CN117989627A - Clean air conditioner utilizing normal temperature air cold energy in fluidization mode and exhaust steam condensation method - Google Patents
Clean air conditioner utilizing normal temperature air cold energy in fluidization mode and exhaust steam condensation method Download PDFInfo
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- 238000000034 method Methods 0.000 title claims abstract description 54
- 238000005243 fluidization Methods 0.000 title claims abstract description 50
- 238000009833 condensation Methods 0.000 title claims description 40
- 230000005494 condensation Effects 0.000 title claims description 40
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 147
- 239000002245 particle Substances 0.000 claims abstract description 68
- 238000001816 cooling Methods 0.000 claims abstract description 46
- 238000001704 evaporation Methods 0.000 claims abstract description 26
- 230000008020 evaporation Effects 0.000 claims abstract description 26
- 238000005057 refrigeration Methods 0.000 claims abstract description 21
- 239000002351 wastewater Substances 0.000 claims abstract description 20
- 230000008016 vaporization Effects 0.000 claims abstract description 19
- 239000007787 solid Substances 0.000 claims abstract description 18
- 238000012546 transfer Methods 0.000 claims abstract description 15
- 238000009834 vaporization Methods 0.000 claims abstract description 13
- 230000000694 effects Effects 0.000 claims abstract description 11
- 239000003595 mist Substances 0.000 claims abstract description 11
- 230000008929 regeneration Effects 0.000 claims abstract description 11
- 238000011069 regeneration method Methods 0.000 claims abstract description 11
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- 230000007613 environmental effect Effects 0.000 claims abstract description 6
- 239000003570 air Substances 0.000 claims description 141
- 239000007789 gas Substances 0.000 claims description 48
- 239000011552 falling film Substances 0.000 claims description 25
- 238000009826 distribution Methods 0.000 claims description 21
- 238000004378 air conditioning Methods 0.000 claims description 15
- 239000007788 liquid Substances 0.000 claims description 11
- 239000000645 desinfectant Substances 0.000 claims description 9
- 239000000243 solution Substances 0.000 claims description 9
- 238000005086 pumping Methods 0.000 claims description 7
- 238000004659 sterilization and disinfection Methods 0.000 claims description 7
- 239000012080 ambient air Substances 0.000 claims description 6
- 239000007921 spray Substances 0.000 claims description 5
- 238000005507 spraying Methods 0.000 claims description 5
- 239000002352 surface water Substances 0.000 claims description 5
- 239000007864 aqueous solution Substances 0.000 claims description 4
- 238000004064 recycling Methods 0.000 claims description 4
- 230000005514 two-phase flow Effects 0.000 claims description 4
- 239000002699 waste material Substances 0.000 claims description 4
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- 230000003068 static effect Effects 0.000 claims description 3
- 239000002912 waste gas Substances 0.000 claims description 3
- 238000004140 cleaning Methods 0.000 claims description 2
- 238000007791 dehumidification Methods 0.000 claims 1
- 238000000926 separation method Methods 0.000 claims 1
- 238000010521 absorption reaction Methods 0.000 abstract description 11
- 238000005265 energy consumption Methods 0.000 abstract description 4
- 229910052799 carbon Inorganic materials 0.000 abstract description 3
- 239000000945 filler Substances 0.000 abstract description 3
- 238000004134 energy conservation Methods 0.000 abstract description 2
- 238000005728 strengthening Methods 0.000 abstract description 2
- 239000002925 low-level radioactive waste Substances 0.000 abstract 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 abstract 1
- 238000009423 ventilation Methods 0.000 description 9
- 230000005611 electricity Effects 0.000 description 6
- 238000005516 engineering process Methods 0.000 description 6
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Classifications
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F24—HEATING; RANGES; VENTILATING
- F24F—AIR-CONDITIONING; AIR-HUMIDIFICATION; VENTILATION; USE OF AIR CURRENTS FOR SCREENING
- F24F5/00—Air-conditioning systems or apparatus not covered by F24F1/00 or F24F3/00, e.g. using solar heat or combined with household units such as an oven or water heater
- F24F5/0007—Air-conditioning systems or apparatus not covered by F24F1/00 or F24F3/00, e.g. using solar heat or combined with household units such as an oven or water heater cooling apparatus specially adapted for use in air-conditioning
- F24F5/0035—Air-conditioning systems or apparatus not covered by F24F1/00 or F24F3/00, e.g. using solar heat or combined with household units such as an oven or water heater cooling apparatus specially adapted for use in air-conditioning using evaporation
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F24—HEATING; RANGES; VENTILATING
- F24F—AIR-CONDITIONING; AIR-HUMIDIFICATION; VENTILATION; USE OF AIR CURRENTS FOR SCREENING
