CN111256485A - Sectional type flue heat utilization device and method for hydrogen production from natural gas - Google Patents
Sectional type flue heat utilization device and method for hydrogen production from natural gas Download PDFInfo
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- CN111256485A CN111256485A CN202010207174.0A CN202010207174A CN111256485A CN 111256485 A CN111256485 A CN 111256485A CN 202010207174 A CN202010207174 A CN 202010207174A CN 111256485 A CN111256485 A CN 111256485A
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F27—FURNACES; KILNS; OVENS; RETORTS
- F27D—DETAILS OR ACCESSORIES OF FURNACES, KILNS, OVENS, OR RETORTS, IN SO FAR AS THEY ARE OF KINDS OCCURRING IN MORE THAN ONE KIND OF FURNACE
- F27D17/00—Arrangements for using waste heat; Arrangements for using, or disposing of, waste gases
- F27D17/004—Systems for reclaiming waste heat
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
- C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
- C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
- C01B3/34—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
- C01B3/38—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using catalysts
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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
- F23D14/46—Details, e.g. noise reduction means
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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
- F23D14/66—Preheating the combustion air or gas
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/02—Processes for making hydrogen or synthesis gas
- C01B2203/0205—Processes for making hydrogen or synthesis gas containing a reforming step
- C01B2203/0227—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step
- C01B2203/0233—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step the reforming step being a steam reforming step
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- 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
- Y02E20/34—Indirect CO2mitigation, i.e. by acting on non CO2directly related matters of the process, e.g. pre-heating or heat recovery
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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
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P10/00—Technologies related to metal processing
- Y02P10/10—Reduction of greenhouse gas [GHG] emissions
- Y02P10/143—Reduction of greenhouse gas [GHG] emissions of methane [CH4]
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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
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P10/00—Technologies related to metal processing
- Y02P10/25—Process efficiency
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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
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
- Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
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Abstract
The invention discloses a sectional flue heat utilization device and method for natural gas hydrogen production, and relates to the field of natural gas hydrogen production, wherein the device comprises a mixed gas preheater, a first natural gas preheater, a second natural gas preheater, a flue gas waste boiler, a burner, an air preheater, an induced draft fan and a chimney, and the method comprises the steps that S1 high-temperature flue gas is subjected to heat exchange through the mixed gas preheater, S2 flue gas is subjected to heat exchange through the first natural gas preheater, S3 flue gas is heated through the burner, S4 flue gas is subjected to heat exchange through the flue gas waste boiler, S5 flue gas is subjected to heat exchange through the second natural gas preheater, S5 flue gas is subjected to heat exchange; the flue gas cools the high-temperature flue gas to a temperature slightly higher than the dew point after a series of heat exchanges, so that the dew point corrosion of the flue gas is prevented, the heat is fully recycled, and the air enters a combustor for combustion after being preheated by an air preheater, so that the consumption of natural gas fuel is reduced; the burner is used to regulate the exhaust gas temperature and rich steam production.
Description
Technical Field
The invention relates to the field of hydrogen production by natural gas, in particular to a sectional type flue heat utilization device and method for hydrogen production by natural gas.
Background
The natural gas hydrogen production technology is a mature hydrogen production method, under the hot tide of hydrogen energy utilization at present, the natural gas hydrogen production technology has the advantages of low cost, obvious scale effect and the like, the research and development of a more advanced new natural gas hydrogen production technology is an important guarantee for solving a cheap hydrogen source, and is also an inevitable choice for long-term development of a natural gas hydrogen production device, but the natural gas hydrogen production device is a device with surplus capacity, rich steam is generated during normal production, for small devices, the rich steam is generally used for removing oxygen from acid water in the device, and the rich steam generated by a large device needs to be balanced with steam of a whole plant due to too large amount.
Disclosure of Invention
The invention aims to solve the problems and designs a sectional flue heat utilization device and a method for hydrogen production from natural gas.
