CN117329896A - Three-layer fluidized bed calcium-based thermochemical hydration exothermic reaction device and working method - Google Patents
Three-layer fluidized bed calcium-based thermochemical hydration exothermic reaction device and working method Download PDFInfo
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- CN117329896A CN117329896A CN202311347578.XA CN202311347578A CN117329896A CN 117329896 A CN117329896 A CN 117329896A CN 202311347578 A CN202311347578 A CN 202311347578A CN 117329896 A CN117329896 A CN 117329896A
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- 238000006243 chemical reaction Methods 0.000 title claims abstract description 64
- 239000011575 calcium Substances 0.000 title claims abstract description 63
- 238000006703 hydration reaction Methods 0.000 title claims abstract description 56
- 230000036571 hydration Effects 0.000 title claims abstract description 42
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 title claims abstract description 22
- 229910052791 calcium Inorganic materials 0.000 title claims abstract description 22
- 238000000034 method Methods 0.000 title claims abstract description 17
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 117
- 239000002245 particle Substances 0.000 claims abstract description 47
- 239000007787 solid Substances 0.000 claims abstract description 30
- 238000010438 heat treatment Methods 0.000 claims abstract description 20
- 238000007599 discharging Methods 0.000 claims abstract description 14
- 230000008569 process Effects 0.000 claims abstract description 8
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 54
- 239000007789 gas Substances 0.000 claims description 42
- 238000003860 storage Methods 0.000 claims description 33
- 239000007788 liquid Substances 0.000 claims description 30
- 229910052757 nitrogen Inorganic materials 0.000 claims description 27
- 238000009827 uniform distribution Methods 0.000 claims description 24
- 238000010926 purge Methods 0.000 claims description 16
- 238000012546 transfer Methods 0.000 claims description 14
- 238000012856 packing Methods 0.000 claims description 13
- 239000000945 filler Substances 0.000 claims description 9
- 238000004321 preservation Methods 0.000 claims description 7
- 230000001105 regulatory effect Effects 0.000 claims description 7
- 238000009826 distribution Methods 0.000 claims description 6
- 239000012265 solid product Substances 0.000 claims description 6
- 239000000126 substance Substances 0.000 claims description 6
- 238000004140 cleaning Methods 0.000 claims description 2
- 238000004146 energy storage Methods 0.000 abstract description 18
- 239000013618 particulate matter Substances 0.000 abstract 1
- 239000010410 layer Substances 0.000 description 253
- 239000000292 calcium oxide Substances 0.000 description 36
- ODINCKMPIJJUCX-UHFFFAOYSA-N calcium oxide Inorganic materials [Ca]=O ODINCKMPIJJUCX-UHFFFAOYSA-N 0.000 description 36
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 6
- 238000000354 decomposition reaction Methods 0.000 description 6
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 6
- 230000009471 action Effects 0.000 description 5
- 238000005516 engineering process Methods 0.000 description 5
- 230000005484 gravity Effects 0.000 description 5
- 238000005338 heat storage Methods 0.000 description 5
- 239000000463 material Substances 0.000 description 5
- 229910001220 stainless steel Inorganic materials 0.000 description 5
- 239000010935 stainless steel Substances 0.000 description 5
- 238000011161 development Methods 0.000 description 4
- 230000000694 effects Effects 0.000 description 4
- 238000005243 fluidization Methods 0.000 description 4
- 230000002441 reversible effect Effects 0.000 description 4
- 238000010521 absorption reaction Methods 0.000 description 3
- 229910021529 ammonia Inorganic materials 0.000 description 3
- 230000001276 controlling effect Effects 0.000 description 3
- 230000002349 favourable effect Effects 0.000 description 3
- 230000009467 reduction Effects 0.000 description 3
- 238000006722 reduction reaction Methods 0.000 description 3
- 238000002407 reforming Methods 0.000 description 3
- VTYYLEPIZMXCLO-UHFFFAOYSA-L Calcium carbonate Chemical compound [Ca+2].[O-]C([O-])=O VTYYLEPIZMXCLO-UHFFFAOYSA-L 0.000 description 2
- BVKZGUZCCUSVTD-UHFFFAOYSA-L Carbonate Chemical compound [O-]C([O-])=O BVKZGUZCCUSVTD-UHFFFAOYSA-L 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 2
- 230000008901 benefit Effects 0.000 description 2
- 230000015572 biosynthetic process Effects 0.000 description 2
- BRPQOXSCLDDYGP-UHFFFAOYSA-N calcium oxide Chemical compound [O-2].[Ca+2] BRPQOXSCLDDYGP-UHFFFAOYSA-N 0.000 description 2
- 230000008859 change Effects 0.000 description 2
- 238000004134 energy conservation Methods 0.000 description 2
- 230000007613 environmental effect Effects 0.000 description 2
- 239000001257 hydrogen Substances 0.000 description 2
- 229910052739 hydrogen Inorganic materials 0.000 description 2
- 239000002440 industrial waste Substances 0.000 description 2
- 229910052751 metal Inorganic materials 0.000 description 2
- 239000002184 metal Substances 0.000 description 2
- 229910052987 metal hydride Inorganic materials 0.000 description 2
- 150000004681 metal hydrides Chemical class 0.000 description 2
- 229910000000 metal hydroxide Inorganic materials 0.000 description 2
- 150000004692 metal hydroxides Chemical class 0.000 description 2
- 229910044991 metal oxide Inorganic materials 0.000 description 2
- 150000004706 metal oxides Chemical class 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 238000007086 side reaction Methods 0.000 description 2
- 239000008247 solid mixture Substances 0.000 description 2
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 229910000019 calcium carbonate Inorganic materials 0.000 description 1
- -1 calcium carbonate) Chemical class 0.000 description 1
- 239000000920 calcium hydroxide Substances 0.000 description 1
- 229910001861 calcium hydroxide Inorganic materials 0.000 description 1
- KIZFHUJKFSNWKO-UHFFFAOYSA-M calcium monohydroxide Chemical compound [Ca]O KIZFHUJKFSNWKO-UHFFFAOYSA-M 0.000 description 1
- 150000004649 carbonic acid derivatives Chemical class 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 238000010924 continuous production Methods 0.000 description 1
- 125000004122 cyclic group Chemical group 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000006297 dehydration reaction Methods 0.000 description 1
- 238000006356 dehydrogenation reaction Methods 0.000 description 1
- 238000010612 desalination reaction Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 229910001873 dinitrogen Inorganic materials 0.000 description 1
- 238000001035 drying Methods 0.000 description 1
- 230000002708 enhancing effect Effects 0.000 description 1
- 150000002431 hydrogen Chemical class 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-M hydroxide Chemical compound [OH-] XLYOFNOQVPJJNP-UHFFFAOYSA-M 0.000 description 1
- 231100000252 nontoxic Toxicity 0.000 description 1
- 230000003000 nontoxic effect Effects 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 239000011148 porous material Substances 0.000 description 1
- 238000010248 power generation Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 238000006479 redox reaction Methods 0.000 description 1
- 238000005057 refrigeration Methods 0.000 description 1
- 239000000523 sample Substances 0.000 description 1
- 239000013535 sea water Substances 0.000 description 1
- 239000002356 single layer Substances 0.000 description 1
- 238000005245 sintering Methods 0.000 description 1
- 238000005979 thermal decomposition reaction Methods 0.000 description 1
- 230000001988 toxicity Effects 0.000 description 1
- 231100000419 toxicity Toxicity 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
Classifications
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
- F28D20/00—Heat storage plants or apparatus in general; Regenerative heat-exchange apparatus not covered by groups F28D17/00 or F28D19/00
- F28D20/003—Heat storage plants or apparatus in general; Regenerative heat-exchange apparatus not covered by groups F28D17/00 or F28D19/00 using thermochemical reactions
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F24—HEATING; RANGES; VENTILATING
- F24H—FLUID HEATERS, e.g. WATER OR AIR HEATERS, HAVING HEAT-GENERATING MEANS, e.g. HEAT PUMPS, IN GENERAL
- F24H7/00—Storage heaters, i.e. heaters in which the energy is stored as heat in masses for subsequent release
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F24—HEATING; RANGES; VENTILATING
- F24H—FLUID HEATERS, e.g. WATER OR AIR HEATERS, HAVING HEAT-GENERATING MEANS, e.g. HEAT PUMPS, IN GENERAL
- F24H9/00—Details
- F24H9/18—Arrangement or mounting of grates or heating means
- F24H9/1809—Arrangement or mounting of grates or heating means for water heaters
Landscapes
- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Physics & Mathematics (AREA)
- Thermal Sciences (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Combustion & Propulsion (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
Abstract
The invention relates to a three-layer fluidized bed calcium-based thermochemical hydration exothermic reaction device and a working method thereof, and relates to the technical field of calcium-based thermochemical energy storage. Comprises a feeding subsystem, a fluidized bed reactor, a discharging subsystem, a heat conduction oil heat exchange subsystem and a water vapor supply subsystem; the feeding subsystem is communicated with the fluidized bed reactor and is used for providing CaO solid particles into the fluidized bed reactor; the discharge subsystem is communicated with the fluidized bed reactor for adding Ca (OH) 2 Solid particulate matter discharge means; the conduction oil heat exchange subsystem is used for conveying conduction oil for heat exchange in the hydration reaction process; the water vapor supply subsystem provides water vapor to enable CaO to generate hydration exothermic reaction; the fluidized bed reactor is used for providing a place where CaO and water vapor react with hydration exotherm. The invention can realize one-time heating or connection of the heat conduction oilThe temperature of the heat conduction oil can be adjusted after heating for a plurality of times, so as to obtain the oil quantity of the heat conduction oil with low, medium and high temperature ranges to the maximum extent.
