by a first fan 3 and then is introduced into a first preheater 5; meanwhile, after a second mixed gas formed by mixing air and nitrogen is pressurized to 8kPag through a second fan 4, the second mixed gas enters the second catalytic reactor 2 through a valve D to perform oxidation regeneration on the catalyst in the second catalytic reactor 2, and the reacted reaction gas enters a second preheater 6 through a valve E;
in the first preheater 5, the first mixed gas is subjected to primary heat exchange with the reaction gas generated in the first catalytic reactor 1 under the normal operation mode, so that the first mixed gas is heated to 40 ℃ in a heat exchange manner; then the mixture enters a second preheater 6 through a corresponding connecting pipeline, and in the second preheater 6, the primarily heated first mixed gas and the reaction gas generated in the second catalytic reactor 2 under the regeneration operation mode are subjected to heat exchange again, so that the first mixed gas is heated to 80 ℃ in a heat exchange manner;
then, the reheated first mixed gas is introduced into the heater 7 through the corresponding connecting pipeline, so that the first mixed gas is finally heated to 110 ℃;
then, the finally heated first mixed gas enters the first catalytic reactor 1 through a valve a, a catalytic reduction reaction is performed, and the reacted reaction gas enters the first preheater 5 through a valve H.
Example two
In the present embodiment the first catalytic reactor 1 is in a regeneration mode of operation and the second catalytic reactor 2 is in a normal mode of operation.
Specifically, please refer to fig. 3, in which the valves in the circular dashed boxes are shown in a closed state, and the valves a, D, E, and H are closed in the embodiment.
As can be seen from the above, in this embodiment, the method for removing reducing gas based on the apparatus for removing reducing gas provided by the present invention includes:
a first mixed gas which is at normal temperature and contains 2% vol of hydrogen is pressurized to 8kPag by a first fan 3 and then is introduced into a first preheater 5; meanwhile, after a second mixed gas formed by mixing air and nitrogen is pressurized to 8kPag through a second fan 4, the second mixed gas enters the first catalytic reactor 1 through a valve B to perform oxidation regeneration on the catalyst in the first catalytic reactor 1, and the reacted reaction gas enters a second preheater 6 through a valve G;
in the first preheater 5, the first mixed gas is subjected to primary heat exchange with the reaction gas generated in the second catalytic reactor 2 under the normal operation mode, so that the first mixed gas is heated to 40 ℃ in a heat exchange manner; then the mixture enters a second preheater 6 through a corresponding connecting pipeline, and in the second preheater 6, the primarily heated first mixed gas and the reaction gas generated in the first catalytic reactor 1 under the regeneration operation mode are subjected to heat exchange again, so that the first mixed gas is heated to 80 ℃ in a heat exchange manner;
then, the reheated first mixed gas is introduced into the heater 7 through the corresponding connecting pipeline, so that the first mixed gas is finally heated to 110 ℃;
then, the finally heated first mixed gas enters the second catalytic reactor 2 through a valve C to perform a catalytic reduction reaction, and the reacted reaction gas enters the first preheater 5 through a valve F.
In conclusion, the method for removing the reducing gas provided by the invention can not only remove the reducing gas, but also realize the oxidation regeneration of the catalyst and the utilization of reaction preheating; in addition, the method has the advantages of flexible operation, low operation cost, high efficiency and high economy.
Although embodiments of the present invention have been shown and described, it will be appreciated by those skilled in the art that changes, modifications, substitutions and alterations can be made in these embodiments without departing from the principles and spirit of the invention, the scope of which is defined in the appended claims and their equivalents.
Claims (10)
1. An apparatus for removing a reducing gas, comprising:
the system comprises two catalytic reactors with switchable operation modes, wherein one of the two catalytic reactors is in a normal operation mode, the other one of the two catalytic reactors is in a regeneration operation mode, and the two catalytic reactors are respectively a first catalytic reactor and a second catalytic reactor;
the two fans are respectively a first fan and a second fan; the first fan is used for introducing a first mixed gas containing reducing gas into one catalytic reactor in a normal operation mode; the second fan is used for introducing a second mixed gas formed by mixing air and nitrogen into the other catalytic reactor in the regeneration operation mode;
the two preheaters are respectively a first preheater and a second preheater; the first preheater is connected between the first fan and the second preheater and is used for realizing preliminary heat exchange between reaction gas generated in one catalytic reactor in the normal operation mode and first mixed gas introduced by the first fan; the second preheater is connected to the gas outlet end of the first preheater and is used for realizing secondary heat exchange between the reaction gas generated in one catalytic reactor in the regeneration operation mode and the first mixed gas after the primary heat exchange;
the heater is connected to the gas outlet end of the second preheater and used for finally heating the first mixed gas after the secondary heat exchange and enabling the heated first mixed gas to enter a catalytic reactor in a normal operation mode;
a plurality of connecting lines and valves; the connecting pipes are used for being in conduction connection with the two catalytic reactors, the two fans, the two preheaters and the heater, the valves are respectively arranged on the corresponding connecting pipelines, and the switching between the normal operation mode and the regeneration operation mode of the catalytic reactors is realized through the opening and closing of the valves.
2. The apparatus for removing reducing gas according to claim 1, wherein: the preheater adopts a shell-and-tube heat exchanger or a plate heat exchanger.
3. The apparatus for removing reducing gas according to claim 1, wherein: the heater adopts an electric heater or a combustion type heater.
4. The apparatus for removing reducing gas according to claim 1, wherein: the first preheater preheats the first mixed gas to 40-500 ℃ initially, the second preheater preheats the first mixed gas to 80-500 ℃ again, and the heater heats the first mixed gas to 100-500 ℃.
5. The apparatus for removing reducing gas according to claim 1, wherein: the first mixed gas comprises hydrogen and/or CO, and the ratio of the hydrogen and/or the CO is 0.01-10 vol%.
6. The apparatus for removing reducing gas according to claim 1, wherein: the catalyst is a granular or regular structure catalyst.
7. The apparatus for removing reducing gas according to claim 6, wherein: the active component of the catalyst is one or a combination of more of transition metal oxides; or an alloy of a transition metal and a noble metal; or a noble metal supported on a transition metal oxide;
the transition metal comprises one or a combination of more of Co, Mn, Cu, Cr, Mo and Fe, and the precious metal comprises one or a combination of more of Pt, Pd and Rh.
8. The apparatus for removing reducing gas according to claim 1, wherein: in the catalytic reactor, the space velocity of the reactor is 1000-100000h-1The reaction temperature is 20-800 ℃.
9. The apparatus for removing reducing gas according to claim 1, wherein: when any catalytic reactor is in a regeneration operation mode, the regeneration gas adopts mixed gas of air and nitrogen; the regeneration temperature of the catalyst is 20-800 ℃, and the regeneration time is 1-24 h.
10. A method for removing reducing gas is characterized by comprising the following steps:
introducing a first mixed gas containing reducing gas into a first preheater for preliminary preheating;
introducing the primarily preheated first mixed gas into a second preheater for secondary preheating;
introducing the preheated first mixed gas into a heater for heating;
introducing the heated first mixed gas into a catalytic reactor which normally operates to perform a reduction catalytic reaction;
and introducing a second mixed gas formed by mixing air and nitrogen into the catalytic reactor in the regeneration operation to perform the oxidation regeneration reaction of the catalyst.
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