The invention realizes the purpose through the following technical scheme:
a sectional flue heat utilization device for hydrogen production from natural gas, high-temperature flue gas enters a flue from a converter for hydrogen production from natural gas, and the device comprises:
a mixed gas preheater; the gas outlet of the mixed gas preheater is communicated with the gas inlet of a conversion pipe in the converter;
a first natural gas preheater; a natural gas outlet of the first natural gas preheater is communicated with a gas inlet of the mixed gas preheater;
a second natural gas preheater; a natural gas outlet of the second natural gas preheater is communicated with a natural gas inlet of the first natural gas preheater;
waste flue gas boiler; the steam outlet of the flue gas waste boiler is communicated with the air inlet of the mixed gas preheater;
the combustor is used for heating the flue gas flowing to the flue gas waste boiler by the reforming furnace;
the air outlet of the air preheater is communicated with the air inlet of the combustor;
the air inlet of the induced draft fan is communicated with the flue, and the air outlet of the induced draft fan is communicated with the air inlet of the combustor;
the air inlet of the chimney is communicated with the air outlet of the induced draft fan; the high-temperature flue gas enters the flue, then sequentially passes through the mixed gas preheater, the first natural gas preheater, the burner, the flue gas waste boiler, the second natural gas preheater and the air preheater, and finally is discharged through the draught fan and the chimney.
Further, the combustor comprises a plurality of combustion heads distributed annularly, and the direction of the combustion heads is perpendicular to the flowing direction of the flue gas.
Further, the combustor still includes installation room, support piece and gas mixing chamber, and gas mixing chamber and flue are all through support piece fixed mounting in the installation room, and the flue setting is in the gas mixing chamber, and the burner ring is installed in the flue, and the gas import and the gas mixing chamber intercommunication of burner, the burner all towards the central axis of flue in the direction of burning, and the support piece intussuseption is filled with refractory castable.
Further, the combustor still includes fuel gas inlet pipe and sleeve pipe, and the fuel gas inlet pipe sets up in the sleeve pipe, sheathed tube air inlet respectively with air heater's air outlet and the gas outlet intercommunication of draught fan, the gas outlet of fuel gas inlet pipe and sheathed tube gas outlet all communicate with the gas mixing chamber, the ignition end setting of the burning torch of combustor is inside the gas mixing chamber.
Furthermore, the conversion pipe on the conversion furnace comprises a flexible element for keeping the sealing performance between the conversion pipe and the interior of the furnace body of the conversion furnace, the lower end of the flexible element is fixedly connected with a pipe orifice which is arranged at the top of the furnace body and used for penetrating through the conversion pipe, the lower end of the conversion pipe is fixedly arranged at the bottom of the furnace body, the upper end of the conversion pipe sequentially penetrates through the pipe orifice at the top of the furnace body and the flexible element, and the upper end of the conversion pipe is fixedly connected with an upper pigtail pipe joint.
Furthermore, the flexible element is an expansion joint, the lower end of the expansion joint is fixedly connected with a pipe orifice at the top of the furnace body, the upper end of the conversion pipe sequentially penetrates through the pipe orifice at the top of the furnace and the expansion joint, and high-temperature ceramic fiber blankets are filled in the expansion joint.
A heat utilization method for a natural gas hydrogen production sectional type flue comprises the following steps:
s1, after entering a flue, the high-temperature flue gas from the reformer exchanges heat with natural gas and steam for the first time through a mixed gas preheater, and after the temperature of the natural gas and the steam is raised, the high-temperature flue gas enters a reformer tube;
s2, performing secondary heat exchange on the flue gas subjected to the primary heat exchange and the natural gas through a first natural gas preheater, and heating the natural gas to enter an air inlet of a mixed gas preheater;
s3, heating the flue gas subjected to the second heat exchange by a burner;
s4, carrying out third heat exchange on the heated flue gas and water through the flue gas waste boiler, and enabling steam generated by the flue gas waste boiler to enter an air inlet of the mixed gas preheater;
s5, performing fourth heat exchange on the flue gas subjected to the third heat exchange with natural gas through a second natural gas preheater, and heating the natural gas to enter a natural gas inlet of the first natural gas preheater;
and (3) finally carrying out the last heat exchange on the flue gas subjected to the S5 and the fourth heat exchange with air through an air preheater, wherein the temperature after cooling is slightly higher than the dew point temperature, and finally, the flue gas subjected to cooling is extracted through an induced draft fan, wherein most of the flue gas is discharged through a chimney, and the other part of the flue gas and the air inlet of the sleeve in the combustor are communicated.