Description
Technical Field
The invention relates to the technical field of water bath devices, in particular to a three-layer fluidized bed calcium-based thermochemical hydration exothermic reaction device and a working method.
Background
With the continuous exhaustion of fossil energy, the problem of energy utilization becomes one of the core problems of future development, and the expansion of new energy utilization is urgent. The solar energy is inexhaustible, and is used as a completely clean energy source without discharging any polluted gas and harmful substances, so that the solar energy gradually becomes a focus point for new energy development and utilization. At present, solar heat is mainly applied to various fields such as power generation, drying, refrigeration, sea water desalination and the like. In addition, the utilization of industrial waste heat is also an important measure for energy conservation and emission reduction of enterprises. The industrial waste heat is recycled, so that the grading utilization can be realized, and the benefit maximization is realized.
According to the energy storage principle, the high temperature energy storage technology can be classified into sensible heat storage, latent heat storage and thermochemical storage. Sensible heat storage is realized based on the temperature change of a heat storage medium, and has the advantages of lower heat storage cost, simple technology, larger heat loss, short energy storage period and most wide application at present. The latent heat energy storage realizes energy storage based on medium phase change absorption and heat release, and the energy storage density is medium. The thermochemical energy storage realizes energy storage through reversible chemical reaction absorption and heat release of a medium, has maximum energy storage density and basically no heat loss, and has good application prospect.
At present, the thermochemical energy storage technology is mainly based on reversible reaction absorption and heat release to realize energy storage, and common thermochemical energy storage systems comprise an ammonia decomposition system, a methane reforming system, a metal carbonate system, a metal hydroxide system, a metal hydride system, a metal oxide system, a calcium oxide/calcium hydroxide system and the like. The ammonia decomposition system adopts the reversible reaction of reacting nitrogen with hydrogen to generate ammonia, has no side reaction and large energy storage density, but needs to consider the problems of large storage and reaction pressure of nitrogen and hydrogen, and has high operation cost. The methane reforming system adopts a reversible reaction of methane reforming, has high energy storage density, but has poor reversibility and side reaction. Metal carbonate systems are based mainly on the thermal decomposition reaction of carbonates (such as calcium carbonate), which are low in material cost but lower in decomposition rate and have sintering problems, and are not suitable for continuous production. The metal hydroxide is based on hydroxide decomposition dehydration reaction, is nontoxic and free of byproducts, has poor reaction activity, and is suitable for industrial application. The metal hydride system is mainly based on MgH 2 The decomposition dehydrogenation reaction of (2) has high energy storage density but lower working temperature. The metal oxide system is mainly based on the oxidation-reduction reaction of oxides to generate oxygen, and a heat exchanger and a gas storage device are not needed, but the material cost is high and a certain toxicity exists.
Therefore, how to provide a three-layer fluidized bed calcium-based thermochemical hydration exothermic reaction device and a working method thereof solves the problems that in the prior art, low, medium and high temperature grade heat conduction oil is difficult to obtain simultaneously, and can solve the problems that in the prior fixed bed technology, the contact area of particles and water vapor is difficult to be large, the hydration reaction rate is low and the reaction is incomplete, and becomes a technical problem which needs to be solved urgently by the technicians in the field.
Disclosure of Invention
The invention aims to solve the technical problems of overcoming the defects of the prior art, and provides a three-layer fluidized bed calcium-based thermochemical hydration exothermic reaction device and a working method thereof, which can realize one-time heating or continuous repeated heating of heat conduction oil, and can adjust the temperature of the heat conduction oil so as to obtain the heat conduction oil quantity of low, medium and high temperature grades to the maximum extent; the reactor adopts a three-layer fluidized bed structure, improves the space utilization rate, and is favorable for enhancing the heat transfer and mass transfer effects, thereby fully carrying out the hydration exothermic reaction.
In order to achieve the aim, the invention provides a three-layer fluidized bed calcium-based thermochemical hydration exothermic reaction device, which comprises: the device comprises a feeding subsystem, a fluidized bed reactor, a discharging subsystem, a heat conduction oil heat exchange subsystem and a water vapor supply subsystem; the fluidized bed reactor is arranged in a three-layer structure, and the feeding subsystem is communicated with one side of the fluidized bed reactor of each layer through a pipeline and is used for providing CaO solid particles into the fluidized bed reactor; the material outlet subsystem is communicated with the other side of the fluidized bed reactor of each layer through a pipeline and is used for collecting Ca (OH) generated by hydration reaction 2 Store a certain amount of Ca (OH) 2 Then timing Ca (OH) 2 Solid particle discharge means; the heat transfer oil heat exchange subsystem is used for conveying heat transfer oil used for heat exchange in the hydration reaction process, and coils of the heat transfer oil heat exchange subsystem are distributed in the middle area of each layer of fluidized bed; the water vapor supply subsystem is directly communicated with the bottom of the fluidized bed reactor through a pipeline, and provides water vapor to enable CaO solid in the fluidized bed reactor to be in fluidized distribution and fully contact with the CaO solid, so that hydration exothermic reaction occurs, and chemical energy stored in the CaO is released; the fluidized bed reactor is used for providing a place where CaO and water vapor react with hydration exotherm.
Further, the feed subsystem includes: the screw feeder, the first feeding pipe, the second feeding pipe and the third feeding pipe are respectively provided with regulating valves; after the whole fluidized bed reactor is filled with water vapor, caO solid particles are fed by a screw feeder and then are respectively conveyed to the fluidized bed reactors of the first layer, the second layer and the third layer along the first feeding pipe, the second feeding pipe and the third feeding pipe to carry out hydration exothermic reaction.
