CN108467014B - Reforming reactor in steam reforming hydrogen production device - Google Patents
Reforming reactor in steam reforming hydrogen production device Download PDFInfo
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- CN108467014B CN108467014B CN201810467229.4A CN201810467229A CN108467014B CN 108467014 B CN108467014 B CN 108467014B CN 201810467229 A CN201810467229 A CN 201810467229A CN 108467014 B CN108467014 B CN 108467014B
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- flue gas
- heat exchange
- reforming
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- 238000002407 reforming Methods 0.000 title claims abstract description 63
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 title claims abstract description 38
- 229910052739 hydrogen Inorganic materials 0.000 title claims abstract description 38
- 239000001257 hydrogen Substances 0.000 title claims abstract description 38
- 238000000629 steam reforming Methods 0.000 title claims abstract description 30
- 238000004519 manufacturing process Methods 0.000 title abstract description 27
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 89
- 239000003546 flue gas Substances 0.000 claims abstract description 85
- 238000006243 chemical reaction Methods 0.000 claims abstract description 72
- 239000000463 material Substances 0.000 claims abstract description 50
- 238000005338 heat storage Methods 0.000 claims abstract description 41
- 239000000779 smoke Substances 0.000 claims abstract description 41
- 239000007789 gas Substances 0.000 claims abstract description 30
- 238000009825 accumulation Methods 0.000 claims abstract description 16
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 32
- 238000005192 partition Methods 0.000 claims description 8
- 230000001105 regulatory effect Effects 0.000 claims description 3
- 238000007599 discharging Methods 0.000 abstract description 10
- 239000002918 waste heat Substances 0.000 abstract description 7
- 230000036632 reaction speed Effects 0.000 abstract description 2
- 229930195733 hydrocarbon Natural products 0.000 description 13
- 150000002430 hydrocarbons Chemical class 0.000 description 13
- 238000006057 reforming reaction Methods 0.000 description 10
- 239000004215 Carbon black (E152) Substances 0.000 description 9
- 238000010438 heat treatment Methods 0.000 description 6
- 229910002091 carbon monoxide Inorganic materials 0.000 description 4
- 239000002737 fuel gas Substances 0.000 description 4
- 238000002485 combustion reaction Methods 0.000 description 2
- 239000007788 liquid Substances 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- 239000012495 reaction gas Substances 0.000 description 2
- 239000000571 coke Substances 0.000 description 1
- 238000006477 desulfuration reaction Methods 0.000 description 1
- 230000023556 desulfurization Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 239000003517 fume Substances 0.000 description 1
- 239000003915 liquefied petroleum gas Substances 0.000 description 1
- 238000000034 method Methods 0.000 description 1
- 239000003345 natural gas Substances 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
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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
- C01B3/36—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 oxygen or mixtures containing oxygen as gasifying agents
-
- 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
- C01B3/48—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 followed by reaction of water vapour with carbon monoxide
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F22—STEAM GENERATION
- F22B—METHODS OF STEAM GENERATION; STEAM BOILERS
- F22B1/00—Methods of steam generation characterised by form of heating method
- F22B1/02—Methods of steam generation characterised by form of heating method by exploitation of the heat content of hot heat carriers
- F22B1/18—Methods of steam generation characterised by form of heating method by exploitation of the heat content of hot heat carriers the heat carrier being a hot gas, e.g. waste gas such as exhaust gas of internal-combustion engines
- F22B1/1807—Methods of steam generation characterised by form of heating method by exploitation of the heat content of hot heat carriers the heat carrier being a hot gas, e.g. waste gas such as exhaust gas of internal-combustion engines using the exhaust gases of combustion engines
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/00002—Chemical plants
- B01J2219/00018—Construction aspects
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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
- C01B2203/0211—Processes for making hydrogen or synthesis gas containing a reforming step containing a non-catalytic reforming step
- C01B2203/0216—Processes for making hydrogen or synthesis gas containing a reforming step containing a non-catalytic reforming step containing a non-catalytic steam reforming step
-
- 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
- C01B2203/08—Methods of heating or cooling
- C01B2203/0805—Methods of heating the process for making hydrogen or synthesis gas
- C01B2203/0833—Heating by indirect heat exchange with hot fluids, other than combustion gases, product gases or non-combustive exothermic reaction product gases
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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
- Y02E20/30—Technologies for a more efficient combustion or heat usage
-
- 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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- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Combustion & Propulsion (AREA)