Further, in S1, the temperature range of the flue gas after the first heat exchange is 560-600 ℃, and the temperature range of the natural gas and the steam is 560-600 ℃; in S2, the temperature range of the flue gas after the second heat exchange is 360-400 ℃, and the temperature range of the natural gas is 320-360 ℃; in S4, the temperature range of the flue gas after the third heat exchange is 200-240 ℃, and in S5, the temperature range of the flue gas after the fourth heat exchange is 160-200 ℃.
The invention has the beneficial effects that: the high-temperature flue gas from the reformer is cooled to a temperature slightly higher than the dew point temperature through the mixed gas preheater, the second natural gas preheater, the flue gas waste boiler, the first natural gas preheater and the air preheater, so that the dew point corrosion of the flue gas is prevented, meanwhile, the heat is fully recycled, the air is preheated by the air preheater and then enters the combustor for combustion, the consumption of natural gas fuel is reduced, and the consumption of a natural gas hydrogen production device reaches 0.391; through the combustor, the regulation and control of exhaust gas temperature and rich steam production quantity is realized, when the natural gas hydrogen production device is in initial operation, the combustor is opened, the waste flue gas boiler generates steam 6 hours faster than the combustor in the initial operation stage, the initial reduction time is greatly advanced, the catalyst is switched from nitrogen heating to steam heating in advance, the nitrogen heating time of the catalyst is shortened, the service life of the catalyst is prolonged, when the device is in normal operation, the flue auxiliary combustor provides heat, the steam quantity of the device byproduct is increased, the whole steam balance of the device is more facilitated, the increased steam can be used for heating tap water for use, the original coal-fired boiler is cancelled, the whole energy consumption is saved, and the environment is protected.
Drawings
FIG. 1 is a schematic structural diagram of a sectional flue heat utilization device for hydrogen production from natural gas according to the invention;
FIG. 2 is a schematic structural diagram of a burner in the sectional flue heat utilization device for hydrogen production from natural gas of the invention;
FIG. 3 is a schematic structural diagram of a conversion pipe in the sectional flue heat utilization device for hydrogen production from natural gas according to the present invention;
FIG. 4 is a schematic flow diagram of a sectional flue heat utilization method for hydrogen production from natural gas according to the present invention;
wherein corresponding reference numerals are:
1-installation chamber, 2-gas mixing chamber, 3-air outlet, 4-ignition gun, 5-fuel gas feeding pipe, 6-air outlet of induced draft fan, 7-refractory casting material, 8-supporting piece, 9-reformer, 10-flue gas waste pot, 11-mixed gas preheater, 12-first natural gas preheater, 13-burner, 14-air preheater, 15-second natural gas preheater, 16-induced draft fan, 17-chimney, 18-reformer, 19-expansion joint, 20-furnace body bottom, 21-furnace body top, 22-high temperature ceramic fiber blanket, 23-upper pigtail pipe joint.
Detailed Description
In order to make the objects, technical solutions and advantages of the embodiments of the present invention clearer, 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. It is to be understood that the embodiments described are only a few embodiments of the present invention, and not all embodiments. The components of embodiments of the present invention generally described and illustrated in the figures herein may be arranged and designed in a wide variety of different configurations.
Thus, the following detailed description of the embodiments of the present invention, presented in the figures, is not intended to limit the scope of the invention, as claimed, but is merely representative of selected embodiments of the invention. 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.
It should be noted that: like reference numbers and letters refer to like items in the following figures, and thus, once an item is defined in one figure, it need not be further defined and explained in subsequent figures.
In the description of the present invention, it is to be understood that the terms "upper", "lower", "inside", "outside", "left", "right", and the like, indicate orientations or positional relationships based on the orientations or positional relationships shown in the drawings, or the orientations or positional relationships that the products of the present invention are conventionally placed in use, or the orientations or positional relationships that are conventionally understood by those skilled in the art, and are used for convenience of describing the present invention and simplifying the description, but do not indicate or imply that the devices or elements referred to must have a specific orientation, be constructed in a specific orientation, and be operated, and thus, should not be construed as limiting the present invention.