Further, the fluidized bed reactor includes: reactor body, heat preservation layer, first gas equipartition board, second gas equipartition board, third gas equipartition board, packing layer, steam outlet pipe, first Ca (OH) 2 Exhaust valve and second Ca (OH) 2 A purge port valve; the heat preservation layer is coated on the outer wall of the reactor body, and the first gas uniform distribution plate, the second gas uniform distribution plate and the third gas uniform distribution plate are plates with the aperture smaller than the diameter of CaO solid particles and are fixed on the inner wall of the inner cavity of the reactor body so as to divide the reactor body into three layers; the top end of the reactor body is connected with a water vapor outlet pipe, and a filler layer is arranged at the inlet of the water vapor outlet pipe; the two sides of the bottom end of the reactor body are provided with first Ca (OH) 2 Purge gate valve and second Ca (OH) 2 A valve for discharging the waste water.
Further, the outfeed subsystem comprises: the device comprises a first funnel, a first discharge valve, a first storage tank, a second funnel, a second discharge valve, a second storage tank, a third funnel, a third discharge valve and a third storage tank; the first hopper is communicated with the reactor body of the first layer, and a first discharge valve is arranged on a pipeline for communicating the first hopper with the first storage tank; the second hopper is communicated with the reactor body of the second layer, and a second discharge valve is arranged on a pipeline for communicating the second hopper with the second storage tank; the third funnel is communicated with the reactor body of the first layer, and a third discharge valve is arranged on a pipeline for communicating the third funnel with the third storage tank.
Further, the conduction oil heat exchange subsystem includes: a first layer inlet pipe, a second layer inlet pipe, a third layer inlet pipe, a first coil pipe, a second coil pipe, a third coil pipe, a first layer outlet pipe, a second layer outlet pipe, a third layer outlet pipe, a first layer oil inlet valve, a second layer oil inlet valve, a third layer oil inlet valve, a first layer oil outlet valve, a second layer oil outlet valve, a third layer oil outlet valve, a first check valve and a second check valve; the first coil pipe, the second coil pipe and the third coil pipe are respectively arranged in the middle area of the reactor body of each layer; the first layer outlet pipe is connected with the second layer inlet pipe through a pipeline and is communicated with the second layer inlet pipe through a first check valve, the second layer outlet pipe is connected with the third layer inlet pipe through a pipeline and is communicated with the third layer inlet pipe through a second check valve, and the first layer inlet pipe, the second layer inlet pipe and the third layer inlet pipe are respectively provided with a first layer oil inlet valve, a second layer oil inlet valve and a third layer oil inlet valve; the first layer outlet pipe, the second layer outlet pipe and the third layer outlet pipe are respectively provided with a first layer oil outlet valve, a second layer oil outlet valve and a third layer oil outlet valve.
Further, the water vapor supply subsystem includes: a water vapor inlet pipe, a heater, a liquid water inlet pipe, a liquid water inlet control valve and a water vapor control valve; one end of the heater is communicated with the bottom of the fluidized bed reactor through a water vapor inlet pipe, a water vapor control valve is arranged on the water vapor inlet pipe, the other end of the heater is connected with a liquid water inlet pipe, and a liquid water inlet control valve is arranged on the liquid water inlet pipe.
Further, a vibrator is arranged on the side wall of the water vapor outlet pipe, and the vibrator can generate pulse vibration force so as to clear scale on the internal parts of the fluidized bed reactor periodically.
Further, the water vapor outlet pipe is communicated with a nitrogen inlet pipeline through a tee joint and a nitrogen inlet valve, high-pressure pulse nitrogen with the pressure of 0-1.0 MPa is regularly introduced into the pipeline, the high-pressure pulse nitrogen is blown to the filler layer through the water vapor outlet pipe, and the generated pulse nitrogen flow regularly eliminates particulate matters in the filler layer.
Further, the fluidized bed reactor further comprises: the three-layer reactor comprises a first baffle, a second baffle and a third baffle, wherein the first baffle, the second baffle and the third baffle are respectively arranged at the positions communicated with a discharging subsystem in the three-layer reactor body.
The working method of the three-layer fluidized bed calcium-based thermochemical hydration exothermic reaction device comprises the following steps:
s1: opening a liquid water inlet control valve, heating liquid water in a heater from an inlet pipe to obtain water vapor with a certain pressure, and opening the water vapor inlet control valve when the set pressure is reached, wherein the water vapor enters the inner cavity of the fluidized bed reactor from the bottom through the water vapor inlet pipe;
s2: starting a screw feeder, and uniformly conveying CaO particles into the first layer, the second layer and the third layer of fluidized bed reactors along the first feeding pipe, the second feeding pipe and the third feeding pipe to carry out hydration exothermic reaction;
S3: to obtain low-temperature heat conduction oil: the normal-temperature cold oil with the flow rate Q enters the first fluidized bed reactor from the first layer inlet pipe to complete heat exchange, the first layer oil outlet valve is opened, the first check valve is closed, and the low-temperature heat conduction oil flows out along the first layer outlet pipe to obtain low-temperature heat conduction oil which is heated once; opening a second-layer oil inlet valve and a second-layer oil outlet valve, closing a second check valve, and enabling normal-temperature cold oil with the flow rate Q to flow out along a second-layer outlet pipe after entering a second-layer fluidized bed from a second-layer inlet pipe to complete heat exchange; opening a third layer oil inlet valve, and enabling normal-temperature cold oil with the flow rate Q to flow out along a third layer outlet pipe after entering the third layer fluidized bed from a third layer inlet pipe to complete heat exchange;
s4: to obtain medium temperature heat conduction oil: closing a first layer oil outlet valve, a second layer oil inlet valve and a second check valve, opening the first check valve and the second layer oil outlet valve, enabling cold heat conduction oil with the flow rate Q to enter a heat exchange system from a first layer inlet pipe, and continuously heating the first layer inlet pipe, the first coil pipe, the first layer outlet pipe, the second layer inlet pipe, the second coil pipe and the second layer outlet pipe in the first layer fluidized bed reactor and the second layer fluidized bed reactor for two times along a pipeline route to obtain medium-temperature gear heat conduction oil which flows out from a second layer oil outlet; in order to obtain heat conduction oil with the same temperature range, a third layer oil inlet valve is opened, so that cold heat conduction oil with the flow of 0.5Q enters a third layer fluidized bed from a third layer inlet pipe to exchange heat, flows out along a third layer outlet pipe (6), and the same medium temperature range heat conduction oil is obtained;
S5: to obtain high-temperature heat conduction oil: closing a first-layer oil outlet valve, a second-layer oil inlet valve, a second-layer oil outlet valve and a third-layer oil inlet valve, opening a first check valve and a second check valve, enabling cold oil with the flow rate Q to enter a heat exchange system from a first-layer inlet pipe, and performing three-time continuous heating on the first-layer inlet pipe, the first coil pipe, the first-layer outlet pipe, the second-layer inlet pipe, the second coil pipe, the second-layer outlet pipe, the third-layer inlet pipe, the third coil pipe and the third-layer outlet pipe in a first-layer fluidized bed, a second-layer fluidized bed and a third-layer fluidized bed along a pipeline route to obtain high-temperature heat conduction oil;
s6: each layer of Ca (OH) obtained by the reaction in the fluidized bed 2 The solid products are deposited at the baffle plate and then flow to the third hopper, the second hopper and the first hopper along the discharge pipe, the third discharge valve, the second discharge valve and the first discharge valve are opened every 12 hours to collect the solid products in the third storage tank, the second storage tank and the first storage tank, and particles in the storage tank are removed periodically;
s7: during the working process, a nitrogen inlet valve is opened when the scale is required to be removed periodically every 1 hour, high-pressure pulse nitrogen with the pressure of 0-1.0 MPa is introduced from a pipeline at the top of the reactor and is blown to a packing layer through a water vapor outlet pipe, and the generated pulse nitrogen flow is matched with the pulse vibration force generated by a vibrator to remove the scale on the packing layer and the internal parts of the fluidized bed reactor periodically.