- Organic Chemistry (AREA)
- Health & Medical Sciences (AREA)
- General Health & Medical Sciences (AREA)
- Inorganic Chemistry (AREA)
- Life Sciences & Earth Sciences (AREA)
- Sustainable Development (AREA)
- Sustainable Energy (AREA)
- Physics & Mathematics (AREA)
- Thermal Sciences (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Hydrogen, Water And Hydrids (AREA)
Abstract
The invention discloses a reforming reactor in a steam reforming hydrogen production device, which comprises: the shell is provided with a flue gas input pipe, a steam input pipe, a material conveying pipe and a reformed gas output pipe, a reforming area and a heat storage area are arranged in the shell, a plurality of reaction pipes are arranged in the reforming area, the flue gas input pipe is communicated with the shell at the feeding end of the reaction pipes, and the reformed gas output pipe is communicated with the discharging end of the reaction pipes and extends out of the shell. The heat accumulation area is positioned at one side of the discharge end of the reaction tube, a plurality of material preheating tubes are arranged in the heat accumulation area, the material conveying tube is communicated with the input end of the material preheating tube, the output end of the material preheating tube and the steam input tube are both communicated with the feed end of the reaction tube, and the heat accumulation area is provided with a smoke output mechanism. The invention has the advantages that: the waste heat of the flue gas can be fully utilized, the hydrogen production cost is reduced, and the reaction speed and the conversion rate can be effectively improved.
Description
Technical Field
The invention relates to the technical field of steam reforming hydrogen production equipment, in particular to a reforming reactor.
Background
At present, the structure of the steam reforming hydrogen production device mainly comprises: reforming reactor, carbon monoxide converter, pressure swing adsorber. The reforming reactor comprises a shell, a reforming reactor and a carbon monoxide converter, wherein a plurality of reaction tubes are arranged in the shell, a fuel gas conveying tube, an air conveying tube, a water vapor input tube, a material conveying tube and a reformed gas output tube are arranged on the shell, the fuel gas conveying tube and the air conveying tube are respectively communicated with the shell, so that gas serving as fuel and gas serving as combustion supporting are respectively conveyed to one end of the shell of the reforming reactor, which is provided with an ignition device, for combustion heating, the water vapor input tube and the material conveying tube are respectively communicated with the reaction tubes in the shell, so that water vapor and hydrocarbon materials which participate in reaction are respectively conveyed to the reaction tubes in the shell, the reformed gas output tube is communicated with the carbon monoxide converter, and reformed gas generated by reaction in the reaction tubes is output by the reformed gas output tube.
The reforming reactor described above has the following drawbacks: 1. the additional use of fuel gas to supply heat is required, which results in high hydrogen production costs. 2. The fuel gas and the combustion-supporting gas need to be ignited in the shell, and an ignition device needs to be additionally arranged in the reforming reactor, so that the structure of the reforming reactor is complex.
In addition, at present, high-temperature flue gas generated in many industries, such as coke oven high-temperature flue gas, is mostly not fully utilized, and therefore, a large amount of heat energy is lost.
Disclosure of Invention
The purpose of the invention is that: the reforming reactor in the steam reforming hydrogen production device can fully utilize the waste heat of high-temperature flue gas and greatly reduce the hydrogen production cost.
In order to achieve the above purpose, the invention adopts the following technical scheme: a reforming reactor in a steam reforming hydrogen plant, comprising: the device comprises a shell, wherein a smoke input pipe, a steam input pipe, a material conveying pipe and a reformed gas output pipe are arranged on the shell, a reforming zone and a heat storage zone are arranged in the shell, a plurality of reaction pipes are arranged in the reforming zone, the smoke input pipe is communicated with the shell at the feeding end of the reaction pipe, the reformed gas output pipe is communicated with the discharging end of the reaction pipe, the heat storage zone is positioned at one side of the discharging end of the reaction pipe, a plurality of material preheating pipes are arranged in the heat storage zone, the material conveying pipe is communicated with the input end of the material preheating pipe, the output end of the material preheating pipe and the steam input pipe are both communicated with the feeding end of the reaction pipe, a smoke output mechanism is arranged in the heat storage zone, high-temperature smoke enters the reforming zone at the feeding end of the reaction pipe from the smoke input pipe, the high-temperature smoke in the reforming zone enters the heat storage zone after moving from the feeding end of the reaction pipe to the discharging end of the reaction pipe, and the smoke in the heat storage zone is discharged through the smoke output mechanism; the reformed gas output pipe extends out of the housing.