Furthermore, the terms "first," "second," and the like are used merely to distinguish one description from another, and are not to be construed as indicating or implying relative importance.
In the description of the present invention, it is also to be noted that, unless otherwise explicitly stated or limited, the terms "disposed" and "connected" are to be interpreted broadly, and for example, "connected" may be a fixed connection, a detachable connection, or an integral connection; can be mechanically or electrically connected; the connection may be direct or indirect via an intermediate medium, and may be a communication between the two elements. The specific meanings of the above terms in the present invention can be understood by those skilled in the art according to specific situations.
The following detailed description of embodiments of the invention refers to the accompanying drawings.
As shown in fig. 1, a sectional flue heat utilization device for hydrogen production from natural gas, in which high-temperature flue gas enters a flue from a reformer 9 for hydrogen production from natural gas, includes:
a mixed gas preheater 11; the gas outlet of the mixed gas preheater 11 is communicated with the gas inlet of a conversion pipe 18 in the converter 9;
a first natural gas preheater 12; a natural gas outlet of the first natural gas preheater 12 is communicated with a gas inlet of the mixed gas preheater 11;
a second natural gas preheater 15; a natural gas outlet of the second natural gas preheater 15 is communicated with a natural gas inlet of the first natural gas preheater 12;
a flue gas waste boiler 10; a steam outlet of the flue gas waste boiler 10 is communicated with an air inlet of the mixed gas preheater 11;
a burner 13 for heating the flue gas flowing from the reformer 9 to the flue gas waste boiler 10;
the air outlet 3 of the air preheater 14 is communicated with the air inlet of the combustor 13;
the air inlet of the draught fan 16 is communicated with the flue, and the air outlet 6 of the draught fan 16 is communicated with the air inlet of the combustor 13;
the air inlet of the chimney 17 is communicated with the air outlet 6 of the induced draft fan 16; the high-temperature flue gas enters the flue, then sequentially passes through the mixed gas preheater 11, the first natural gas preheater 12, the combustor 13, the flue gas waste boiler 10, the second natural gas preheater 15 and the air preheater 14, and finally is discharged through the induced draft fan 16 and the chimney 17.
As shown in fig. 2, the burner 13 comprises a plurality of burner heads distributed annularly, the direction of the burner heads being perpendicular to the flow direction of the flue gas.
As shown in fig. 2, the combustor 13 further includes an installation chamber 1, a support member 8 and a gas mixing chamber, the gas mixing chamber and the flue are both fixedly installed in the installation chamber 1 through the support member 8, the flue is arranged in the gas mixing chamber, the burner is annularly installed in the flue, a gas inlet of the burner is communicated with the gas mixing chamber, the burning direction of the burner is towards the central axis of the flue, and the support member 8 is filled with a refractory castable.
As shown in fig. 2, the burner 13 further comprises a fuel gas feeding pipe 5 and a sleeve, the fuel gas feeding pipe 5 is arranged in the sleeve, an air inlet of the sleeve is respectively communicated with an air outlet 3 of the air preheater 14 and an air outlet 6 of the induced draft fan 16, an air outlet of the fuel gas feeding pipe 5 and an air outlet of the sleeve are both communicated with the gas mixing chamber, and a firing end of a firing gun 4 of the burner 13 is arranged inside the gas mixing chamber.
The air is preheated by the air preheater 14 and then enters the combustor 13 for air distribution and combustion, so that the consumption of natural gas fuel is reduced, and the consumption of the natural gas hydrogen production device reaches 0.391.
The effect of the combustor 13 can be used for solving the steam balance of the whole natural gas hydrogen production device, and meanwhile, part of low-temperature flue gas and air are mixed and fed into the gas mixing cavity through the draught fan 16, so that the combustion speed and the temperature in the furnace are reduced due to the fact that the flue gas absorbs heat and dilutes the oxygen concentration, the thermal NOx is reduced, the thermal NOx can be reduced by 30-50%, and the natural gas hydrogen production device is more energy-saving and environment-friendly.
