CN111320135A - Small-size distributed combined heat and power generation system - Google Patents
Small-size distributed combined heat and power generation system Download PDFInfo
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- CN111320135A CN111320135A CN202010241709.6A CN202010241709A CN111320135A CN 111320135 A CN111320135 A CN 111320135A CN 202010241709 A CN202010241709 A CN 202010241709A CN 111320135 A CN111320135 A CN 111320135A
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- 238000010248 power generation Methods 0.000 title claims description 16
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 119
- 239000001257 hydrogen Substances 0.000 claims abstract description 85
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 85
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 83
- 238000002407 reforming Methods 0.000 claims abstract description 62
- 239000007789 gas Substances 0.000 claims abstract description 60
- 238000004519 manufacturing process Methods 0.000 claims abstract description 53
- 239000008367 deionised water Substances 0.000 claims abstract description 42
- 229910021641 deionized water Inorganic materials 0.000 claims abstract description 42
- 230000008676 import Effects 0.000 claims abstract description 21
- 239000000446 fuel Substances 0.000 claims abstract description 16
- 238000000746 purification Methods 0.000 claims abstract description 16
- 239000002737 fuel gas Substances 0.000 claims abstract description 10
- 239000002912 waste gas Substances 0.000 claims abstract description 8
- 238000006243 chemical reaction Methods 0.000 claims description 68
- 238000003860 storage Methods 0.000 claims description 49
- 238000000629 steam reforming Methods 0.000 claims description 32
- 238000002347 injection Methods 0.000 claims description 30
- 239000007924 injection Substances 0.000 claims description 30
- 239000002351 wastewater Substances 0.000 claims description 30
- 238000001914 filtration Methods 0.000 claims description 29
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 24
- 239000001301 oxygen Substances 0.000 claims description 24
- 229910052760 oxygen Inorganic materials 0.000 claims description 24
- 238000001223 reverse osmosis Methods 0.000 claims description 24
- 239000003054 catalyst Substances 0.000 claims description 23
- 229910021645 metal ion Inorganic materials 0.000 claims description 19
- 238000006555 catalytic reaction Methods 0.000 claims description 18
- 238000002485 combustion reaction Methods 0.000 claims description 18
- 238000001179 sorption measurement Methods 0.000 claims description 17
- 239000011148 porous material Substances 0.000 claims description 12
- 239000002994 raw material Substances 0.000 claims description 10
- 239000002699 waste material Substances 0.000 claims description 7
- 210000001503 joint Anatomy 0.000 claims description 3
- 230000011218 segmentation Effects 0.000 claims description 2
- 238000010438 heat treatment Methods 0.000 abstract description 5
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 42
- 239000003345 natural gas Substances 0.000 description 20
- 239000012495 reaction gas Substances 0.000 description 12
- 210000004027 cell Anatomy 0.000 description 11
- 239000000567 combustion gas Substances 0.000 description 6
- 239000008399 tap water Substances 0.000 description 6
- 235000020679 tap water Nutrition 0.000 description 6
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 4
- 229910002091 carbon monoxide Inorganic materials 0.000 description 4
- 239000000376 reactant Substances 0.000 description 4
- 239000012535 impurity Substances 0.000 description 3
- 239000007788 liquid Substances 0.000 description 3
- 210000002421 cell wall Anatomy 0.000 description 2
- 239000007809 chemical reaction catalyst Substances 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 150000002431 hydrogen Chemical class 0.000 description 2
- 238000002156 mixing Methods 0.000 description 2
- 239000000843 powder Substances 0.000 description 2
- 239000003507 refrigerant Substances 0.000 description 2
- 239000002002 slurry Substances 0.000 description 2
- 150000003568 thioethers Chemical class 0.000 description 2
- 239000003463 adsorbent Substances 0.000 description 1
- 230000005540 biological transmission Effects 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 230000003247 decreasing effect Effects 0.000 description 1
- 230000018109 developmental process Effects 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 238000009826 distribution Methods 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 239000002803 fossil fuel Substances 0.000 description 1
- 238000005286 illumination Methods 0.000 description 1
- 239000010410 layer Substances 0.000 description 1
- 238000000034 method Methods 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 230000002572 peristaltic effect Effects 0.000 description 1
- 239000002574 poison Substances 0.000 description 1
- 231100000614 poison Toxicity 0.000 description 1
- 239000000523 sample Substances 0.000 description 1
- 239000002344 surface layer Substances 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
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F24—HEATING; RANGES; VENTILATING
- F24D—DOMESTIC- OR SPACE-HEATING SYSTEMS, e.g. CENTRAL HEATING SYSTEMS; DOMESTIC HOT-WATER SUPPLY SYSTEMS; ELEMENTS OR COMPONENTS THEREFOR
- F24D15/00—Other domestic- or space-heating systems
-
- H—ELECTRICITY
- H01—ELECTRIC ELEMENTS
