CN112283738B - Dry steam hydrogen-oxygen catalytic combustion system - Google Patents
Dry steam hydrogen-oxygen catalytic combustion system Download PDFInfo
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- CN112283738B CN112283738B CN202011027750.XA CN202011027750A CN112283738B CN 112283738 B CN112283738 B CN 112283738B CN 202011027750 A CN202011027750 A CN 202011027750A CN 112283738 B CN112283738 B CN 112283738B
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23L—SUPPLYING AIR OR NON-COMBUSTIBLE LIQUIDS OR GASES TO COMBUSTION APPARATUS IN GENERAL ; VALVES OR DAMPERS SPECIALLY ADAPTED FOR CONTROLLING AIR SUPPLY OR DRAUGHT IN COMBUSTION APPARATUS; INDUCING DRAUGHT IN COMBUSTION APPARATUS; TOPS FOR CHIMNEYS OR VENTILATING SHAFTS; TERMINALS FOR FLUES
- F23L7/00—Supplying non-combustible liquids or gases, other than air, to the fire, e.g. oxygen, steam
- F23L7/002—Supplying water
- F23L7/005—Evaporated water; Steam
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23D—BURNERS
- F23D14/00—Burners for combustion of a gas, e.g. of a gas stored under pressure as a liquid
- F23D14/02—Premix gas burners, i.e. in which gaseous fuel is mixed with combustion air upstream of the combustion zone
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23D—BURNERS
- F23D14/00—Burners for combustion of a gas, e.g. of a gas stored under pressure as a liquid
- F23D14/12—Radiant burners
- F23D14/18—Radiant burners using catalysis for flameless combustion
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23D—BURNERS
- F23D14/00—Burners for combustion of a gas, e.g. of a gas stored under pressure as a liquid
- F23D14/46—Details, e.g. noise reduction means
- F23D14/62—Mixing devices; Mixing tubes
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E20/00—Combustion technologies with mitigation potential
- Y02E20/32—Direct CO2 mitigation
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Abstract
The invention discloses a dry steam hydrogen-oxygen catalytic combustion system, which comprises a dry steam pure oxygen premixing subsystem, a mixed gas distribution subsystem, a catalytic combustion subsystem and a waste heat utilization subsystem, wherein the dry steam pure oxygen premixing subsystem is used for generating dry steam and premixing the dry steam with pure oxygen to form dry steam pure oxygen mixed gas, an outlet of the dry steam pure oxygen premixing subsystem is connected with the mixed gas distribution subsystem, and hydrogen and the dry steam pure oxygen are uniformly distributed by utilizing a coaxial rotational flow uniform distribution structure and then are conveyed to the catalytic combustion subsystem; the mixed gas is subjected to catalytic reaction in the catalytic combustion subsystem to release heat and generate high-temperature flue gas; the waste heat utilization subsystem is connected with the high-temperature flue gas outlet, and is used for preheating pure oxygen and hydrogen by utilizing the heat of the flue gas and recovering condensed water in the flue gas. The invention is used for catalytic combustion of hydrogen in pure oxygen, and dry steam as a thermal diluent can reduce the combustion rate of fuel in pure oxygen and adjust the temperature of a reaction bed layer, thereby greatly improving the safety of the high-purity reactor.
Description
Technical Field
The invention belongs to the field of pure oxygen catalytic combustion, and particularly relates to a dry steam oxyhydrogen catalytic combustion system which is used for safe and controllable combustion of pure oxygen.
Background
Pure oxygen combustion has a very high flame temperature compared to conventional combustion, which has an adiabatic combustion temperature of 1950 c, and a pure oxygen combustion temperature of 2500 c, which is very demanding on the burner and heat conversion device materials. Therefore, the pure oxygen combustion temperature needs to be reduced, which is very important for the material selection of the combustor and the safety guarantee of the system.
The pure oxygen catalytic combustion technology can realize the combustion of fuel at low temperature, and the flameless catalytic combustion mode has better safety and higher thermal efficiency due to the reduction of the combustion temperature. To further improve the safety of the system, water vapor is used as a diluent to regulate the reaction temperature.