Further, the reforming reactor in the steam reforming hydrogen production device is characterized in that the flue gas output mechanism of the heat accumulation area is communicated with the heat exchange boiler, flue gas of the heat accumulation area enters the heat exchange boiler through the flue gas output mechanism to supply heat to the heat exchange boiler, a heat exchange water pipe is arranged in the heat exchange boiler, one end of the heat exchange water pipe is communicated with a water supply pipe of the heat exchange boiler with a water pump, the other end of the heat exchange water pipe is communicated with a steam pipeline, a smoke exhaust pipeline is arranged at the top of the heat exchange boiler, flue gas in the heat exchange boiler is discharged from the smoke exhaust pipeline, and steam generated in the heat exchange water pipe is output outwards through the steam pipeline.
Further, in the reforming reactor in the steam reforming hydrogen production device, the shell of the heat exchange boiler is integrated with the shell, and the shell side of the heat exchange boiler is separated from the reforming zone and the heat storage zone by a partition plate.
Further, the reforming reactor in the steam reforming hydrogen production apparatus, wherein the structure of the flue gas output mechanism comprises: a plurality of smoke exhaust holes are formed in the partition plate at the input end of the material preheating pipe, the smoke exhaust holes are communicated with the heat exchange boiler, a smoke exhaust pipe of a heat storage area is further arranged on the shell of the heat storage area at the input end of the material preheating pipe, part of smoke in the heat storage area enters the heat exchange boiler to supply heat through the smoke exhaust holes, and part of smoke is output outwards through the smoke exhaust pipe of the heat storage area.
Still further, in the reforming reactor in the foregoing steam reforming hydrogen production apparatus, the smoke discharge holes are arranged on a partition plate directly below the heat exchange water pipe.
Further, in the reforming reactor in the steam reforming hydrogen production device, a blower for continuously conveying the flue gas outwards is arranged on the flue gas exhaust pipeline.
Further, in the reforming reactor in the steam reforming hydrogen production device, the flue gas input pipe is provided with a temperature regulator, and the high-temperature flue gas enters the reforming zone after the temperature of the high-temperature flue gas is regulated by the temperature regulator.
Further, in the reforming reactor in the steam reforming hydrogen production device, the temperature regulator is a heat transfer oil temperature controller, the heat transfer oil temperature controller is connected with a heat transfer oil heat exchange tube, the heat transfer oil heat exchange tube is arranged in a heat exchange boiler, a heat transfer oil pump is arranged on the heat transfer oil heat exchange tube, and under the action of the heat transfer oil pump, heat transfer oil continuously enters the heat transfer oil heat exchange tube from the heat transfer oil temperature controller, and then enters the heat transfer oil temperature controller from the output end of the heat transfer oil heat exchange tube; the high-temperature flue gas enters the heat conduction oil temperature controller through the flue gas input pipe for temperature adjustment, and then enters the reforming zone of the shell.
Further, in the reforming reactor in the steam reforming hydrogen production device, the reforming region at the feeding end position of the reaction tube is provided with a mixer, and the output end of the material preheating tube and the steam input tube are both communicated to the mixer first and then to the feeding ends of the reaction tubes.
Further, in the reforming reactor in the steam reforming hydrogen production device, the reformed gas output pipe extending out of the shell is connected to the evaporator, the reformed gas generated by the reaction in the reaction pipe is conveyed to the evaporator by the reformed gas output pipe to supply heat, the steam output end of the evaporator is communicated with the steam input pipe, and the steam generated in the evaporator enters the steam input pipe.