- H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
- H01M8/00—Fuel cells; Manufacture thereof
- H01M8/06—Combination of fuel cells with means for production of reactants or for treatment of residues
- H01M8/0606—Combination of fuel cells with means for production of reactants or for treatment of residues with means for production of gaseous reactants
- H01M8/0612—Combination of fuel cells with means for production of reactants or for treatment of residues with means for production of gaseous reactants from carbon-containing material
- H01M8/0618—Reforming processes, e.g. autothermal, partial oxidation or steam reforming
-
- 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
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F24—HEATING; RANGES; VENTILATING
- F24D—DOMESTIC- OR SPACE-HEATING SYSTEMS, e.g. CENTRAL HEATING SYSTEMS; DOMESTIC HOT-WATER SUPPLY SYSTEMS; ELEMENTS OR COMPONENTS THEREFOR
- F24D2200/00—Heat sources or energy sources
- F24D2200/16—Waste heat
- F24D2200/18—Flue gas recuperation
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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
- Y02E60/00—Enabling technologies; Technologies with a potential or indirect contribution to GHG emissions mitigation
- Y02E60/30—Hydrogen technology
- Y02E60/50—Fuel cells
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- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Combustion & Propulsion (AREA)
- Organic Chemistry (AREA)
- Life Sciences & Earth Sciences (AREA)
- Electrochemistry (AREA)
- General Health & Medical Sciences (AREA)
- Health & Medical Sciences (AREA)
- Manufacturing & Machinery (AREA)
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Abstract
The invention discloses a small-sized distributed cogeneration system, comprising: reforming hydrogen production device, desulfurizer, hydrogen fuel cell, deionized water purification system, gas air mixer, heat exchanger, reforming hydrogen production device's feed gas inlet links to each other with the export of desulfurizer, the import of desulfurizer links to each other with the feed gas house steward, reforming hydrogen production device's main fuel gas inlet links to each other with the export of gas air mixer, gas air mixer's first import links to each other with the feed gas house steward, gas air mixer's second import is linked together with the atmosphere, reforming hydrogen production device's deionized water inlet links to each other with the export of deionized water output tube of deionized water purification system, reforming hydrogen production device's reformed gas export links to each other with hydrogen fuel cell's positive pole import, reforming hydrogen production device's burning waste gas export links to each other with heat medium import of heat exchanger. The cogeneration system has a relatively simple structure, is miniaturized, is suitable for household use, and can well meet the requirements of civil use on electric power, heating and hot water.
Description
Technical Field
The invention relates to the field of reforming hydrogen production equipment, in particular to a small distributed cogeneration system.
Background
Environmental pollution and the constant consumption of non-renewable fossil fuels are the focus of global attention. The development of clean, efficient and sustainable new energy has become common knowledge. Hydrogen energy has become a clean energy source recognized by the market because of its advantages such as high combustion heat value, no pollution to the environment by combustion product water, etc.
With the global promotion of the construction of the hydrogen energy society, a small-sized cogeneration system which uses a hydrogen fuel cell as a main power generation body, can supply power and heat and is suitable for household or public places is urgently needed.
Disclosure of Invention
The technical problem to be solved by the invention is as follows: a small distributed cogeneration system which is small in size, uses a hydrogen fuel cell as a power generation main body, can supply power and heat, and is suitable for use in home or public places.
In order to solve the problems, the technical scheme adopted by the invention is as follows: a small scale distributed combined heat and power generation system comprising: reforming hydrogen plant, desulfurizer, hydrogen fuel cell, its characterized in that: further comprising: the device comprises a deionized water purification system, a gas-air mixer and a heat exchanger, wherein a feed gas inlet of a reforming hydrogen production device is connected with an outlet of a desulfurizer through a pipeline, an inlet of the desulfurizer is connected with a feed gas main pipe through a pipeline, a main fuel gas inlet of the reforming hydrogen production device is connected with an outlet of the gas-air mixer through a pipeline, a first inlet of the gas-air mixer is connected with the feed gas main pipe through a pipeline, a second inlet of the gas-air mixer is communicated with the atmosphere, a deionized water inlet of the reforming hydrogen production device is connected with an outlet of a deionized water output pipe of the deionized water purification system through a pipeline, a reforming gas outlet of the reforming hydrogen production device is connected with an anode inlet of a hydrogen fuel cell through a pipeline, and a combustion waste gas outlet of the reforming hydrogen.