However, studies have shown that the presence of water vapour adversely affects catalytic combustion, with conversion decreasing with increasing partial pressure of water vapour in the gas. The research shows that water vapor contained in the reaction gas and gaseous water generated in the reaction process can be condensed on the inner surface of the catalyst to form tiny water spots, so that the pore passages and part of active centers of the combustion-supporting gas are covered, and dry steam can not be adsorbed on the surface of the catalyst.
Therefore, the dry steam can be used as a thermal diluent to be added to perform reactivity control on the pure oxygen, and meanwhile, according to the reaction temperature, the adding amount of the dry steam can be increased or reduced strategically, so that the reaction temperature can be effectively adjusted, and the method has important significance for ensuring the safety of the pure oxygen catalytic combustion reaction.
Disclosure of Invention
Aiming at the improvement requirements of the prior art, the invention provides a dry steam hydrogen-oxygen catalytic combustion system, which can realize the safe and controllable combustion of hydrogen in pure oxygen, can simply and efficiently recover condensed water and is particularly suitable for use occasions without air sources.
The technical scheme adopted by the invention for solving the technical problems is as follows: a dry steam oxyhydrogen catalytic combustion system comprises a dry steam pure oxygen premixing subsystem, a mixed gas distribution subsystem connected with an outlet of the dry steam pure oxygen premixing subsystem, a catalytic combustion subsystem arranged at the downstream of the mixed gas distribution subsystem, and a waste heat utilization subsystem respectively connected with the dry steam pure oxygen premixing subsystem, the mixed gas distribution subsystem and the catalytic combustion subsystem; the dry steam pure oxygen premixing subsystem comprises a steam spray pipe with a double-layer sleeve structure and a steam nozzle connected with the steam spray pipe, wherein an inner pipe of the steam spray pipe is connected with an evaporation drying tank through a steam control valve, the inlet end of an outer-layer clamping pipe of the steam spray pipe is connected with a saturated steam inlet pipe and used for introducing external saturated steam, the outlet end of the outer-layer clamping pipe is connected with the evaporation drying tank and used for conveying the saturated steam to the evaporation drying tank for re-evaporation, the saturated steam is heated and insulated by using latent heat of the saturated steam through the inner pipe after being changed into dry steam and enters the steam nozzle, the steam nozzle is vertically connected with a pure oxygen inlet pipe, and the saturated steam treated into the dry steam and pure oxygen in a certain proportion are uniformly premixed by the steam nozzle and then are supplied to a mixed gas distribution subsystem; the mixed gas distribution subsystem is of a coaxial rotational flow uniform distribution structure and comprises a dry steam-pure oxygen inlet pipe connected with a steam nozzle and a hydrogen inlet pipe sleeved outside the dry steam-pure oxygen inlet pipe, hydrogen enters an outer annular channel hydrogen inlet pipe, dry steam-pure oxygen mixed gas enters an inner annular channel dry steam-pure oxygen inlet pipe, hydrogen-dry steam-pure oxygen outlets are connected to the outlets of the dry steam-pure oxygen inlet pipe and the hydrogen inlet pipe, and rotational flow blades are respectively arranged in the dry steam-pure oxygen inlet pipe and the hydrogen-dry steam-pure oxygen outlet to enable the flowing gas to form rotational flow; the catalytic combustion subsystem comprises a catalytic combustion reactor with a reaction gas inlet and a flue gas outlet, wherein the reaction gas inlet is connected with a hydrogen-dry steam-pure oxygen outlet, so that the injected hydrogen and dry steam-pure oxygen mixed gas perform catalytic combustion reaction, release a large amount of heat and generate high-temperature flue gas; the waste heat utilization subsystem mainly include the one-level condenser, the second grade condenser of being connected with the one-level condenser and the vapour and liquid separator who is connected with the second grade condenser, the one-level condenser advance the pipe with the pure oxygen respectively, hydrogen advances pipe and exhanst gas outlet connection for three kinds of working media to cold flow body hydrogen and pure oxygen and hot-fluid high temperature flue gas carry out the heat transfer, utilize high temperature flue gas waste heat to preheat hydrogen and pure oxygen, the second grade condenser further cools off the flue gas, make steam condensate water retrieve, still be provided with fuel gas import and pure oxygen import on the one-level condenser, still be provided with cooling water import and cooling water export on the second grade condenser, last tail gas export and the comdenstion water export of being provided with of vapour and liquid separator, a comdenstion water for retrieve the comdenstion water in the flue gas.