The invention has the beneficial effects that:
the rotating speed of the spiral feeder is adjustable; each layer of fluidized bed reactor can independently control the opening of a corresponding feeding valve, the hydration exothermic reaction temperature is reduced, the opening of the feeding valve is also reduced, so that the feeding amount is reduced, and vice versa, thereby ensuring the balance between the heated heat conducting oil temperature and the feeding amount, and realizing the high conversion rate of the hydration exothermic reaction; the check valve is used for controlling the oil outlet valve and the oil inlet valve to control the flow direction of the heat conduction oil, so that the heat conduction oil can be heated once or continuously and repeatedly, and the temperature of the heat conduction oil can be regulated, so that the oil quantity of the heat conduction oil with low, medium and high temperature ranges can be obtained to the maximum extent; the fluidized bed reactor adopts a three-layer fluidized bed structure, so that the space utilization rate is improved, the contact area of fluidized particles is increased, the reaction rate is increased, the reaction is more complete, the heat transfer and mass transfer effects are enhanced, and the hydration exothermic reaction is fully carried out; the device adopts the spiral feeder, the packing layer and the coil pipe to improve the raw material utilization rate and the energy recovery utilization rate; solves the problems that the prior fixed bed technology is difficult to lead the contact area of particles and water vapor to be large, and the hydration reaction rate is slow and the reaction is incomplete.
Drawings
FIG. 1 is a schematic view of the overall structure of the device of the present invention;
FIG. 2 is a schematic diagram of the structure with control points according to the present invention;
fig. 3 is a schematic structural view of a first gas distribution plate according to the present invention.
Wherein, in the figure:
1-a screw feeder; 2-a third feed tube; 3-a water vapor outlet tube; 4-a filler layer; 5-an insulating layer; 6-third layer outlet pipe; 7-a third coil; 8-a third layer oil inlet valve; 9-a third layer inlet pipe; 10-a second feed inlet; 11-a third gas uniform distribution plate; 12-a third baffle; 13-a third funnel; 14-a third discharge valve; 15-a third reservoir; 16-a second check valve; 17-a second layer oil outlet valve; 18-a second coil; 19-a second layer inlet pipe; 20-a first feed tube; 21-a second gas uniform distribution plate; 22-a second baffle; 23-a second funnel; 24-a second reservoir; 25-a first layer outlet pipe; 26-a first check valve; 27-a first layer oil outlet valve; 28-a first coil; 29-a first layer inlet pipe; 30-a first gas uniform distribution plate; 31-a first baffle; 32-a first funnel; 33-a first reservoir; 34-a first purge valve; 35-a water vapor inlet tube; 36-a second purge valve; 37-fluidized bed reactor; 38-a conduction oil heat exchange subsystem; 39-a second layer oil inlet valve; 40-a second discharge valve; 41-a first discharge valve; 42-a first layer oil outlet; 43-second layer oil outlet; 44-a heater; 45-a steam control valve; 46-a second layer outlet pipe; 47-liquid water inlet control valve; 48-a liquid water inlet pipe; 49-a steam outlet valve; a 50-nitrogen inlet valve; 51-a third layer oil outlet valve; 52-a first layer oil inlet valve; 53-vibrator; 54-tube feed subsystem; 55-a discharge subsystem; 56-a water vapour supply subsystem.
Detailed Description
In order to achieve the above objects and effects, the present invention adopts the technical means and structure, and the features and functions of the preferred embodiments of the present invention will be described in detail with reference to the accompanying drawings.
The existing industrial application of the thermochemical energy storage reactor mainly adopts a fixed bed reactor, and the reaction rate is lower due to the small heat and mass transfer rate. The fluidized bed can make solid particles present fluidization, the contact area with the air flow is far higher than that of a fixed bed reactor, and the heat and mass transfer rate is very high. But the single-layer fluidized bed can only obtain heat conduction oil for heat exchange at one temperature grade. Therefore, the invention selects three layers of fluidized beds, the fluidized particles increase the contact area, increase the reaction rate, lead the reaction to be more complete, and can obtain heat conduction oil with low, medium and high 3 temperature grades.
As shown in fig. 1-3, the present invention provides a three-layer fluidized bed calcium-based thermochemical hydration exothermic reaction device, comprising: a feed subsystem 54, a fluidized bed reactor 37, a discharge subsystem 55, a conduction oil heat exchange subsystem 38, and a steam supply subsystem 56; the fluidized bed reactor 37 is arranged in a three-layer structure, and a feeding subsystem is communicated with one side of the fluidized bed reactor 37 of each layer through a pipeline and is used for providing CaO solid particles into the fluidized bed reactor 37; the discharge subsystem is communicated with the other side of the fluidized bed reactor 37 of each layer through a pipeline and is used for collecting Ca (OH) generated by hydration reaction 2 Store a certain amount of Ca (OH) 2 Then timing Ca (OH) 2 Solid particle discharge means; the heat transfer oil heat exchange subsystem is used for conveying heat transfer oil used for heat exchange in the hydration reaction process, the coil pipes of the heat transfer oil heat exchange subsystem are distributed in the middle area of each layer of fluidized bed, and pipelines and valves are arranged outside the fluidized beds to communicate the heat transfer oil heat exchange subsystems of all layers; the water vapor supply subsystem is directly communicated with the bottom of the fluidized bed reactor 37 through a pipeline, and provides water vapor to enable CaO solid in the fluidized bed reactor 37 to be in fluidized distribution and fully contact with the CaO solid, so as to generate hydration exothermic reaction and release chemical energy stored in the CaO; the fluidized bed reactor 37 is used to provide a place for the hydration exothermic reaction of CaO with water vapor.
The feed subsystem 54 includes: the screw feeder 1, the first feeding pipe 20, the second feeding pipe 10 and the third feeding pipe 2 are provided with regulating valves respectively; after the whole fluidized bed reactor 37 is filled with the water vapor, caO solid particles are fed through the screw feeder 1 and then are transferred to the first, second and third fluidized bed reactors 37 along the first, second and third feed pipes 20, 10 and 2, respectively, to carry out hydration exothermic reactions. The first feeding pipe 20, the second feeding pipe 10 and the third feeding pipe 2 are inclined pipelines arranged at the upper part of each layer of fluidized bed, so that CaO can conveniently enter the fluidized bed by means of gravity and can be in a fluidized state favorable for CaO, and the reaction is more sufficient. The feed amount of each layer can be controlled by the opening degree of each regulating valve. The spiral feeder 1 adopts spiral plate type material conveying, and can vertically convey CaO particles to the first layer, the second layer and the third layer of fluidized bed reactors, so that CaO solid particles can be uniformly distributed on the cross section of the whole fluidized bed, and the conveying is uniform and stable. The amount of CaO transported can be adjusted by changing the precession angular velocity of the screw feeder. After the entire fluidized bed reactor is filled with water vapor, caO solid particles are fed by a screw feeder, and the feeding flow rate is adjusted by the precession angular velocity of the screw feeder 1. And the precession angular velocity can be adjusted according to the hydration reaction temperature and the heat conduction oil inlet amount so as to match the temperature of the heat conduction oil to be obtained. CaO particles entering from the screw feeder can be uniformly and stably conveyed into the first, second and third fluidized beds along the first, second and third feeding pipes 20, 10 and 2 respectively, and can be uniformly distributed in a liquid state in the whole cross section under the action of steam airflow and react with steam in a hydration exothermic reaction. The first feeding pipe 20, the second feeding pipe 10 and the third feeding pipe 2 are inclined pipelines arranged at the upper part of each layer of fluidized bed, so that CaO particles can conveniently enter the fluidized bed by gravity and can be in a fluidized state under the action of steam flow, and the reaction is more sufficient. In the embodiment, the valves controlled by the temperature indication controllers are arranged on the feeding pipes of all layers, the feeding amount of CaO particles can be controlled by adjusting the opening of the valves, and the opening of the valves is matched with the required low, medium and high temperatures, so that the feeding requirements of heat conduction oil can be flexibly met.