Further, the foregoing small-sized distributed cogeneration system, wherein: the structure of the deionized water purification system comprises: the water inlet pipeline, the export of water inlet pipeline links to each other with reverse osmosis unit's import, and reverse osmosis unit's export passes through the pipeline and links to each other with the import of oxygen dissolving device, and oxygen dissolving device's export passes through the pipeline and links to each other with metal ion adsorption equipment's import, and metal ion adsorption equipment's export passes through the pipeline and links to each other with the import of deionized water output tube.
Further, the foregoing small-sized distributed cogeneration system, wherein: the pipeline between the reverse osmosis device and the dissolved oxygen removal device is provided with a primary filtering water storage tank, the outlet of the reverse osmosis device is connected with the primary filtering water storage tank through a pipeline, so that the filtered water of the reverse osmosis device can be discharged into the primary filtering water storage tank, the outlet of the primary filtering water storage tank is connected with the inlet of the dissolved oxygen removal device through a pipeline with a pump, and the water in the primary filtering water storage tank can be conveyed into the dissolved oxygen removal device through the pump.
Further, the foregoing small-sized distributed cogeneration system, wherein: be provided with a terminal aqua storage tank on the pipeline between metal ion adsorption equipment and deionized water output tube, metal ion adsorption equipment's export passes through the pipeline and links to each other with the terminal aqua storage tank for during the hydroenergy after metal ion adsorption equipment filters discharged to the terminal aqua storage tank, the import of deionized water output tube links to each other with the terminal aqua storage tank, makes the hydroenergy in the terminal aqua storage tank outwards export through the deionized water output tube.
Further, the foregoing small-sized distributed cogeneration system, wherein: the terminal water storage tank is connected with the primary filtering water storage tank through a pipeline, so that water in the terminal water storage tank can overflow into the primary filtering water storage tank.
Further, the foregoing small-sized distributed cogeneration system, wherein: the deionized water purification system further comprises: a wastewater disposal basin, reverse osmosis unit's waste discharge opening passes through the pipeline and links to each other with the wastewater disposal basin, make the waste water that reverse osmosis unit during operation produced can arrange into to the wastewater disposal basin in, the water storage tank of elementary filtration passes through the pipeline and links to each other with the wastewater disposal basin, make the hydroenergy overflow in the water storage tank of elementary filtration in to the wastewater disposal basin, the waste discharge opening that goes dissolved oxygen device links to each other with the wastewater disposal basin through the pipeline of taking the pump, make waste water and the waste residue that goes dissolved oxygen device during operation to produce can pass through the pump and deliver to the wastewater disposal basin in.
Further, the foregoing small-sized distributed cogeneration system, wherein: the reforming hydrogen production device is also provided with an air injection ring, the upper surface of the air injection ring is provided with a plurality of air injection holes arranged along the air injection ring, the air injection ring is positioned below the steam reforming reaction cavity of the reforming hydrogen production device, the air injection ring is also provided with a feeding pipe, raw materials and steam required by the steam reforming reaction are input into the air injection ring through the feeding pipe, and then the raw materials and the steam are upwards sprayed out from the air injection holes of the air injection ring and enter the steam reforming reaction cavity to carry out the steam reforming reaction.
Further, the foregoing small-sized distributed cogeneration system, wherein: spongy porous supporting bodies are filled in a steam reforming reaction cavity, a water vapor transfer catalytic reaction cavity and a selective methanation reaction cavity of the reforming hydrogen production device, and catalysts required by reaction in each reaction cavity are scattered and adhered to each hole wall of the spongy porous supporting body in the cavity in a powdery manner.
Further, the foregoing small-sized distributed cogeneration system, wherein: a steam reforming reaction cavity, a water vapor transfer catalytic reaction cavity and a selective methanation reaction cavity in the reforming hydrogen production device are vertically arranged from bottom to top in sequence, and reaction raw materials enter the steam reforming reaction cavity, the water vapor transfer catalytic reaction cavity and the selective methanation reaction cavity from bottom to top in sequence for reaction; reforming hydrogen plant's steam reforming reaction chamber, steam transfer catalytic reaction chamber, selectivity methanation reaction chamber is equallyd divide into upper and lower region and the lower region that butt joint the intercommunication from top to bottom, the lower region of each reaction chamber all dwindles by supreme down gradually, the upper region of each reaction chamber all enlarges by supreme down gradually, and the upper region of each reaction chamber still falls into the hypomere by supreme down in proper order, the middle section, the upper segment, the lower region and the upper region of each reaction chamber, hypomere and middle section, all separate with the mesh board between middle section and the upper segment, the spongy porous supporter is not filled in the lower region of each reaction chamber, all pack in each segmentation of the upper region of each reaction chamber has spongy porous supporter.