The invention has the advantages that: 1. the high-temperature flue gas is adopted for heating, and the waste heat of the flue gas can be fully utilized, so that the hydrogen production cost is reduced. 2. The shell of the reforming reactor is divided into a reforming zone and a heat storage zone, and a material preheating pipe in the heat storage zone preheats hydrocarbon materials entering the reaction pipe for reaction, so that the waste heat of flue gas is fully utilized, and the rate and conversion rate of reforming reaction in the reaction pipe can be effectively improved. 3. The heat exchange boiler is arranged, the flue gas after heat exchange between the heat storage area and the material preheating pipe is conveyed into the heat exchange boiler for heat supply, and the generated steam in the heat exchange boiler can be used as heating medium of other devices in the steam reforming hydrogen production device, so that the hydrogen production cost can be greatly reduced. 4. The heat exchange boiler has the advantages that the boiler barrel and the shell are integrated into a whole, the structure is greatly simplified, the occupied space of equipment is greatly reduced, and smoke in the heat accumulation area can enter the heat exchange boiler in the shortest path, so that the loss of heat of the smoke can be effectively reduced.
Drawings
Fig. 1 is a schematic diagram of a reforming reactor in a steam reforming hydrogen plant according to the present invention.
Detailed Description
The invention will be described in further detail with reference to the drawings and the preferred embodiments.
As shown in fig. 1, a reforming reactor in a steam reforming hydrogen plant includes: the shell 11 is provided with a flue gas input pipe 12, a steam input pipe 13, a material conveying pipe 14 and a reformed gas output pipe 15. The housing 11 is divided into a reforming region 101 and a heat storage region 102. A plurality of reaction tubes 16 are arranged in the reforming zone 101, the flue gas input tube 12 is communicated with the shell 11 at the feeding end of the reaction tubes 16, and the reformed gas output tube 15 is communicated with the discharging end of the reaction tubes 16 and extends out of the shell 11. The heat accumulation area 102 is located one side of the discharge end of the reaction tube 16, a plurality of material preheating tubes 17 are arranged in the heat accumulation area 102, the material conveying tube 14 is communicated with the input end of the material preheating tubes 17, the output end of the material preheating tubes 17 and the steam input tube 13 are both communicated with the feed end of the reaction tube 16, and a flue gas output mechanism is arranged on the shell 11 of the heat accumulation area 102. The high-temperature flue gas enters the reforming zone 101 at the feeding end of the reaction tube 16 from the flue gas input tube 12, the high-temperature flue gas in the reforming zone 101 moves from the feeding end of the reaction tube 16 to the discharging end of the reaction tube 16 and then enters the heat accumulating zone 102, and the flue gas in the heat accumulating zone 102 is discharged through the flue gas output mechanism.
In this embodiment, a mixer 19 is disposed in the reforming zone 101 at the feeding end of the reaction tube 16, and the output end of the material preheating tube 17 and the steam input tube 13 are both connected to the mixer 19, and the mixer 19 is then connected to the feeding end of each reaction tube 16. The purpose of the mixer 19 is to: the hydrocarbon materials participating in the reforming reaction are uniformly mixed with the steam and then enter the reaction tube 16, so that the conversion rate of the reforming reaction in the reaction tube 16 can be effectively improved.
The flue gas output mechanism of heat accumulation area 102 is linked together with heat transfer boiler 4, the flue gas of heat accumulation area 102 passes through flue gas output mechanism and gets into heat transfer boiler 4 in the heat transfer boiler, be provided with heat transfer water pipe 401 in the heat transfer boiler 4, heat transfer water pipe 401's one end is linked together with the heat transfer boiler feed pipe 41 of taking water pump 411, heat transfer water pipe 401's the other end is linked together with steam pipe 42, heat transfer boiler 4's top is provided with exhaust pipe 43, flue gas in the heat transfer boiler 4 is discharged from exhaust pipe, the steam that produces in the heat transfer water pipe 401 is outwards exported by steam pipe 43, be provided with the air-blower 431 of constantly outwards carrying the flue gas on the exhaust pipe 43. The steam generated in the heat exchange boiler 4 is outputted outwards by the steam pipe 43.