The fluidized bed reactor 37 includes: reactor body, heat preservation layer 5, first gas equipartition board 30, second gas equipartition board 21, third gas equipartition board 11, packing layer 4, steam outlet pipe 3, first Ca (OH) 2 Purge gate valve 34 and second Ca (OH) 2 A purge port valve 36; the heat preservation layer 5 is coated on the outer wall of the reactor body, and the first gas uniform distribution plate 30, the second gas uniform distribution plate 21 and the third gas uniform distribution plate 11 are plates with the aperture smaller than the diameter of CaO solid particles and are fixed on the inner wall of the inner cavity of the reactor body so as to divide the reactor body into three layers; the top end of the reactor body is connected with a water vapor outlet pipe 3, and a filler layer 4 is arranged at the inlet of the water vapor outlet pipe 3; the two sides of the bottom end of the reactor body are provided with first Ca (OH) 2 Purge gate valve 34 and a second Ca (OH) 2 A purge port valve 36. The fluidized bed reactor 37 further includes: the first baffle 31, the second baffle 22 and the third baffle 12 are respectively arranged at the positions communicated with the discharging subsystem 55 in the three-layer reactor body, and the first baffle 31, the second baffle 22 and the third baffle 12 are respectively arranged at the positions communicated with the discharging subsystem 55. The pressurized water vapor is distributed more uniformly after passing through the first gas uniform distribution plate 30, the second gas uniform distribution plate 21 and the third gas uniform distribution plate 11, which is favorable for fluidization formation, so that the water vapor can be uniformly distributed after passing through and the hydration reaction is more sufficient; the pore diameter is smaller than the average particle diameter of CaO particles, so that a certain amount of CaO can be kept in each laminar flow bed, and the reaction is more uniformly balanced. After the whole reactor cavity is finished, the water vapor is separated out of solid particles through the packing layer 4 and flows out of the reactor. CaO is fluidized after entering the inner cavity of the reactor body and reacts with water vapor to generate Ca (OH) 2 And release a large amount of heat. After passing through the first baffle 31, the second baffle 22 and the third baffle 12, the gas-solid mixture in the reactor body flows into the discharge subsystem after the solid particles therein are free to settle. Small amount of solid Ca (OH) during the reaction 2 Falls to the bottom of the reactor through the first gas distribution plate 30, and opens the first Ca (OH) at intervals 2 Purge gate valve 34 and a second Ca (OH) 2 A purge outlet valve 36 for discharging solid Ca (OH) accumulated at the bottom 2 And (5) discharging. The inner cavity of the reactor is provided with 3 first gas uniform distribution plates 30, second gas uniform distribution plates 21 and third gas uniform distribution plates 11 with the same specification, and the first gas uniform distribution plates, the second gas uniform distribution plates and the third gas uniform distribution plates are used for dividing the reactor into three layers of fluidized beds. The first gas uniform distribution plate 30, the second gas uniform distribution plate 21 and the third gas uniform distribution plate 11 are provided with a plurality of through holes with the aperture smaller than about 1mm, and the pressurized water vapor is distributed more uniformly after passing through the plates, which is beneficial to CaO and Ca (OH) 2 The formation of fluidization of the particles, and the hydration reaction is more sufficient. CaO particles enter the corresponding layer of the inner cavity of the reactor and are fluidized and distributed under the action of steam airflow, and react with the steam to generate Ca (OH) 2 And release a large amount of heat. Small amounts of solid Ca (OH) occur during the reaction 2 The first Ca (OH) was opened every 8 hours by dropping the first gas distribution plate 30 to the bottom of the reactor 2 Purge gate valve 34 and a second Ca (OH) 2 A purge outlet valve 36 for discharging solid Ca (OH) accumulated at the bottom 2 And (5) discharging. In this embodiment, the fluidized bed reactor 37 is provided with a temperature display instrument, and a temperature probe is arranged in the inner cavity space of the reactor to detect the temperature during hydration reaction and transmit the temperature value to other temperature controllers.
The outfeed subsystem 55 comprises: first hopper 32, first discharge valve 41, first reservoir 33, second hopper 23, second discharge valve 40, second reservoir 24, third hopper 13, third discharge valve 14, and third reservoir 15; the first funnel 32 is communicated with the reactor body of the first layer, and a first discharge valve 41 is arranged on a pipeline of the first funnel 32 communicated with the first storage tank 33; the second funnel 23 is communicated with the reactor body of the second layer, and a second discharge valve 40 is arranged on a pipeline of the second funnel 23 communicated with the second storage tank 24; the third hopper 13 is communicated with the reactor body of the first layer, and a third discharge valve 14 is arranged on a pipeline of the third hopper 13 communicated with the third storage tank 15. Each layer of fluidized bed is provided with a first baffle 31, a second baffle 22 and a third baffle 12 below the discharge hole, and the gas-solid mixture floats above the baffles after contacting for a period of time, so that solid particles Ca (OH) are formed 2 The drag force caused by the water vapor from the lower part is lost, so that Ca (OH) 2 Is deposited on the baffle plate under the action of gravity and flows along the discharging pipe toThe third hopper 13, the second hopper 23 and the first hopper 32 can be opened at intervals to collect the materials in the third storage tank 15, the second storage tank 24 and the first storage tank 33, then periodically discharged, and processed for recycling. The discharging pipe is an inclined pipeline arranged at the lower part of each layer of fluidized bed, which is convenient for Ca (OH) 2 Flows out of the reactor cavity into the funnel under the action of gravity. And the discharge hole is arranged at the diagonal position of the feeding position, so that CaO particles flow along with gas in the reactor, the residence time is longer, and the hydration reaction is more thoroughly carried out. Collected Ca (OH) 2 The particles can be used for other occasions such as calcium-based energy storage decomposition reaction and the like so as to realize cyclic utilization.
The conduction oil heat exchange subsystem 38 includes: a first layer inlet pipe 29, a second layer inlet pipe 19, a third layer inlet pipe 9, a first coil 28, a second coil 18, a third coil 7, a first layer outlet pipe 25, a second layer outlet pipe 46, a third layer outlet pipe 6, a first layer oil inlet valve 52, a second layer oil inlet valve 39, a third layer oil inlet valve 8, a first layer oil outlet valve 27, a second layer oil outlet valve 17, a third layer oil outlet valve 51, a first check valve 26, and a second check valve 16; the first coil 28, the second coil 18 and the third coil 7 are respectively arranged in the middle area of the reactor body of each layer; the first layer outlet pipe 25 is connected with the second layer inlet pipe 19 through a pipeline and is communicated with the second layer inlet pipe 19 through a first check valve 26 in a control manner, the second layer outlet pipe 46 is connected with the third layer inlet pipe 9 through a pipeline and is communicated with the third layer inlet pipe 9 through a second check valve 16 in a control manner, and the first layer inlet pipe 29, the second layer inlet pipe 19 and the third layer inlet pipe 9 are respectively provided with a first layer oil inlet valve 52, a second layer oil inlet valve 39 and a third layer oil inlet valve 8; the first layer outlet pipe 25, the second layer outlet pipe 46, and the third layer outlet pipe 6 are provided with a first layer outlet valve 27, a second layer outlet valve 17, and a third layer outlet valve 51, respectively. The flow direction of the heat exchange oil can be determined by controlling the opening and closing of different valves. The pipeline is provided with a temperature indication control instrument for controlling the opening, closing and opening of the valve on the pipeline so as to control the flow direction of the heat conduction oil, realize one-time heating or continuous heating of the heat conduction oil and further regulate the temperature of the heat conduction oil. Each pipeline is wrapped by a heat preservation layer.