Further, the foregoing small-sized distributed cogeneration system, wherein: the total pore wall expanded area of the spongy porous support body at the lower section of each upper region is less than the total pore wall expanded area of the spongy porous support body at the middle section and less than the total pore wall expanded area of the spongy porous support body at the upper section.
The invention has the advantages that: compared with the traditional large central power generation and heating station, the small distributed cogeneration system can realize the value thereof more quickly, reduce the demand pressure on a power grid, and reduce the loss of electric power and heating during transmission and distribution; the natural gas water heater can normally work after being connected with natural gas and tap water pipelines in scenes such as households, communities, restaurants and the like, thereby well meeting the requirements of public places such as residential units, small communities, commercial or industrial buildings, hospitals and the like on illumination, electrical equipment, heating, hot water and the like.
Drawings
Fig. 1 is a schematic structural diagram of a small distributed cogeneration system according to the present invention.
Fig. 2 is a schematic structural diagram of a reforming hydrogen production apparatus.
FIG. 3 is a schematic view of the gas injection ring shown in FIG. 2.
Detailed Description
The present invention will be described in further detail below with reference to specific embodiments and the attached drawings.
As shown in fig. 1, a small distributed cogeneration system comprises: the device comprises a reforming hydrogen production device 1, a desulfurizer 2, a hydrogen fuel cell 3, a deionized water purification system 4, a fuel gas-air mixer 5 and a heat exchanger 6, wherein the reforming hydrogen production device 1 is an existing device capable of converting a hydrogen-containing compound into a hydrogen-containing reformed gas, and the existing reforming hydrogen production device is generally provided with a raw gas inlet for inputting natural gas, a main combustion gas inlet for inputting combustion gas, a deionized water inlet for inputting water, a combustion waste gas outlet for discharging combustion waste gas, a reformed gas outlet for outputting the reformed gas, a steam reforming reaction cavity for performing steam reforming reaction, a steam transfer catalytic reaction cavity for performing steam transfer catalytic reaction, a selective methanation reaction cavity for performing selective methanation reaction and a combustion cylinder for providing heat for each reaction by combustion fuel gas; in the embodiment, natural gas is used as a raw material to carry out reforming hydrogen production, and the process for producing hydrogen by reforming natural gas mainly comprises the following steps: firstly, steam reforming reaction: in the reaction, methane in natural gas reacts with steam in the presence of a steam reforming reaction catalyst to produce a primary reformed gas, which mainly contains hydrogen and carbon monoxide, and a large amount of heat needs to be absorbed in the step, and the temperature is usually maintained at 800-1000 ℃. Secondly, water vapor transfer catalytic reaction: in the reaction, carbon monoxide in the primary reformed gas reacts with water under the condition of a water-vapor transfer catalyst, so that the carbon monoxide in the primary reformed gas is removed to prepare a secondary reformed gas. The reaction requires controlling the temperature between 300 ℃ and 350 ℃. Thirdly, selective methanation reaction: in the reaction, under the condition of a selective methanation reaction catalyst, carbon monoxide in the secondary reformed gas is further reacted and removed, so that purified hydrogen is prepared; the reforming hydrogen production device 1 adopted in the embodiment can be an integrated reforming hydrogen production device disclosed in the patent with the patent number of 201910859068.8, and can also be other common small reforming hydrogen production devices; the feed gas inlet 11 of the reforming hydrogen production device 1 is connected with the outlet of the desulfurizer 2 through a pipeline, the inlet of the desulfurizer 2 is connected with the feed gas main pipe 7 through a pipeline, and when the reforming hydrogen production device works, the inlet of the feed gas main pipe 7 is communicated with a household natural gas pipeline, so that natural gas for reaction and natural gas for combustion heating can be provided for the reforming hydrogen production device 1, and the desulfurizer 2 contains a desulfurizer, so that the desulfurizer 2 can desulfurize the natural gas, so that sulfides in the natural gas are removed, the sulfides can not only react with hydrogen, but also poison a catalyst for catalyzing hydrogen production reaction, and the catalyst is ineffective; the main fuel gas inlet 12 of the reforming hydrogen production device 1 is connected with the outlet of the fuel gas air mixer 5 through a pipeline, the first inlet 51 of the fuel gas air mixer 5 is connected with the raw material gas main pipe 7 through a pipeline, the second inlet 52 of the fuel gas air mixer 5 is communicated with the atmosphere, the fuel gas air mixer 5 can be a mixing blower or a mixing pump, the combustion efficiency can be greatly improved after natural gas and air are premixed in the fuel gas air mixer 5, and the mixed natural gas and air enter the combustion cylinder of the reforming hydrogen production device 1 for combustion to provide heat for each reaction; a deionized water inlet 13 of the reforming hydrogen production device 1 is connected with an outlet of a deionized water output pipe 41 of the deionized water purification system 4 through a pipeline, and the deionized water purification system 4 provides the reforming hydrogen production device 1 with deionized water for reaction; the reformed gas outlet 14 of the reforming hydrogen production device 1 is connected with the anode inlet 31 of the hydrogen fuel cell 3 through a pipeline, so that the reforming hydrogen production device 1 can provide hydrogen for the hydrogen fuel cell 3, the combustion waste gas outlet 16 of the reforming hydrogen production device 1 is connected with the heat medium inlet of the heat exchanger 6 through a pipeline, so that the high-temperature combustion waste gas in the reforming hydrogen production device 1 can exchange heat with a refrigerant in the heat exchanger 6, the refrigerant is usually cold water or cold air, and thus warm air or hot water can be provided for an application scene.