In order to simplify the structure and reduce the occupied space of the equipment, the boiler barrel 40 of the heat exchange boiler 4 is integrated with the shell 11 into a whole in the embodiment, and the shell side of the heat exchange boiler 4 is separated from the reforming zone 101 and the heat storage zone 102 by the partition 111. The structure of the fume output mechanism of the heat accumulation area 102 includes: a plurality of smoke discharging holes 110 are formed in a baffle 111 at the input end position of the material preheating pipe 17, the smoke discharging holes 110 are communicated with the boiler barrel 40 of the heat exchange boiler 4, and a heat storage area smoke discharging pipe 112 is further arranged on the shell 11 of the heat storage area 102 at the input end position of the material preheating pipe 17. Part of the flue gas in the heat storage area enters the heat exchange boiler 4 through the smoke exhaust hole 110 to supply heat, and part of the flue gas is output outwards through the flue gas discharge pipe 112 in the heat storage area, and the flue gas in the flue gas discharge pipe 112 can be input into other devices in the steam reforming hydrogen production device, such as the flue gas is conveyed into a desulfurizer to supply heat for desulfurization reaction. The structure in which the drum 40 of the heat exchange boiler 4 is integrated with the housing 11 also has the following advantages: the flue gas in the heat accumulation area 102 can enter the heat exchange boiler 4 in the shortest path, so that the loss of the heat of the flue gas can be effectively reduced.
In order to regulate and control the temperature of the high-temperature flue gas entering the shell 11, a temperature regulator is arranged on the flue gas input pipe 12, and the high-temperature flue gas enters the reforming reactor 1 after the temperature is regulated by the temperature regulator. Specifically, the temperature regulator in this embodiment is a heat-conducting oil temperature controller 120, the heat-conducting oil temperature controller 120 is connected with a heat-conducting oil heat exchange tube 121, the heat-conducting oil heat exchange tube 121 is arranged in the heat exchange boiler 4, a heat-conducting oil pump 122 is arranged on the heat-conducting oil heat exchange tube 121, and under the action of the heat-conducting oil pump 122, heat-conducting oil continuously enters from the heat-conducting oil temperature controller 120 to the heat-conducting oil heat exchange tube 121, and then enters into the heat-conducting oil temperature controller 120 from the output end of the heat-conducting oil heat exchange tube 121; the high-temperature flue gas enters the heat conducting oil temperature controller 120 through the flue gas input pipe 12 for temperature adjustment and then enters the shell 11 of the reforming reactor 1, so that the reaction temperature of the reforming reaction in the reaction pipe 16 can be effectively ensured, and the reforming reaction efficiency is effectively improved.
It is also preferable that the smoke discharge holes 110 are arranged on the partition 111 directly under the heat exchange water pipe 401 so that primary heat exchange, in which the smoke exchanges heat with the heat exchange water pipe 401, and secondary heat exchange, in which the smoke exchanges heat with the heat transfer oil heat exchange pipe 121, are formed in the boiler 4.
In order to fully utilize the waste heat of the reformed gas output by the reaction tube 16, the reformed gas output tube 15 conveys the reformed gas generated by the reaction in the reaction tube 16 to the evaporator 6 for heating, the steam output end of the evaporator 6 is communicated with the steam input tube 13, and the steam generated in the evaporator 6 enters the steam input tube 13.
The principles of operation of the reforming reactor in the steam reforming hydrogen plant are further described below.
Hydrocarbon materials that may be used for hydrogen production, as conveyed by material conveying pipe 14, may be generally classified into gaseous hydrocarbons and liquid hydrocarbons, the gaseous hydrocarbons being mainly: natural gas, biogas, hydrogenated dry gas, coked dry gas, aromatized dry gas, and the like; the liquid hydrocarbons are mainly: straight run naphtha, hydrogenated light naphtha, raffinate oil from reformer, topped oil, saturated liquefied petroleum gas, and the like.
The hydrocarbon materials are conveyed by the material conveying pipe 14 into the material preheating pipe 17 in the heat storage area 102 of the shell 11 for preheating, and the hydrocarbon materials in the material preheating pipe 17 enter the mixer 19 from the output end of the material preheating pipe 17. The hydrocarbon material is sufficiently preheated in the heat storage area 102 so as to be fully prepared for the reforming reaction in the reaction tube 16, which can greatly accelerate the reaction speed of the reforming reaction and effectively improve the conversion rate of the reforming reaction.