The water vapor supply subsystem 56 includes: a water vapor inlet pipe 35, a heater 44, a liquid water inlet pipe 48, a liquid water inlet control valve 47, and a water vapor control valve 45; one end of the heater 44 is communicated with the bottom of the fluidized bed reactor 37 through a water vapor inlet pipe 35, a water vapor control valve 45 is arranged on the water vapor inlet pipe 35, the other end of the heater 44 is connected with a liquid water inlet pipe 48, and a liquid water inlet control valve 47 is arranged on the liquid water inlet pipe 48. The liquid water is heated into water vapor with the pressure of 0.25-1.75 MPa in the heater, the water vapor enters the fluidized bed reactor 37 through the water vapor inlet pipe 35 after the flow rate is regulated by the water vapor control valve 45, the whole reactor is filled with the water vapor, and the water vapor flowing at high speed enables CaO particles to be fluidized, and the CaO particles undergo full hydration exothermic reaction. The water vapor supply subsystem heats liquid water into water vapor, and then the water vapor is introduced into the inner cavity of the fluidized bed reactor through the water vapor inlet pipe 35, so that light CaO particles are driven to be uniformly dispersed in the fluidized bed reactor in a fluidization manner, the contact area between CaO and water vapor is increased, and the reaction is enabled to be full. And the reaction process is environment-friendly, and the main component of the tail gas is water vapor which can be recycled after condensation treatment. A temperature indicating control instrument is arranged on a pipeline of the water vapor supply subsystem and controls the opening degree of a valve on the pipeline so as to regulate the flow of water vapor. The heater 44 is provided with a pressure indication control instrument to regulate the temperature of the water vapor. Each pipeline and heater are wrapped by an insulating layer.
In this embodiment, the side wall of the steam outlet pipe 3 is provided with a vibrator 53, and the vibrator 53 can generate pulse vibration force to clean the scale on the inner parts of the fluidized bed reactor periodically.
In this embodiment, the steam outlet pipe 3 is communicated with the nitrogen inlet pipeline through a tee joint and a nitrogen inlet valve 50, high-pressure pulse nitrogen with the pressure of 0-1.0 MPa is introduced into the pipeline every 3 hours for 5 minutes, and is blown to the filler layer 4 through the steam outlet pipe 3, and the generated pulse nitrogen flow periodically cleans particles in the filler layer 4.
The invention also provides a working method of the three-layer fluidized bed calcium-based thermochemical hydration exothermic reaction device, which comprises the following steps:
s1: the liquid water inlet control valve 47 is opened, the liquid water enters the heater 44 from the inlet pipe 48 for heating, water vapor with a certain pressure is obtained, and the heating medium can be 180-300 ℃ heat exchange oil obtained by solar heating. When the set pressure is reached, the steam inlet control valve 45 is opened, steam enters the fluidized bed reactor cavity from the bottom through the steam inlet pipe 35, and the steam flow entering the reactor can be regulated by adjusting the opening of the control valve 45.
S2: starting a screw feeder and adjusting the precession angular velocity, and uniformly conveying CaO particles into the first layer, the second layer and the third layer of fluidized bed reactors along the first feeding pipe, the second feeding pipe and the third feeding pipe to carry out hydration exothermic reaction; the feeding amount of CaO particles into the fluidized bed is controlled by valves on the corresponding feeding pipes.
S3: to obtain the low-temperature 150-250 ℃ grade heat conduction oil: the normal-temperature cold oil with the flow rate Q enters the first-layer fluidized bed reactor from the first-layer inlet pipe 29 to complete heat exchange, the first-layer oil outlet valve 27 is opened, the first check valve 26 is closed, and the low-temperature heat conduction oil flows out along the first-layer outlet pipe 25 to obtain low-temperature heat conduction oil which is heated once; the second-layer oil inlet valve 39 and the second-layer oil outlet valve 17 are opened, the second check valve 16 is closed, and the normal-temperature cold oil with the flow rate Q flows out along the second-layer outlet pipe 46 after entering the second-layer fluidized bed from the second-layer inlet pipe 19 to complete heat exchange; opening a third-layer oil inlet valve 8, and enabling normal-temperature cold oil with the flow rate Q to flow out along a third-layer outlet pipe 6 after entering the third-layer fluidized bed from a third-layer inlet pipe 9 to complete heat exchange;
s4: to obtain medium-temperature 250-350 ℃ grade heat conduction oil: closing the first-layer oil outlet valve 27, the second-layer oil inlet valve 39 and the second check valve 16, opening the first check valve 26 and the second-layer oil outlet valve 17, enabling cold heat conduction oil with the flow rate Q to enter the heat exchange system from the first-layer inlet pipe 29, and performing two continuous heating on the first-layer inlet pipe 29, the first coil pipe 28, the first-layer outlet pipe 25, the second-layer inlet pipe 19, the second coil pipe 18 and the second-layer outlet pipe 46 in the first-layer fluidized bed reactor and the second-layer fluidized bed reactor along a pipeline route to obtain medium-temperature-grade heat conduction oil, and enabling the medium-temperature-grade heat conduction oil to flow out from the second-layer oil outlet 43; in order to obtain heat conduction oil with the same temperature range, a third layer oil inlet valve 8 is opened, so that cold heat conduction oil with the flow rate of 0.5Q enters a third layer fluidized bed from a third layer inlet pipe 9 to exchange heat, and flows out along a third layer outlet pipe 6 to obtain the same heat conduction oil with the medium temperature range;
S5: to obtain the heat conduction oil with the high temperature of 350-450 ℃: closing the first-layer oil outlet valve 27, the second-layer oil inlet valve 39, the second-layer oil outlet valve 17 and the third-layer oil inlet valve 8, opening the first check valve 26 and the second check valve 16, enabling cold oil with the flow rate Q to enter the heat exchange system from the first-layer inlet pipe 29, and performing three times of continuous heating in the first-layer, second-layer and third-layer fluidized beds along the pipeline route by the first-layer inlet pipe 29, the first coil pipe 28, the first-layer outlet pipe 25, the second-layer inlet pipe 19, the second coil pipe 18, the second-layer outlet pipe 46, the third-layer inlet pipe 9, the third coil pipe 7 and the third-layer outlet pipe 6 to obtain high-temperature-grade heat conduction oil;
s6: each layer of Ca (OH) obtained by the reaction in the fluidized bed 2 The solid products deposited at the baffle plate flow to the third hopper 13, the second hopper 23 and the first hopper 32 along the discharge pipe, the third discharge valve 14, the second discharge valve 40 and the first discharge valve 41 are opened every 12 hours to collect the solid products in the third storage tank 15, the second storage tank 24 and the first storage tank 33, and particles in the storage tanks are removed periodically;
s7: during the operation, the nitrogen inlet valve 50 is opened during the period of periodically cleaning the scale every 1 hour, high-pressure pulse nitrogen with the pressure of 0-1.0 MPa is introduced from the pipeline at the top of the reactor and is blown to the packing layer 4 through the water vapor outlet pipe 3, and the generated pulse nitrogen flow is matched with the pulse vibration force generated by the vibrator 53 to periodically clean the scale on the packing layer and the internal parts of the fluidized bed reactor.
After the scheme is implemented, the chemical energy of the calcium oxide can be fully utilized, the reasonable development and utilization of the chemical energy are realized, the environmental protection and the sustainable development of the human society are also realized, and the energy conservation, the consumption reduction, the environmental protection and the emission reduction are realized. If the device is used, the heat generated by the fluidized bed energy release reactor heats the heat conduction oil in the coil heat exchanger. For a specific gravity of 820kg/m 3 Certain heat conduction oil with specific heat capacity of 2.0KJ/kg DEG C can be increased to about 150 ℃ to 450 ℃ from normal temperature.
Application example
The invention adopts heat exchange oil with the temperature of 250 ℃ obtained by solar heating as a high-temperature medium of a heater in a water vapor supply subsystem to heat liquid water to water vapor with the temperature of 200 ℃. The inner diameter of the fluidized bed reactor is 3m and the height is 6m, the fluidized bed reactor is made of stainless steel, 3 layers of gas uniformly-distributed plates are all made of stainless steel, a plurality of through holes are formed in the plates, the aperture is 1mm,3 coils are all made of stainless steel with the diameter phi of 50mm, the diameter of a screw shaft of a screw feeder is phi 200mm, the thickness of a screw blade is 4mm, the fluidized bed reactor is made of stainless steel, 2 check valves, 3 phi 100mm tee joints and 3 phi 200mm funnels are arranged in the fluidized bed reactor, and the fluidized bed reactor is made of stainless steel.