In this embodiment, the reforming hydrogen production apparatus 1 is further provided with an auxiliary combustion gas inlet 15, the auxiliary combustion gas inlet 15 is communicated with the combustion cylinder of the reforming hydrogen production apparatus 1 through an internal pipeline, the auxiliary combustion gas inlet 15 is further connected with the anode outlet of the hydrogen fuel cell 3 through an external pipeline, in general, the hydrogen fuel cell 3 cannot completely consume all hydrogen in the reforming gas, in this embodiment, the tail gas of the unreacted fuel cell containing hydrogen can enter the combustion cylinder through the auxiliary combustion gas inlet 15 to be combusted, so that natural gas can be saved.
In addition, an exhaust pipeline with a stop valve is communicated with the reformed gas outlet 14 of the reforming hydrogen production device 1, and the exhaust pipeline can exhaust the reformed gas which does not reach the standard during startup.
A mass flow meter, a booster pump and a natural gas proportional valve are sequentially arranged on the pipeline between the desulfurizer 2 and the feed gas inlet 11 along the flowing direction. A peristaltic pump and a mass flow meter are sequentially arranged on the pipeline between the deionized water output pipe 41 and the deionized water inlet 13 along the flow direction.
In the present embodiment, the structure of the deionized water purification system 4 includes: the water inlet pipeline 42, during operation, the import of water inlet pipeline 42 is linked together with the water pipe, and the export of water inlet pipeline 42 links to each other with reverse osmosis unit 43's import, and reverse osmosis unit 43's export links to each other with the import of oxygen dissolving removal device 44 through the pipeline, and the export of oxygen dissolving removal device 44 passes through the pipeline and links to each other with the import of metal ion adsorption equipment 45, and the export of metal ion adsorption equipment 45 passes through the pipeline and links to each other with the import of deionized water output tube 41. The reverse osmosis device 43 removes large-particle impurities in tap water by the reverse osmosis principle, the dissolved oxygen removing device 44 is used for removing dissolved gas in the tap water and sucking out some fine impurities, and the principle of the dissolved oxygen removing device 44 is as follows: the solubility of each gas in water decreases with increasing temperature or decreasing pressure. When the water temperature reaches the boiling point, the water vapor pressure on the water interface is equal to the external pressure, and the water no longer has the capacity of dissolving gas, namely, various gases are desorbed and separated because the gases cannot be dissolved in the water. According to different working pressures, the vacuum type is selected in the embodiment, so that the discharge of gas in liquid is accelerated, and fine impurities are sucked out at the same time. The metal ion adsorption device 45 removes metal ions in the tap water by a built-in metal ion adsorbent, and the tap water becomes deionized water after reverse osmosis, dissolved oxygen removal and metal ion adsorption.
In addition, a primary filtering water storage tank 46 is provided on a pipeline between the reverse osmosis device 43 and the dissolved oxygen removal device 44, an outlet of the reverse osmosis device 43 is connected to the primary filtering water storage tank 46 through a pipeline so that water filtered by the reverse osmosis device 43 can be discharged into the primary filtering water storage tank 46, and an outlet of the primary filtering water storage tank 46 is connected to an inlet of the dissolved oxygen removal device 44 through a pipeline with a diaphragm pump so that water in the primary filtering water storage tank 46 can be transferred to the dissolved oxygen removal device 44 through a pump.