Wherein, the dry steam dryness of the steam entering the steam nozzle from the inner pipe of the steam nozzle is more than 95 percent.
Furthermore, the dry steam is reversely sprayed in the steam nozzle at an included angle of 100-120 degrees with the axial direction, and is uniformly premixed with the axially inflowing pure oxygen.
Furthermore, the steam nozzle is a porous stainless steel nozzle, and the aperture of the nozzle is 0.1-0.4 mm.
The dry steam hydrogen-oxygen catalytic combustion system is characterized in that the swirl blades comprise inner annular channel swirl blades and outer annular channel swirl blades, the rotation angle of the inner annular channel swirl blades is 15-45 degrees, and the rotation directions of the inner annular channel swirl blades and the outer annular channel swirl blades are opposite.
The catalytic combustion reactor of the dry steam hydrogen-oxygen catalytic combustion system is a cylindrical fixed bed reactor filled with catalyst, a plate reactor or other reactors.
The dry steam hydrogen-oxygen catalytic combustion system is characterized in that a reactor temperature sensor is arranged in a catalytic combustion reactor. The reactor temperature sensor measures the temperature of the reaction bed and is interlocked with the steam control valve, and the temperature of the reaction bed is adjusted by controlling the amount of dry steam.
The invention has the beneficial effects that:
according to the invention, the dry steam with the dryness of more than 95% is prepared by drying the saturated steam, and the dry steam is used as a thermal diluent and can not be adsorbed on the surface of the catalyst, so that the condensation of the water vapor generated by the reaction on the surface of the catalyst can be effectively inhibited to block the catalytic reaction, the combustion rate of the fuel in pure oxygen can be reduced, the temperature of a reaction bed layer can be adjusted, and the safety of the high-purity reactor can be greatly improved.
2, the invention can ensure the uniformity of the mixed gas by optimizing the blade angle of the cyclone uniform distributor to adjust the cyclone strength of the fuel and the dry steam-pure oxygen, thereby effectively ensuring the uniformity of the temperature field and the operation safety of the catalytic reactor.
3, the invention provides possibility for hydrogen to be used in occasions without air source, relying on pure oxygen and the like; particularly, hydrogen is catalytically combusted in dry steam pure oxygen to generate tail gas only containing water vapor, so that the tail gas treatment is very simple, and condensed water can be utilized after being recovered.
Drawings
FIG. 1 is a schematic diagram of the structural system of the present invention;
FIG. 2 is a schematic diagram of the dry steam pure oxygen premixing subsystem according to the present invention;
FIG. 3 is a schematic structural diagram of the mixed gas distribution subsystem of the present invention;
FIG. 4 is a left side view of the mixed gas distribution subsystem of the present invention;
FIG. 5 is a schematic structural diagram of a catalytic combustion subsystem of the present invention;
FIG. 6 is a schematic structural diagram of a waste heat utilization subsystem of the present invention;
FIG. 7 is a schematic material flow diagram of a hydrogen dry steam hydrogen-oxygen catalytic combustion system provided by the invention.
The figures are numbered: the system comprises a dry steam and pure oxygen premixing subsystem, a mixed gas distribution subsystem, a catalytic combustion subsystem, a residual heat utilization subsystem, a saturated steam inlet pipe, a steam evaporation drying tank, a steam control valve, a steam spray pipe, a 15 pure oxygen inlet pipe, a steam nozzle, a 21 hydrogen inlet pipe, a 22 dry steam and pure oxygen inlet pipe, a 23 hydrogen-dry steam and pure oxygen outlet, a 24 outer annular channel swirl vane, a 25 inner annular channel swirl vane, a 31 catalytic combustion reactor, a 32 reaction gas inlet, a 33 flue gas outlet, a 34 reactor temperature sensor, a 41 primary condenser, a 42 secondary condenser and a 43 gas-liquid separator.