The invention aims to obtain medium-temperature 250-350 ℃ heat conduction oil, which is operated according to the following steps:
The first step is as follows: the distributed control system was activated and the liquid water inlet control valve 47 was opened to let liquid water with a molar flow of 150mol/s from the inlet pipe 48 into the heater 44 for heating. The 250 c heat exchange oil is passed to heater 44 and the liquid water is heated to a vapor pressure of 1554kPa at 200 c. The opening of the steam inlet control valve 45 was opened and adjusted to allow steam having a molar flow rate of 150mol/s to enter the fluidized bed reactor cavity from the bottom through the gas inlet.
The second step is as follows: the screw feeder was turned on and the precession angular velocity was adjusted to 3rpm. And adjusting the opening of a valve on the feeding pipe to ensure that CaO particles with the molar flow of 60mol/s are respectively conveyed into the first, second and third fluidized beds along the first feeding pipe, the second feeding pipe and the third feeding pipe at uniform speed to carry out hydration exothermic reaction.
And a third step of: the first-layer oil outlet valve 27, the second-layer oil inlet valve 39 and the second check valve 16 are closed, the first check valve 26 and the second-layer oil outlet valve 17 are opened, heat conduction oil with the flow rate of 50L/min and the temperature of 20 ℃ enters a coil pipe heat exchange system of the first-layer fluidized bed and the second-layer fluidized bed from the first-layer inlet pipe 29, the first coil pipe 28, the first-layer outlet pipe 25, the second-layer inlet pipe 19, the second coil pipe 18 and the second-layer outlet pipe 46, and the heat conduction oil with the temperature of 300 ℃ is obtained by two continuous heating through heat exchange with hydration exothermic reaction in the first-layer fluidized bed and the second-layer fluidized bed along a pipeline route, and flows out from the second-layer oil outlet 43. And opening the third layer oil inlet valve 8 to enable the heat conduction oil with the flow rate of 25L/min and the temperature of 20 ℃ to enter the third layer fluidized bed from the third layer inlet pipe 9 for heat exchange, and flow out along the third layer outlet pipe 6 to obtain the heat conduction oil with the temperature of 300 ℃. Through the step, the 300 ℃ medium temperature heat conduction oil with the flow of 75L/min can be obtained.
The fourth step is: in the working process, the third discharge valve 14, the second discharge valve 40 and the first discharge valve 41 are opened every 12 hours to discharge Ca (OH) 2 The solid product is collected in third reservoir 15, second reservoir 24, first reservoir 33, and particles in the reservoirs are periodically removed.
The fifth step is: during the working process, the scale is removed periodically every 1 hour. At this time, the nitrogen inlet valve 50 was opened, and pulse nitrogen gas having a pressure of 0.8MPa was introduced from the top line of the reactor and blown toward the filler layer 4 through the steam outlet pipe 3 at a pulse frequency of 20 times/minute for 3 minutes. At this time, the rapper 53 is turned on again, and the rapping frequency of the rapper is 20 times/minute for 3 minutes.
The foregoing description is only of the preferred embodiments of the present invention and is not intended to limit the technical scope of the present invention, so that any minor modifications, equivalent changes and modifications made to the above embodiments according to the technical principles of the present invention still fall within the scope of the technical solutions of the present invention.
Claims (10)
1. A three-layer fluidized bed calcium-based thermochemical hydration exothermic reaction device, comprising: a feed subsystem (54), a fluidized bed reactor (37), a discharge subsystem (55), a conduction oil heat exchange subsystem (38) and a steam supply subsystem (56); the fluidized bed reactors (37) are arranged in a three-layer structure, and the feeding subsystem is communicated with one side of each layer of fluidized bed reactor (37) through a pipeline and is used for providing CaO solid particles into the fluidized bed reactors (37); the discharge subsystem is communicated with the other side of the fluidized bed reactor (37) of each layer through a pipeline and is used for collecting Ca (OH) generated by hydration reaction 2 Store a certain amount of Ca (OH) 2 Then timing Ca (OH) 2 Solid particle discharge means; thermal conductionThe oil heat exchange subsystem is used for conveying heat conduction oil for heat exchange in the hydration reaction process, and coils of the heat conduction oil heat exchange subsystem are distributed in the middle area of each layer of fluidized bed; the water vapor supply subsystem is directly communicated with the bottom of the fluidized bed reactor (37) through a pipeline, and provides water vapor to enable CaO solid in the fluidized bed reactor (37) to be in fluidized distribution and fully contact with the CaO solid, so as to generate hydration exothermic reaction and release chemical energy stored in the CaO; the fluidized bed reactor (37) is used for providing a place for the hydration exothermic reaction of CaO and water vapor.
2. A three-layer fluidized bed calcium-based thermochemical hydration exothermic reaction device according to claim 1, wherein the feed subsystem (54) comprises: the screw feeder (1), the first feeding pipe (20), the second feeding pipe (10) and the third feeding pipe (2), wherein regulating valves are arranged on the first feeding pipe (20), the second feeding pipe (10) and the third feeding pipe (2); after the whole fluidized bed reactor (37) is filled with water vapor, caO solid particles are fed by the screw feeder (1) and then are respectively conveyed to the first layer, the second layer and the third layer of fluidized bed reactors (37) along the first feeding pipe (20), the second feeding pipe (10) and the third feeding pipe (2) to carry out hydration exothermic reaction.
3. A three-layer fluidized bed calcium-based thermochemical hydration exothermic reaction device according to claim 1, wherein the fluidized bed reactor (37) comprises: reactor body, heat preservation (5), first gas equipartition board (30), second gas equipartition board (21), third gas equipartition board (11), packing layer (4), steam outlet pipe (3), first Ca (OH) 2 Purge port valve (34) and second Ca (OH) 2 A purge port valve (36); the heat preservation layer (5) is coated on the outer wall of the reactor body, and the first gas uniform distribution plate (30), the second gas uniform distribution plate (21) and the third gas uniform distribution plate (11) are plates with the aperture smaller than the diameter of CaO solid particles and are fixed on the inner wall of the inner cavity of the reactor body so as to divide the reactor body into three layers; the top end of the reactor body is connected with a water vapor outlet pipe (3), and a filler layer (4) is arranged at the inlet of the water vapor outlet pipe (3); by a means ofThe two sides of the bottom end of the reactor body are provided with first Ca (OH) 2 A purge outlet valve (34) and a second Ca (OH) 2 A purge port valve (36).
4. A three-layer fluidized bed calcium-based thermochemical hydration exothermic reaction device according to claim 3, wherein the outfeed subsystem (55) comprises: a first funnel (32), a first discharge valve (41), a first storage tank (33), a second funnel (23), a second discharge valve (40), a second storage tank (24), a third funnel (13), a third discharge valve (14) and a third storage tank (15); the first funnel (32) is communicated with the reactor body of the first layer, and a first discharge valve (41) is arranged on a pipeline for communicating the first funnel (32) with the first storage tank (33); the second funnel (23) is communicated with the reactor body of the second layer, and a second discharge valve (40) is arranged on a pipeline for communicating the second funnel (23) with the second storage tank (24); the third funnel (13) is communicated with the reactor body of the first layer, and a third discharge valve (14) is arranged on a pipeline for communicating the third funnel (13) with the third storage tank (15).