When the hydrogen production equipment is initially started, the combustor 13 is opened, the combustion head burns and heats the flue gas in the flue gas channel, the flue gas is heated, the high-temperature flue gas exchanges heat with the flue gas waste boiler 10, the steam yield and the steam production speed of the device are improved, the initial running time of the device can be reduced during initial running, the steam passivation time of the catalyst is reduced, the service life of the catalyst is prolonged, the self yield of the steam can be greatly increased, and the purpose of heating the self-produced steam is achieved; when the natural gas hydrogen production equipment normally operates, the combustor 13 provides heat, the amount of byproduct steam of the natural gas hydrogen production equipment is increased, the whole steam balance of the device is facilitated, and whether the combustor 13 is continuously used for combusting and heating smoke can be selected according to actual steam demand conditions when the natural gas hydrogen production equipment normally operates.
Because the burning head of combustor 13 is towards the axial axis direction of flue gas passageway, flame is short when such combustor 13 burns, and the rigidity is strong, under the circumstances of guaranteeing the utilization of flue gas heat, flame can not contact flue gas waste boiler 10 heat exchange tube, causes flue gas waste boiler 10 to damage.
When the device normally operates, the combustor 13 provides heat, the amount of byproduct steam is increased, the whole steam balance of the device is more facilitated, the increased steam can be used for heating tap water for use, an original coal-fired boiler is omitted, the whole energy consumption is saved, and the environment is protected.
As shown in fig. 3, the reformer tube 18 of the reformer 9 includes a flexible element for maintaining the sealing performance between the reformer tube 18 and the interior of the reformer body of the reformer 9, the lower end of the flexible element is fixedly connected with the nozzle of the top 21 of the reformer body for passing through the reformer tube 18, the lower ends of the reformer tubes 18 are all fixedly mounted at the bottom of the reformer body, the upper end of the reformer tube 18 sequentially passes through the nozzle of the top 21 of the reformer body and the flexible element, and the upper end of the reformer tube 18 is fixedly connected with the upper pigtail connector 23.
As shown in FIG. 3, the flexible element is an expansion joint 19, the lower end of the expansion joint 19 is fixedly connected with a nozzle at the top 21 of the furnace body, the upper end of the conversion pipe 18 sequentially passes through the nozzle at the top of the furnace and the expansion joint 19, and the expansion joint 19 is filled with high-temperature ceramic fiber blankets 22.
When the conversion tube 18 is installed, the conversion tube 18 is pre-stretched and fixed downwards, the conversion tube 18 is fixedly connected with the bottom 20 of the furnace body of the conversion furnace 9 by adopting a fixed flange, the upper end of the conversion tube 18 sequentially penetrates through a tube opening at the top 21 of the furnace body of the conversion furnace 9 and an expansion joint 19 from bottom to top, the upper end of the conversion tube 18 is fixedly connected with an upper pigtail joint 23, the expansion joint 19 is pre-compressed when being installed, the pre-compression amount of the expansion joint is larger than the maximum variation amount of the conversion tube 18, a high-temperature ceramic fiber blanket 22 is filled in the expansion joint 19, the expansion joint 19 can effectively solve the problems of expansion caused by heat and contraction caused by cold of the conversion tube 18, meanwhile, the sealing problem between the conversion furnace 9 and the conversion tube 18 can be effectively ensured by combining the expansion joint 19 and the high-temperature ceramic fiber blanket 22, meanwhile, the high-temperature ceramic fiber blanket 22 also has the heat preservation function, the energy consumption is increased, and meanwhile, the expansion joint 19 can be fixed at the top 21 of the converter body of the converter 9 only by the flange, so that a large number of steel structures are effectively avoided, and the operation space on the top of the converter 9 is greatly liberated.