Detailed Description
In order to make the technical solution of the present invention more apparent, the present invention is further described in detail with reference to the following drawings and examples.
As shown in figure 1, the invention provides a dry steam hydrogen-oxygen catalytic combustion system, which comprises a dry steam pure oxygen premixing subsystem 1, a mixed gas distribution subsystem 2, a catalytic combustion subsystem 3 and a waste heat utilization subsystem 4.
The mixed gas distribution subsystem 2 is connected with the outlet of the dry steam and pure oxygen premixing subsystem 1, and uniformly distributes the introduced hydrogen and the dry steam-pure oxygen mixed gas; the catalytic combustion subsystem 3 is arranged at the downstream of the mixed gas distribution subsystem 2, and performs catalytic combustion reaction by using injected hydrogen and dry steam-pure oxygen to release a large amount of heat and generate high-temperature flue gas; the waste heat utilization subsystem 4 preheats hydrogen and pure oxygen by using high-temperature flue gas generated by catalytic combustion, and recovers condensed water in the flue gas.
As shown in fig. 2, the dry steam pure oxygen premixing subsystem 1 includes a steam spray pipe 14 of a double-layer sleeve structure and a steam nozzle 16 connected with the steam spray pipe 14, an inner pipe of the steam spray pipe 14 is connected with an evaporation drying tank 12 through a steam control valve 13, an inlet end of an outer-layer clamping pipe of the steam spray pipe 14 is connected with a saturated steam inlet pipe 11, an outlet end of the outer-layer clamping pipe is connected with the evaporation drying tank 12, the steam nozzle 16 is vertically connected with a pure oxygen inlet pipe 15, saturated steam is provided from the outside, and pure oxygen with a certain proportion is supplied to the dry steam pure oxygen premixing subsystem 1 through the saturated steam inlet pipe 11 and the pure oxygen inlet pipe 15 respectively, and after the saturated steam is re-evaporated and dried by the evaporation drying tank 12, the dryness can reach more than 95%; dry steam passes through a steam spray pipe 14 which is a double-layer steam sleeve, saturated steam is arranged in an outer-layer clamping pipe, dry steam is arranged in an inner pipe, and the latent heat of the saturated steam is utilized for heating and heat preservation, so that the dryness of the steam in the inner pipe is effectively ensured, and condensation is avoided; wherein the steam nozzle 16 is a porous stainless steel nozzle, the aperture of the nozzle is 0.1-0.4 mm, dry steam is reversely sprayed in the steam nozzle 16 at an included angle of 100-120 degrees with the axial direction, and is uniformly premixed with axially inflowing pure oxygen.
As shown in fig. 3 and 4, the mixed gas distribution subsystem 2 is a coaxial rotational flow uniform distribution structure, and includes a dry steam-pure oxygen inlet pipe 22 connected to the steam nozzle 16 and a hydrogen inlet pipe 21 sleeved outside the dry steam-pure oxygen inlet pipe 22, the premixed dry steam and pure oxygen enter the mixed gas distribution subsystem 2 from the dry steam-pure oxygen inlet pipe 22, and simultaneously hydrogen enters the mixed gas distribution subsystem 2 from the hydrogen inlet pipe 21, the system is a coaxial rotational flow uniform distribution structure, hydrogen enters an outer annular passage, and a mixed gas of dry steam-pure oxygen enters an inner annular passage, both the inner and outer annular passages are provided with rotational flow blades, and gas forms rotational flow through the blades; the rotation angles of the outer annular channel swirl blades 24 and the inner annular channel swirl blades 25 are 15-45 degrees, and the rotation directions are opposite; the positive and negative two rotational flows form a backflow area at the 23 end of the hydrogen-dry steam-pure oxygen outlet so as to intensively mix the air flows; the swirling strength of the two air flows can be adjusted by selecting the rotating angle of the blades.
As shown in fig. 5, the catalytic combustion subsystem 3 is disposed downstream of the mixed gas distribution subsystem 2, and includes a catalytic combustion reactor 31 with a reaction gas inlet 32 and a flue gas outlet 33, and the mixed gas in the recirculation zone enters the catalytic combustion reactor 31 from the reaction gas inlet 32 to perform a low-temperature catalytic reaction, release a large amount of heat and generate high-temperature flue gas. The catalytic combustion reactor 31 is a cylindrical fixed bed reactor, a plate reactor or other type of reactor, and the reactor bed is filled with a catalyst.