The water vapor generated in the evaporator 6 enters the mixer 19 from the water vapor input pipe 13. In general, in order to improve the reaction efficiency, the feed water in the evaporator 6 is demineralized water, and the produced water vapor is demineralized water vapor.
The hydrocarbon material and desalted water vapor are mixed uniformly in the mixer 19 and then enter each reaction tube 16 for reforming reaction. The reaction tube 16 reacts to produce a reformed reaction gas. The reformed reaction gas is first supplied from the reformed gas output pipe 15 to the evaporator 16 for heat supply, and then supplied to the carbon monoxide converter in the steam reforming hydrogen production apparatus for reaction.
In the above working process, the high temperature flue gas is firstly input into the heat conducting oil temperature controller 120 by the flue gas input pipe 12 for temperature adjustment, the high temperature flue gas after temperature adjustment enters the reforming zone 101 of the reforming reactor 1 to supply heat for the reaction pipe 16, the high temperature flue gas moves from the feeding end of the reaction pipe 16 to the discharging end of the reaction pipe 16 in the reforming zone 101 to release a large amount of heat, the flue gas releasing a large amount of heat enters the heat storage zone 102, the flue gas of the heat storage zone 102 exchanges heat with the material preheating pipe 17 to further release heat, a part of the flue gas releasing heat in the heat storage zone 102 enters the heat exchange boiler 4, and a part of the flue gas is output outwards by the flue gas discharge pipe 112 in the heat storage zone. The flue gas entering the heat exchange boiler 4 exchanges heat with the heat exchange water pipe and the heat transfer oil heat exchange pipe 121 in the heat exchange boiler 4, so that heat is fully released, and the flue gas with the heat fully released in the heat exchange boiler 4 is discharged from the smoke exhaust pipeline 43. The flue gas in the flue gas outlet pipe 112 can be input to other devices in the steam reforming hydrogen plant for heat supply.
The invention has the advantages that: 1. the high-temperature flue gas is adopted for heating, and the waste heat of the flue gas can be fully utilized, so that the hydrogen production cost is reduced. 2. The reforming zone 101 and the heat storage zone 102 are arranged in the shell 11, and the hydrocarbon materials entering the reaction tube 16 for reaction are preheated by the material preheating tube 17 in the heat storage zone 102, so that the waste heat of the flue gas is fully utilized, and the rate and the conversion rate of the reforming reaction in the reaction tube 16 can be effectively improved. 3. The heat exchange boiler 4 is arranged, the flue gas after heat exchange with the material preheating pipe 17 in the heat accumulation area 102 is conveyed into the heat exchange boiler 4 for heat supply, and the generated steam in the heat exchange boiler 4 can be used as heating medium of other devices in the steam reforming hydrogen production device, so that the hydrogen production cost can be greatly reduced. 4. The drum 40 of the heat exchange boiler 4 is integrated with the shell 11, the structure is greatly simplified, the occupied space of equipment is greatly reduced, and the flue gas in the heat storage area 102 can enter the heat exchange boiler 4 in the shortest path, so that the loss of the heat of the flue gas can be effectively reduced.