As shown in fig. 4, a method for utilizing heat of a natural gas hydrogen production segmented flue comprises the following steps:
s1, after entering a flue, the high-temperature flue gas from the reformer 9 exchanges heat with natural gas and steam for the first time through the mixed gas preheater 11, the temperature of the flue gas is reduced to 560-600 ℃, and the temperature of the natural gas and the steam is increased to 560-600 ℃ and then enters the reformer tube 18;
s2, performing secondary heat exchange on the flue gas subjected to the primary heat exchange and the natural gas through the first natural gas preheater 12, reducing the temperature of the flue gas to 360-400 ℃, heating the natural gas to 320-360 ℃, and then feeding the natural gas into an air inlet of the mixed gas preheater 11;
s3, heating the flue gas subjected to the second heat exchange by the combustor 13;
s4, carrying out third heat exchange on the heated flue gas and water through the flue gas waste boiler 10, reducing the temperature of the flue gas to 200-240 ℃, and enabling steam generated by the flue gas waste boiler 10 to enter an air inlet of the mixed gas preheater 11;
s5, performing fourth heat exchange on the flue gas subjected to the third heat exchange with the natural gas through a second natural gas preheater 15, reducing the temperature of the flue gas to 160-200 ℃, and heating the natural gas to enter a natural gas inlet of the first natural gas preheater 12;
and S6, performing the last heat exchange between the flue gas subjected to the fourth heat exchange and the air through the air preheater 14, wherein the temperature after the temperature reduction is slightly higher than the dew point temperature, and finally extracting the cooled flue gas through the induced draft fan 16, wherein most of the flue gas is discharged through the chimney 17, and the other part of the flue gas enters the air inlet of the middle sleeve of the combustor 13.
The technical solution of the present invention is not limited to the limitations of the above specific embodiments, and all technical modifications made according to the technical solution of the present invention fall within the protection scope of the present invention.
Claims (8)
1. A natural gas hydrogen production sectional type flue heat utilization device, high temperature flue gas gets into the flue from the reborner that is used for natural gas hydrogen production, its characterized in that includes:
a mixed gas preheater; the gas outlet of the mixed gas preheater is communicated with the gas inlet of a conversion pipe in the converter;
a first natural gas preheater; a natural gas outlet of the first natural gas preheater is communicated with a gas inlet of the mixed gas preheater;
a second natural gas preheater; a natural gas outlet of the second natural gas preheater is communicated with a natural gas inlet of the first natural gas preheater;
waste flue gas boiler; the steam outlet of the flue gas waste boiler is communicated with the air inlet of the mixed gas preheater;
the combustor is used for heating the flue gas flowing to the flue gas waste boiler by the reforming furnace;
the air outlet of the air preheater is communicated with the air inlet of the combustor;
the air inlet of the induced draft fan is communicated with the flue, and the air outlet of the induced draft fan is communicated with the air inlet of the combustor;
the air inlet of the chimney is communicated with the air outlet of the induced draft fan; the high-temperature flue gas enters the flue, then sequentially passes through the mixed gas preheater, the first natural gas preheater, the burner, the flue gas waste boiler, the second natural gas preheater and the air preheater, and finally is discharged through the draught fan and the chimney.
2. The segmented flue heat utilization device for hydrogen production from natural gas as claimed in claim 1, wherein the burner comprises a plurality of annularly distributed combustion heads, and the direction of the combustion heads is perpendicular to the flow direction of the flue gas.
3. The sectional flue heat utilization device for hydrogen production from natural gas as claimed in claim 2, wherein the burner further comprises an installation chamber, a support member and a gas mixing chamber, the gas mixing chamber and the flue are both fixedly installed in the installation chamber through the support member, the flue is arranged in the gas mixing chamber, the burner head is annularly installed in the flue, a gas inlet of the burner head is communicated with the gas mixing chamber, the burning directions of the burner head are both towards the central axis of the flue, and the support member is filled with a refractory castable material.
4. The sectional flue heat utilization device for hydrogen production from natural gas as claimed in claim 3, wherein the burner further comprises a fuel gas feeding pipe and a sleeve, the fuel gas feeding pipe is arranged in the sleeve, an air inlet of the sleeve is respectively communicated with an air outlet of the air preheater and an air outlet of the induced draft fan, both the air outlet of the fuel gas feeding pipe and the air outlet of the sleeve are communicated with the fuel gas mixing chamber, and a firing end of a firing gun of the burner is arranged inside the fuel gas mixing chamber.