The strategy of dry steam injection as a hot diluent is based on both reaction safety and bed temperature considerations. Therefore, on one hand, pure oxygen of the fuel gas and the combustion-supporting gas is strictly introduced into the catalytic combustion reactor 31 according to the stoichiometric ratio, but from the beginning of reaction safety, the fuel gas must be consumed cleanly, so the pure oxygen excess coefficient of the combustion-supporting gas can be 1.0-1.1; on the other hand, a temperature sensor 34 is arranged in the reaction bed layer for measuring the temperature of the reaction bed layer, and is interlocked with the steam control valve 13, and the bed layer temperature is fed back and adjusted by controlling the introduction amount of the dry steam;
as shown in fig. 6, the waste heat utilization subsystem 4 mainly includes a first-stage condenser 41, a second-stage condenser 42 connected to the first-stage condenser 41, and a gas-liquid separator 43 connected to the second-stage condenser 42, the primary condenser 41 is respectively connected with the pure oxygen inlet pipe 15, the hydrogen inlet pipe 21 and the flue gas outlet 33, high-temperature flue gas generated by catalytic combustion reaction is discharged from the flue gas outlet 33 and enters the waste heat utilization subsystem 4, firstly, heat exchange is carried out on three working media through a primary condenser 41, cold fluid is hydrogen and pure oxygen, hot fluid is catalytic combustion high-temperature flue gas, the hydrogen and the pure oxygen are preheated by utilizing the waste heat of the high-temperature flue gas so as to improve the heat utilization rate of the system, the high-temperature flue gas after primary condensation enters a secondary condenser 42 for further condensation, at the moment, water vapor in the flue gas is condensed into liquid water, and then condensed water is separated from combustion tail gas in the flue gas through a gas-liquid separator 43; the flue gas generated after the hydrogen fuel is catalytically combusted according to the stoichiometric ratio only contains water vapor, and the water vapor is condensed and then recovered, so that real zero emission is realized.
The first-stage condenser 41 is also provided with a fuel gas inlet and a pure oxygen inlet, the second-stage condenser 42 is also provided with a cooling water inlet and a cooling water outlet, and the gas-liquid separator 43 is provided with a tail gas outlet and a condensed water outlet for recovering condensed water in the flue gas.
The invention is used for catalytic combustion of hydrogen in pure oxygen, and dry steam as a thermal diluent can reduce the combustion rate of fuel in pure oxygen and adjust the temperature of a reaction bed layer, thereby greatly improving the safety of the high-purity reactor; meanwhile, the swirl strength of the fuel and the dry steam-pure oxygen is adjusted by optimizing the angle of the blades of the swirl equipartition device, so that the uniformity of mixed gas can be ensured, and the uniformity of a temperature field and the operation safety of the catalytic reactor can be effectively guaranteed; the invention provides possibility for using hydrogen in occasions without air source, relying on pure oxygen and the like, only water vapor is generated in tail gas generated by hydrogen-oxygen catalytic combustion, so that the tail gas treatment is very simple, and condensed water can be utilized after being recovered.
The dry steam hydrogen-oxygen catalytic combustion system provided by the invention is further explained by taking hydrogen as a working condition of fuel gas. Pure oxygen is very reactive and requires dilution with dry steam for safety reasons, in the following examples dry steam and pure oxygen are diluted in a ratio of nitrogen to oxygen to produce air-like reactive properties.