Claims (6)
1. A reforming reactor in a steam reforming hydrogen plant, comprising: the shell is provided with a flue gas input pipe, a steam input pipe, a material conveying pipe and a reformed gas output pipe, and is characterized in that: the device comprises a shell, a reforming zone and a heat storage zone, wherein a plurality of reaction tubes are arranged in the reforming zone, a flue gas input tube is communicated with the shell at the feed end of the reaction tubes, a reformed gas output tube is communicated with the discharge end of the reaction tubes, the heat storage zone is positioned at one side of the discharge end of the reaction tubes, a plurality of material preheating tubes are arranged in the heat storage zone, a material conveying tube is communicated with the input end of the material preheating tubes, the output end of the material preheating tubes and a steam input tube are both communicated with the feed end of the reaction tubes, a flue gas output mechanism is arranged in the heat storage zone, high-temperature flue gas enters the reforming zone at the feed end of the reaction tubes from the flue gas input tube, the high-temperature flue gas in the reforming zone enters the heat storage zone after moving from the feed end of the reaction tubes to the discharge end of the reaction tubes, and the flue gas in the heat storage zone is discharged through the flue gas output mechanism; the reformed gas output pipe extends out of the shell; the flue gas output mechanism of the heat accumulation area is communicated with the heat exchange boiler, flue gas of the heat accumulation area enters the heat exchange boiler through the flue gas output mechanism so as to supply heat for the heat exchange boiler, a heat exchange water pipe is arranged in the heat exchange boiler, one end of the heat exchange water pipe is communicated with a water supply pipe of the heat exchange boiler with a water pump, the other end of the heat exchange water pipe is communicated with a steam pipeline, a smoke exhaust pipeline is arranged at the top of the heat exchange boiler, flue gas in the heat exchange boiler is discharged from the smoke exhaust pipeline, and steam generated in the heat exchange water pipe is output outwards through the steam pipeline; the shell side of the heat exchange boiler is separated from the reforming zone and the heat storage zone by a partition plate; the structure of the flue gas output mechanism comprises: a plurality of smoke exhaust holes are formed in the partition plate at the input end of the material preheating pipe, the smoke exhaust holes are communicated with the heat exchange boiler, a smoke exhaust pipe of a heat storage area is further arranged on the shell of the heat storage area at the input end of the material preheating pipe, part of smoke in the heat storage area enters the heat exchange boiler through the smoke exhaust holes to supply heat, and part of smoke is output outwards through the smoke exhaust pipe of the heat storage area; the reformed gas output pipe extending out of the shell is connected to the evaporator, the reformed gas generated by the reaction in the reaction pipe is conveyed to the evaporator by the reformed gas output pipe to supply heat, the steam output end of the evaporator is communicated with the steam input pipe, and the steam generated in the evaporator enters the steam input pipe.
2. A reforming reactor in a steam reforming hydrogen plant as defined in claim 1, wherein: the smoke exhaust holes are arranged on the partition board right below the heat exchange water pipe.
3. A reforming reactor in a steam reforming hydrogen plant as defined in claim 1 or 2, wherein: the smoke exhaust pipeline is provided with a blower for continuously conveying the smoke outwards.
4. A reforming reactor in a steam reforming hydrogen plant as defined in claim 1 or 2, wherein: the flue gas input pipe is provided with a temperature regulator, and the high-temperature flue gas enters the reforming zone after the temperature of the high-temperature flue gas is regulated by the temperature regulator.
5. A reforming reactor in a steam reforming hydrogen plant as defined in claim 4, wherein: the temperature regulator is a heat-conducting oil temperature controller, the heat-conducting oil temperature controller is connected with a heat-conducting oil heat exchange tube, the heat-conducting oil heat exchange tube is arranged in a heat exchange boiler, a heat-conducting oil pump is arranged on the heat-conducting oil heat exchange tube, and under the action of the heat-conducting oil pump, heat-conducting oil continuously enters the heat-conducting oil heat exchange tube from the heat-conducting oil temperature controller and then enters the heat-conducting oil temperature controller from the output end of the heat-conducting oil heat exchange tube; the high-temperature flue gas enters the heat conduction oil temperature controller through the flue gas input pipe for temperature adjustment, and then enters the reforming zone of the shell.
6. A reforming reactor in a steam reforming hydrogen plant as defined in claim 1 or 2, wherein: the reforming zone at the feeding end of the reaction tube is provided with a mixer, the output end of the material preheating tube and the steam input tube are both communicated to the mixer, and the mixer is communicated to the feeding end of each reaction tube.
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| CN109573945B (en) * | 2018-12-14 | 2020-08-28 | 中国科学院广州能源研究所 | Steam separation and recycling device and method for flue gas in methane reforming hydrogen production combustor |
| CN114789990A (en) * | 2021-11-30 | 2022-07-26 | 苏州科瑞工程科技有限公司 | Methanol hydrogen production converter and methanol hydrogen production device |
| CN115321630B (en) * | 2022-10-11 | 2023-02-14 | 浙江百能科技有限公司 | Method and system for producing hydrogen by coal grading utilization and wastewater zero discharge coupling |
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