Be provided with a terminal aqua storage tank 47 on the pipeline between metal ion adsorption equipment 45 and deionized water output tube 41, metal ion adsorption equipment 45's export passes through the pipeline and links to each other with terminal aqua storage tank 47 for during the hydroenergy after metal ion adsorption equipment 45 filters is arranged into terminal aqua storage tank 47, the import of deionized water output tube 41 links to each other with terminal aqua storage tank 47, makes the hydroenergy in the terminal aqua storage tank 47 outwards export through deionized water output tube 41.
The deionized water purification system 4 further includes: and the waste water tank 48 is connected with a waste water outlet of the reverse osmosis device 43 through a pipeline, so that waste water generated when the reverse osmosis device 43 works can be discharged into the waste water tank 48, the primary filtering water storage tank 46 is connected with the waste water tank 48 through a pipeline, so that water in the primary filtering water storage tank 46 can overflow into the waste water tank 48, and the waste water outlet of the dissolved oxygen removing device 44 is connected with the waste water tank 48 through a pipeline with a vacuum pump, so that waste water and waste residues generated when the dissolved oxygen removing device 44 works can be conveyed into the waste water tank 48 through a pump.
The final sump 47 and the primary filtering sump 46 are connected by a pipe so that the water in the final sump 47 can overflow into the primary filtering sump 46. All be provided with the liquid level switch of control liquid level in terminal aqua storage tank 47, elementary filtration aqua storage tank 46, the wastewater disposal basin 48, still be provided with the probe that detects conductivity and resistivity in the terminal aqua storage tank 47, can discharge in overflowing to wastewater disposal basin 48 when the water in terminal aqua storage tank 47 and elementary filtration aqua storage tank 46 is too much, can increase the reliability of system like this.
When the device works, the inlet of the raw material gas main pipe 7 is communicated with a household natural gas pipeline, the inlet of the water inlet pipeline 42 is communicated with a tap water pipe, a part of natural gas and air are mixed and then enter a combustion cylinder through a pipeline to be combusted to provide heat for each reaction, deionized water supplied by the deionized water purification system 4 enters the reforming hydrogen production device 1 to be heated and evaporated into steam, then the steam and the other part of natural gas are mixed and then enter a steam reforming reaction cavity to be subjected to steam reforming reaction, then primary reformed gas enters a steam transfer catalytic reaction cavity to be subjected to steam transfer catalytic reaction, then secondary reformed gas enters a selective methanation reaction cavity to be subjected to selective methanation reaction, so as to prepare reformed gas with high-purity hydrogen, the prepared reformed gas is introduced into a hydrogen fuel cell to generate electric energy for users to use, and high-temperature combustion waste gas generated by the reforming device 1 and cold water or cold air in the heat exchanger 6 are subjected to hydrogen production And heat exchange is carried out, so that warm air or hot water can be provided for the operation scene.
As shown in fig. 2 and 3, a gas injection ring 8 is further provided in the reforming hydrogen production apparatus 1, a plurality of gas injection holes 81 are uniformly arranged along the gas injection ring 8 on the upper surface of the gas injection ring 8, the gas injection ring 8 is located below the steam reforming reaction chamber 9 of the reforming hydrogen production apparatus 1, a feed pipe 82 is further provided on the gas injection ring 8, and natural gas and steam required for the steam reforming reaction are input into the gas injection ring 8 through the feed pipe 82 and then are ejected upwards from the gas injection holes 81 of the gas injection ring 8 and enter the steam reforming reaction chamber 9 for the steam reforming reaction. After the gas injection ring 8 is arranged, the natural gas and the steam can be premixed in the gas injection ring 8, and the obtained mixed gas can be uniformly distributed and enter the steam reforming reaction cavity 9 for reaction, so that the steam reforming reaction can be better carried out.
Sponge-like porous supporting bodies 83 are filled in the steam reforming reaction cavity 9, the water vapor transfer catalytic reaction cavity 91 and the selective methanation reaction cavity 92 of the reforming hydrogen production device 1, and catalysts required by the reaction in each reaction cavity are dispersed and adhered to the pore walls of the sponge-like porous supporting bodies 83 in the cavity in a powder form. The original catalyst is piled in a reaction cavity in a granular form, in order to ensure that reaction gas can smoothly pass through a catalyst layer to be catalyzed by the catalyst, the granularity of the catalyst cannot be too small, so that only the surface layer of the large-granular catalyst participates in catalytic reaction, the inside of the catalyst can be wasted, the catalyst is scattered in a powdery form and adhered to each pore wall of the spongy porous support body 83, the fluidity of the reaction gas is ensured, and the catalyst can be fully utilized.
The catalyst dispersed and adhered in powder form to each cell wall of the sponge-like porous support 83 can be obtained by: the sponge-like porous support 83 is immersed in the catalyst slurry so that the sponge-like porous support 83 sufficiently absorbs the slurry, and then the sponge-like porous support 83 is dried.