As shown in fig. 7, saturated steam with a volume fraction of 80% is provided from the outside, and pure oxygen with a volume fraction of 20% is supplied to the dry steam and pure oxygen premixing subsystem 1 through the saturated steam inlet pipe 11 and the pure oxygen inlet pipe 15, respectively, the saturated steam firstly moves in the outer-layer pipe clamp of the steam nozzle 14 along the axial direction, and the latent heat is used for heating and insulating the inner pipe, so as to ensure the dryness of the steam in the inner pipe; after the axial flow is turned back, the mixture enters an evaporation drying tank 12 for re-evaporation and drying treatment, and the dryness can reach more than 95 percent; the amount of dry steam entering a nozzle is automatically controlled through a steam control valve 13, and after the dry steam enters a steam nozzle 16, the dry steam is reversely sprayed at an included angle of 100-120 degrees with the axial direction and is uniformly premixed with axially inflowing pure oxygen; after premixing, dry steam pure oxygen enters an inner annular channel of a coaxial rotational flow uniform distribution structure of the mixed gas distribution subsystem 2 from a dry steam-pure oxygen inlet pipe 22, meanwhile, hydrogen with stoichiometric ratio enters an outer annular channel of the coaxial rotational flow uniform distribution structure of the mixed gas distribution subsystem 2 from a hydrogen inlet pipe 21, the rotating angle of a rotational flow blade 24 of the outer annular channel forms 30 degrees with the axial direction, the outer annular channel rotates clockwise, the rotating angle of a rotational flow blade 25 of the inner annular channel forms 30 degrees with the axial direction, the inner annular channel rotates anticlockwise, the inner annular channel and the axial direction form strong mixed flow, positive and negative rotational flows form a backflow area at the hydrogen-dry steam-pure oxygen outlet 23 end, and air flows are mixed strongly. The mixed gas in the reflux zone enters the catalytic combustion reactor 31 from the reaction gas inlet 32 to perform low-temperature catalytic reaction, a large amount of heat is released, high-temperature flue gas is generated, and at the moment, dry steam is used as a thermal diluent to adjust the temperature of a bed layer; the reaction bed layer is provided with a temperature sensor 34 for measuring the temperature of the reaction bed layer, and the temperature sensor is interlocked with the steam control valve 13 to feed back and adjust the temperature of the bed layer by controlling the introduction amount of dry steam. The hydrogen and the oxygen in the catalytic combustion reaction completely react according to the stoichiometric ratio, and the only reaction product, namely high-temperature water vapor, is discharged through the flue gas outlet 33 and enters the waste heat utilization subsystem 4. Firstly, the cold fluid is hydrogen and pure oxygen, the hot fluid is catalytic combustion high-temperature steam, and the hydrogen and the pure oxygen are preheated by utilizing the waste heat of the high-temperature steam so as to improve the heat utilization rate of the system after passing through the primary condenser 41. The water vapor after the first-stage condensation enters a second-stage condenser 42 for further condensation, the water vapor is condensed into liquid water at the moment, and the condensed water is recovered through a gas-liquid separator 43, so that real zero emission is realized.
It will be understood by those skilled in the art that the foregoing is only a preferred embodiment of the present invention, and is not intended to limit the invention, and that any modification, equivalent replacement, or improvement made within the spirit and principle of the present invention should be included in the scope of the present invention.
Claims (7)
1. A dry steam hydrogen-oxygen catalytic combustion system is characterized in that: the system comprises a dry steam and pure oxygen premixing subsystem (1), a mixed gas distribution subsystem (2) connected with the outlet of the dry steam and pure oxygen premixing subsystem (1), a catalytic combustion subsystem (3) arranged at the downstream of the mixed gas distribution subsystem (2), and a waste heat utilization subsystem (4) respectively connected with the dry steam and pure oxygen premixing subsystem (1), the mixed gas distribution subsystem (2) and the catalytic combustion subsystem (3);