5. The segmented flue heat utilization device for hydrogen production from natural gas as claimed in any one of claims 1 to 4, wherein the reformer tube on the reformer comprises a flexible element for maintaining the sealing performance between the reformer tube and the inside of the reformer body of the reformer, the lower end of the flexible element is fixedly connected with a nozzle at the top of the reformer body for passing through the reformer tube, the lower ends of the reformer tube are fixedly arranged at the bottom of the reformer body, the upper end of the reformer tube sequentially passes through the nozzle at the top of the reformer body and the flexible element, and the upper end of the reformer tube is fixedly connected with the upper pigtail tube joint.
6. The segmented flue heat utilization device for hydrogen production from natural gas as claimed in claim 5, wherein the flexible element is an expansion joint, the lower end of the expansion joint is fixedly connected with a pipe orifice at the top of the furnace body, the upper end of the conversion pipe sequentially penetrates through the pipe orifice at the top of the furnace and the expansion joint, and high-temperature ceramic fiber blankets are filled in the expansion joint.
7. A heat utilization method for a natural gas hydrogen production sectional type flue is characterized by comprising the following steps:
s1, after entering a flue, the high-temperature flue gas from the reformer exchanges heat with natural gas and steam for the first time through a mixed gas preheater, and after the temperature of the natural gas and the steam is raised, the high-temperature flue gas enters a reformer tube;
s2, performing secondary heat exchange on the flue gas subjected to the primary heat exchange and the natural gas through a first natural gas preheater, and heating the natural gas to enter an air inlet of a mixed gas preheater;
s3, heating the flue gas subjected to the second heat exchange by a burner;
s4, carrying out third heat exchange on the heated flue gas and water through the flue gas waste boiler, and enabling steam generated by the flue gas waste boiler to enter an air inlet of the mixed gas preheater;
s5, performing fourth heat exchange on the flue gas subjected to the third heat exchange with natural gas through a second natural gas preheater, and heating the natural gas to enter a natural gas inlet of the first natural gas preheater;
and (3) finally carrying out the last heat exchange on the flue gas subjected to the S6 and the fourth heat exchange with air through an air preheater, wherein the temperature after cooling is slightly higher than the dew point temperature, and finally, the flue gas subjected to cooling is extracted through an induced draft fan, wherein most of the flue gas is discharged through a chimney, and the other part of the flue gas and the air inlet of the sleeve in the combustor are communicated.
8. The heat utilization method for the segmented flue for hydrogen production from natural gas as claimed in claim 7, wherein in S1, the temperature range of the flue gas after the first heat exchange is 560-600 ℃, and the temperature range of the natural gas and the steam is 560-600 ℃; in S2, the temperature range of the flue gas after the second heat exchange is 360-400 ℃, and the temperature range of the natural gas is 320-360 ℃; in S4, the temperature range of the flue gas after the third heat exchange is 200-240 ℃, and in S5, the temperature range of the flue gas after the fourth heat exchange is 160-200 ℃.
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112827335A (en) * | 2020-12-22 | 2021-05-25 | 四川天采科技有限责任公司 | Low NOXNatural gas hydrogen production process with flue gas emission |
| CN114136114A (en) * | 2021-11-12 | 2022-03-04 | 上海置信能源综合服务有限公司 | Low-carbon-dioxide-emission external-heating calcining kiln combustion heating system |
| CN114377547A (en) * | 2021-12-03 | 2022-04-22 | 国能(山东)能源环境有限公司 | Flue gas low-nitrogen treatment device and method for natural gas hydrogen production reformer |
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2020
- 2020-03-23 CN CN202010207174.0A patent/CN111256485A/en active Pending
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112827335A (en) * | 2020-12-22 | 2021-05-25 | 四川天采科技有限责任公司 | Low NOXNatural gas hydrogen production process with flue gas emission |
| CN114136114A (en) * | 2021-11-12 | 2022-03-04 | 上海置信能源综合服务有限公司 | Low-carbon-dioxide-emission external-heating calcining kiln combustion heating system |
| CN114377547A (en) * | 2021-12-03 | 2022-04-22 | 国能(山东)能源环境有限公司 | Flue gas low-nitrogen treatment device and method for natural gas hydrogen production reformer |
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