The steam reforming reaction cavity 9, the water vapor transfer catalytic reaction cavity 91 and the selective methanation reaction cavity 92 in the reforming hydrogen production device 1 are vertically arranged from bottom to top in sequence, and reaction raw materials enter the steam reforming reaction cavity 9, the water vapor transfer catalytic reaction cavity 91 and the selective methanation reaction cavity 92 from bottom to top in sequence for reaction; the steam reforming reaction cavity 9, the water vapor transfer catalytic reaction cavity 91 and the selective methanation reaction cavity 92 of the reforming hydrogen production device 1 are respectively divided into an upper area 93 and a lower area 94 which are in butt joint and communicated up and down, the lower area 93 of each reaction cavity is gradually reduced from bottom to top, the upper area 94 of each reaction cavity is gradually enlarged from bottom to top, the upper area 94 of each reaction cavity is further sequentially divided into a lower section 941, a middle section 942 and an upper section 943 from bottom to top, the lower area 93 and the upper area 94 of each reaction cavity, the lower section 941 and the middle section 942, the middle section 942 and the upper section 943 of each reaction cavity are separated by a mesh plate, the lower area 93 of each reaction cavity is not filled with a spongy porous support 83, each section of the upper area 94 of each reaction cavity is filled with a spongy porous support 83, and the total pore wall expansion area of the spongy porous support 83 of the lower section 941 of each upper area 94 is less than the total pore wall expansion area of the spongy porous support 83 of the middle section is less than that of the spongy porous support 83 of the The cell walls of struts 83 expand in total area. The lower region 93 can play a role in gathering reaction gas after being gradually reduced from bottom to top, so that the reaction can be efficiently carried out; the upper region 94 is gradually enlarged from bottom to top to accelerate the flow of the reaction gas, thereby improving the reaction efficiency and preventing the reaction gas from flowing back, so that the reaction gas moves forward in a single direction, and the disorder of the gas inside the reaction chamber is avoided. The total expanded pore wall area of the sponge-like porous support 83 in the lower 941, middle 942, and upper 943 sections is gradually increased, and the larger the total expanded pore wall area, the more catalyst adheres, so that the amount of catalyst in the lower 941 is less than the amount of catalyst in the middle 942 than the amount of catalyst in the upper 943, and when the reaction gas enters the lower 941 section, the more reactant in the reaction gas, which may affect the reaction due to the severe temperature fluctuation caused by excessive reaction, and the reaction intensity is reduced by reducing the amount of catalyst in the lower 941 section, and when the reaction gas enters the middle 942 and upper 943 sections, the reactant in the reaction gas is reduced by sequentially reducing a part of the reactant due to the reaction, so that the amounts of catalyst in the middle 942 and upper 943 sections can be properly and sequentially increased to ensure that the reactant in the reaction gas can fully react, and at the same time, the lower 941 section, the upper section, and the catalyst, The reaction strengths in the middle section 942 and the upper section 943 can be made uniform, thereby ensuring uniformity of the temperature inside the chamber.
Claims (10)
1. A small scale distributed combined heat and power generation system comprising: reforming hydrogen plant, desulfurizer, hydrogen fuel cell, its characterized in that: further comprising: the device comprises a deionized water purification system, a gas-air mixer and a heat exchanger, wherein a feed gas inlet of a reforming hydrogen production device is connected with an outlet of a desulfurizer through a pipeline, an inlet of the desulfurizer is connected with a feed gas main pipe through a pipeline, a main fuel gas inlet of the reforming hydrogen production device is connected with an outlet of the gas-air mixer through a pipeline, a first inlet of the gas-air mixer is connected with the feed gas main pipe through a pipeline, a second inlet of the gas-air mixer is communicated with the atmosphere, a deionized water inlet of the reforming hydrogen production device is connected with an outlet of a deionized water output pipe of the deionized water purification system through a pipeline, a reforming gas outlet of the reforming hydrogen production device is connected with an anode inlet of a hydrogen fuel cell through a pipeline, and a combustion waste gas outlet of the reforming hydrogen.
2. A small scale distributed combined heat and power generation system according to claim 1, wherein: the structure of the deionized water purification system comprises: the water inlet pipeline, the export of water inlet pipeline links to each other with reverse osmosis unit's import, and reverse osmosis unit's export passes through the pipeline and links to each other with the import of oxygen dissolving device, and oxygen dissolving device's export passes through the pipeline and links to each other with metal ion adsorption equipment's import, and metal ion adsorption equipment's export passes through the pipeline and links to each other with the import of deionized water output tube.