the dry steam and pure oxygen premixing subsystem (1) comprises a steam spray pipe (14) with a double-layer sleeve structure and a steam nozzle (16) connected with the steam spray pipe (14), wherein an inner pipe of the steam spray pipe (14) is connected with an evaporation drying tank (12) through a steam control valve (13), the inlet end of an outer pipe of the steam spray pipe (14) is connected with a saturated steam inlet pipe (11) for introducing external saturated steam, the outlet end of the outer pipe is connected with the evaporation drying tank (12) for sending the saturated steam to the evaporation drying tank (12) for re-evaporation, the saturated steam is changed into dry steam and then enters the steam nozzle (16) through the inner pipe, the steam nozzle (16) is vertically connected with a pure oxygen inlet pipe (15), and the steam nozzle (16) uniformly pre-mixes the dry steam and the pure oxygen and then supplies the dry steam to the mixed gas distribution subsystem (2);
the mixed gas distribution subsystem (2) comprises a dry steam-pure oxygen inlet pipe (22) connected with a steam nozzle (16) and a hydrogen inlet pipe (21) sleeved outside the dry steam-pure oxygen inlet pipe (22), the outlets of the dry steam-pure oxygen inlet pipe (22) and the hydrogen inlet pipe (21) are connected with a hydrogen-dry steam-pure oxygen outlet (23), and swirl blades are respectively arranged in the dry steam-pure oxygen inlet pipe (22) and the hydrogen-dry steam-pure oxygen outlet (23) to enable the flowing gas to form swirl;
the catalytic combustion subsystem (3) comprises a catalytic combustion reactor (31) with a reaction gas inlet (32) and a flue gas outlet (33), wherein the reaction gas inlet (32) is connected with a hydrogen-dry steam-pure oxygen outlet (23) so that hydrogen and dry steam-pure oxygen mixed gas perform catalytic combustion reaction, heat is released, and high-temperature flue gas is generated;
waste heat utilization subsystem (4) include one-level condenser (41), second grade condenser (42) be connected with one-level condenser (41) and vapour and liquid separator (43) be connected with second grade condenser (42), one-level condenser (41) advance pipe (15), hydrogen respectively with the pure oxygen, advance pipe (21) and exhanst gas outlet (33) and be connected for carry out the heat exchanger to hydrogen and pure oxygen and high temperature flue gas, second grade condenser (42) further cools off the flue gas, still be provided with fuel gas import and pure oxygen import on one-level condenser (41), still be provided with cooling water import and cooling water outlet on second grade condenser (42), be provided with tail gas outlet and comdenstion water export on vapour and liquid separator (43) for retrieve the comdenstion water in the flue gas.
2. The dry steam hydrogen-oxygen catalytic combustion system according to the claim 1, characterized in that the dry steam is reversely injected in the steam nozzle (16) at an angle of 100-120 ° with the axial direction.
3. The dry steam hydrogen-oxygen catalytic combustion system according to claim 1, wherein the steam nozzle (16) is a porous stainless steel nozzle with a diameter of 0.1-0.4 mm.
4. The dry steam hydrogen-oxygen catalytic combustion system as claimed in claim 1, wherein the swirl vanes comprise inner annular passage swirl vanes (25) and outer annular passage swirl vanes (24) which rotate at an angle of 15-45 ° in opposite directions.
5. A dry steam oxyhydrogen catalytic combustion system according to claim 1, characterized in that the catalytic combustion reactor (31) is a cylindrical fixed bed reaction or a plate reactor filled with catalyst.
6. A dry steam oxyhydrogen catalytic combustion system according to claim 1, characterized in that a reactor temperature sensor (34) is arranged in the catalytic combustion reactor (31).
7. A dry steam hydrogen and oxygen catalytic combustion system according to claim 6, characterized in that the reactor temperature sensor (34) is interlocked with the steam control valve (13) to control the amount of dry steam to regulate the temperature of the reaction bed.
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| CN108603658A (en) * | 2016-03-15 | 2018-09-28 | 杰伊·凯勒 | Non- premixed swirl burner end and combustion strategies |
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| US10994254B2 (en) * | 2017-03-17 | 2021-05-04 | Rasirc, Inc. | System, device, and method for controlling mass flow of a catalytically reactive gas in a mixed gas stream |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH10232297A (en) * | 1997-02-19 | 1998-09-02 | Toshiba Corp | Recombination treating method for combustible gas and its gas waste disposal facility |
| JP2003214768A (en) * | 2002-01-23 | 2003-07-30 | Stm:Kk | Thermal treatment equipment using superheated steam |
| CN201439954U (en) * | 2009-08-13 | 2010-04-21 | 上海凯鸿环保工程有限公司 | Steam combustion-supporting torch burner |
| CN108603658A (en) * | 2016-03-15 | 2018-09-28 | 杰伊·凯勒 | Non- premixed swirl burner end and combustion strategies |
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