5. A three-layer fluidized bed calcium-based thermochemical hydration exothermic reaction device according to claim 3, wherein the heat transfer oil heat exchange subsystem (38) comprises: a first layer inlet pipe (29), a second layer inlet pipe (19), a third layer inlet pipe (9), a first coil pipe (28), a second coil pipe (18), a third coil pipe (7), a first layer outlet pipe (25), a second layer outlet pipe (46), a third layer outlet pipe (6), a first layer oil inlet valve (52), a second layer oil inlet valve (39), a third layer oil inlet valve (8), a first layer oil outlet valve (27), a second layer oil outlet valve (17), a third layer oil outlet valve (51), a first check valve (26) and a second check valve (16); the first coil pipe (28), the second coil pipe (18) and the third coil pipe (7) are respectively arranged in the middle area of the reactor body of each layer; the first layer outlet pipe (25) is connected with the second layer inlet pipe (19) through a pipeline and is communicated with the second layer inlet pipe (19) through a first check valve (26), the second layer outlet pipe (46) is connected with the third layer inlet pipe (9) through a pipeline and is communicated with the third layer inlet pipe through a second check valve (16), and the first layer inlet pipe (29), the second layer inlet pipe (19) and the third layer inlet pipe (9) are respectively provided with a first layer oil inlet valve (52), a second layer oil inlet valve (39) and a third layer oil inlet valve (8); the first layer outlet pipe (25), the second layer outlet pipe (46) and the third layer outlet pipe (6) are respectively provided with a first layer oil outlet valve (27), a second layer oil outlet valve (17) and a third layer oil outlet valve (51).
6. A three-layer fluidized bed calcium-based thermochemical hydration exothermic reaction device according to claim 1, wherein the water vapor supply subsystem (56) comprises: a water vapor inlet pipe (35), a heater (44), a liquid water inlet pipe (48), a liquid water inlet control valve (47) and a water vapor control valve (45); one end of the heater (44) is communicated with the bottom of the fluidized bed reactor (37) through a water vapor inlet pipe (35), a water vapor control valve (45) is arranged on the water vapor inlet pipe (35), the other end of the heater (44) is connected with a liquid water inlet pipe (48), and a liquid water inlet control valve (47) is arranged on the liquid water inlet pipe (48).
7. A three-layer fluidized bed calcium-based thermochemical hydration exothermic reaction device according to claim 3, wherein the side wall of the steam outlet pipe (3) is provided with a vibrator (53), wherein the vibrator (53) is capable of generating a pulsed vibrating force to periodically remove scale from the internal parts of the fluidized bed reactor.
8. The three-layer fluidized bed calcium-based thermochemical hydration exothermic reaction device according to claim 7, wherein the water vapor outlet pipe (3) is communicated with a nitrogen inlet pipeline through a tee joint and a nitrogen inlet valve (50), high-pressure pulse nitrogen with the pressure of 0-1.0 MPa is periodically introduced into the pipeline, the high-pressure pulse nitrogen is blown to the packing layer (4) through the water vapor outlet pipe (3), and the generated pulse nitrogen flow periodically removes particles in the packing layer (4).
9. A three-layer fluidized bed calcium-based thermochemical hydration exothermic reaction device according to claim 3, wherein the fluidized bed reactor (37) further comprises: the three-layer reactor comprises a first baffle (31), a second baffle (22) and a third baffle (12), wherein the first baffle (31), the second baffle (22) and the third baffle (12) are respectively arranged at the positions communicated with a discharging subsystem (55) in the three-layer reactor body.
10. A method of operating a three-layer fluidized bed calcium-based thermochemical hydration exothermic reaction device as recited in claim 1, comprising the steps of:
s1: opening a liquid water inlet control valve (47), heating liquid water in an inlet pipe (48) in a heater (44) to obtain water vapor with a certain pressure, opening the water vapor inlet control valve (45) when the set pressure is reached, and allowing the water vapor to enter the inner cavity of the fluidized bed reactor from the bottom through a water vapor inlet pipe (35);
s2: starting a screw feeder, and uniformly conveying CaO particles into the first layer, the second layer and the third layer of fluidized bed reactors along the first feeding pipe, the second feeding pipe and the third feeding pipe to carry out hydration exothermic reaction;
s3: to obtain low-temperature heat conduction oil: the normal-temperature cold oil with the flow rate Q enters the first-layer fluidized bed reactor from the first-layer inlet pipe (29) to complete heat exchange, the first-layer oil outlet valve (27) is opened, the first check valve (26) is closed, and the low-temperature heat conduction oil flows out along the first-layer outlet pipe (25) to obtain low-temperature heat conduction oil which is heated once; opening a second-layer oil inlet valve (39) and a second-layer oil outlet valve (17), closing a second check valve (16), and enabling normal-temperature cold oil with the flow rate Q to flow out along a second-layer outlet pipe (46) after entering the second-layer fluidized bed from a second-layer inlet pipe (19) to complete heat exchange; opening a third-layer oil inlet valve (8), and enabling normal-temperature cold oil with the flow rate Q to flow out along a third-layer outlet pipe (6) after entering the third-layer fluidized bed from a third-layer inlet pipe (9) to complete heat exchange;
S4: to obtain medium temperature heat conduction oil: closing a first-layer oil outlet valve (27), a second-layer oil inlet valve (39) and a second-layer oil outlet valve (16), opening the first-layer check valve (26) and the second-layer oil outlet valve (17), enabling cold heat conduction oil with flow rate Q to enter a heat exchange system from a first-layer inlet pipe (29), a first coil pipe (28), a first-layer outlet pipe (25), a second-layer inlet pipe (19), a second coil pipe (18) and a second-layer outlet pipe (46), and continuously heating in the first-layer fluidized bed reactor and the second-layer fluidized bed reactor for two times along a pipeline route to obtain medium-temperature-grade heat conduction oil, and enabling the medium-temperature-grade heat conduction oil to flow out from a second-layer oil outlet (43); in order to obtain heat conduction oil with the same temperature range, a third layer oil inlet valve (8) is opened, so that cold heat conduction oil with the flow rate of 0.5Q enters a third layer fluidized bed from a third layer inlet pipe (9) to exchange heat, flows out along a third layer outlet pipe (6), and the same medium temperature range heat conduction oil is obtained;
s5: to obtain high-temperature heat conduction oil: closing a first-layer oil outlet valve (27), a second-layer oil inlet valve (39), a second-layer oil outlet valve (17) and a third-layer oil inlet valve (8), opening a first check valve (26) and a second check valve (16), enabling cold oil with the flow rate Q to enter a heat exchange system from a first-layer inlet pipe (29), a first coil pipe (28), a first-layer outlet pipe (25), a second-layer inlet pipe (19), a second coil pipe (18), a second-layer outlet pipe (46), a third-layer inlet pipe (9), a third coil pipe (7) and a third-layer outlet pipe (6), and continuously heating for three times in the first-layer, second-layer and third-layer fluidized beds along a pipeline route to obtain high-temperature-grade heat conduction oil;
S6: each layer of Ca (OH) obtained by the reaction in the fluidized bed 2 The solid products are deposited at the baffle plate and then flow to a third funnel (13), a second funnel (23) and a first funnel (32) along a discharge pipe, a third discharge valve (14), a second discharge valve (40) and a first discharge valve (41) are opened every 12 hours to be collected in a third storage tank (15), a second storage tank (24) and a first storage tank (33), and particles in the storage tanks are removed periodically;
s7: during the working process, during the period of periodically cleaning the scale, a nitrogen inlet valve (50) is opened, high-pressure pulse nitrogen with the pressure of 0-1.0 MPa is introduced from a pipeline at the top of the reactor and is blown to a packing layer (4) through a water vapor outlet pipe (3), and the generated pulse nitrogen flow is matched with the pulse vibration force generated by a vibrator (53) to periodically clean the scale on the packing layer and the internal parts of the fluidized bed reactor.
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| CN117074602B (en) * | 2023-08-29 | 2024-05-24 | 湛江电力有限公司 | Sample preparation system and method for calcium-based thermochemical energy storage material under multiple factors |
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