3. A small scale distributed combined heat and power generation system according to claim 2, wherein: the pipeline between the reverse osmosis device and the dissolved oxygen removal device is provided with a primary filtering water storage tank, the outlet of the reverse osmosis device is connected with the primary filtering water storage tank through a pipeline, so that the filtered water of the reverse osmosis device can be discharged into the primary filtering water storage tank, the outlet of the primary filtering water storage tank is connected with the inlet of the dissolved oxygen removal device through a pipeline with a pump, and the water in the primary filtering water storage tank can be conveyed into the dissolved oxygen removal device through the pump.
4. A small scale distributed combined heat and power generation system according to claim 3, wherein: be provided with a terminal aqua storage tank on the pipeline between metal ion adsorption equipment and deionized water output tube, metal ion adsorption equipment's export passes through the pipeline and links to each other with the terminal aqua storage tank for during the hydroenergy after metal ion adsorption equipment filters discharged to the terminal aqua storage tank, the import of deionized water output tube links to each other with the terminal aqua storage tank, makes the hydroenergy in the terminal aqua storage tank outwards export through the deionized water output tube.
5. A small scale distributed combined heat and power generation system according to claim 4, wherein: the terminal water storage tank is connected with the primary filtering water storage tank through a pipeline, so that water in the terminal water storage tank can overflow into the primary filtering water storage tank.
6. A small scale distributed combined heat and power generation system according to claim 5, wherein: the deionized water purification system further comprises: a wastewater disposal basin, reverse osmosis unit's waste discharge opening passes through the pipeline and links to each other with the wastewater disposal basin, make the waste water that reverse osmosis unit during operation produced can arrange into to the wastewater disposal basin in, the water storage tank of elementary filtration passes through the pipeline and links to each other with the wastewater disposal basin, make the hydroenergy overflow in the water storage tank of elementary filtration in to the wastewater disposal basin, the waste discharge opening that goes dissolved oxygen device links to each other with the wastewater disposal basin through the pipeline of taking the pump, make waste water and the waste residue that goes dissolved oxygen device during operation to produce can pass through the pump and deliver to the wastewater disposal basin in.
7. A small scale distributed combined heat and power generation system according to claim 1 or 2 or 3 or 4 or 5 or 6, characterized in that: the reforming hydrogen production device is also provided with an air injection ring, the upper surface of the air injection ring is provided with a plurality of air injection holes arranged along the air injection ring, the air injection ring is positioned below the steam reforming reaction cavity of the reforming hydrogen production device, the air injection ring is also provided with a feeding pipe, raw materials and steam required by the steam reforming reaction are input into the air injection ring through the feeding pipe, and then the raw materials and the steam are upwards sprayed out from the air injection holes of the air injection ring and enter the steam reforming reaction cavity to carry out the steam reforming reaction.
8. A small scale distributed combined heat and power generation system according to claim 7, wherein: spongy porous supporting bodies are filled in a steam reforming reaction cavity, a water vapor transfer catalytic reaction cavity and a selective methanation reaction cavity of the reforming hydrogen production device, and catalysts required by reaction in each reaction cavity are scattered and adhered to each hole wall of the spongy porous supporting body in the cavity in a powdery manner.
9. A small scale distributed combined heat and power generation system according to claim 8, wherein: a steam reforming reaction cavity, a water vapor transfer catalytic reaction cavity and a selective methanation reaction cavity in the reforming hydrogen production device are vertically arranged from bottom to top in sequence, and reaction raw materials enter the steam reforming reaction cavity, the water vapor transfer catalytic reaction cavity and the selective methanation reaction cavity from bottom to top in sequence for reaction; reforming hydrogen plant's steam reforming reaction chamber, steam transfer catalytic reaction chamber, selectivity methanation reaction chamber is equallyd divide into upper and lower region and the lower region that butt joint the intercommunication from top to bottom, the lower region of each reaction chamber all dwindles by supreme down gradually, the upper region of each reaction chamber all enlarges by supreme down gradually, and the upper region of each reaction chamber still falls into the hypomere by supreme down in proper order, the middle section, the upper segment, the lower region and the upper region of each reaction chamber, hypomere and middle section, all separate with the mesh board between middle section and the upper segment, the spongy porous supporter is not filled in the lower region of each reaction chamber, all pack in each segmentation of the upper region of each reaction chamber has spongy porous supporter.
10. A small scale distributed combined heat and power generation system according to claim 9, wherein: the total pore wall expanded area of the spongy porous support body at the lower section of each upper region is less than the total pore wall expanded area of the spongy porous support body at the middle section and less than the total pore wall expanded area of the spongy porous support body at the upper section.
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