- F24F13/00—Details common to, or for air-conditioning, air-humidification, ventilation or use of air currents for screening
- F24F13/30—Arrangement or mounting of heat-exchangers
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F24—HEATING; RANGES; VENTILATING
- F24F—AIR-CONDITIONING; AIR-HUMIDIFICATION; VENTILATION; USE OF AIR CURRENTS FOR SCREENING
- F24F8/00—Treatment, e.g. purification, of air supplied to human living or working spaces otherwise than by heating, cooling, humidifying or drying
- F24F8/20—Treatment, e.g. purification, of air supplied to human living or working spaces otherwise than by heating, cooling, humidifying or drying by sterilisation
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28B—STEAM OR VAPOUR CONDENSERS
- F28B1/00—Condensers in which the steam or vapour is separate from the cooling medium by walls, e.g. surface condenser
- F28B1/02—Condensers in which the steam or vapour is separate from the cooling medium by walls, e.g. surface condenser using water or other liquid as the cooling medium
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28B—STEAM OR VAPOUR CONDENSERS
- F28B7/00—Combinations of two or more condensers, e.g. provision of reserve condenser
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- Engineering & Computer Science (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Combustion & Propulsion (AREA)
- Life Sciences & Earth Sciences (AREA)
- Sustainable Development (AREA)
- Heat-Exchange Devices With Radiators And Conduit Assemblies (AREA)
Abstract
A clean air conditioner utilizing cold energy of normal temperature air and a dead steam condensing method are provided, which lead the mixed evaporation cooling mass transfer process of air and water mist to be carried out on the surface of fluidized air-solid particles, the specific surface area and mass transfer coefficient of the air-solid particles are higher than those of common fillers by a plurality of orders of magnitude without dirt influence, and the low-level waste heat is utilized to heat the fluidized system to improve saturated vapor pressure, thereby further strengthening the application effect of cold energy of normal temperature air, and greatly improving the refrigeration intensity and operation reliability of equipment. The method is applied to an all fresh air conditioner with public space exhaust fluidization heat absorption auxiliary solar refrigeration, the comprehensive energy efficiency coefficient COP is more than 3.1, and the hygienic risk of air supply and exhaust is completely avoided; the method is applied to auxiliary utilization of low-level waste heat for process waste water vaporization regeneration, more than half of the waste water can be recycled as regenerated condensed water, and the comprehensive energy consumption of a workshop is not increased in the regeneration process. The method has the outstanding characteristics of low carbon, energy conservation and environmental protection.
Description
Technical Field
The invention relates to low-level energy extraction and application and near-room temperature refrigeration and clean air conditioning technology, in particular to the technical field of multiphase flow heat and mass transfer, which is coupled with waste gas and wastewater treatment and efficiently utilizes normal-temperature air cooling energy.
Background
The near-room temperature refrigeration technology is mainly applied to the field of air conditioning refrigeration in summer at present, and has a very wide application range. The vapor compression heat removal method is generally high in energy consumption, and remarkably aggravates urban heat island effect, and needs to be improved in two aspects of low-carbon energy conservation and human-occupied environment protection. The evaporative air conditioner with obvious energy-saving characteristic is characterized in that air is directly contacted with a water spraying filler layer through a fan, sensible heat of the air is transferred to water to realize humidification and cooling, and sensible heat refrigerating capacity is defined as the quantity of sensible heat of the air which is reduced through water evaporation and heat absorption (GB/T25860-2010 evaporative air conditioner). The limit of the evaporation heat absorption of the water is that the humidity content of the air reaches the temperature of saturation state (wet bulb temperature), the temperature of the wet bulb of the ambient air in summer in a dry area is 23 ℃, the temperature is lower than the design air supply temperature (26 ℃) of an air conditioner, and the evaporative air conditioner is available; the temperature of the wet bulb of the summer ambient air in the damp and hot area reaches 28 ℃, and the evaporative air conditioner is not applicable. The international latest improved indirect evaporative cooling technology M-Cycle IEC（Indirect evaporative cooling for buildings: A comprehensive patents review,J. of Building Eng.,2022, v50） cannot overcome the environmental condition limitation, and the IEC technology also has the problems of uniformity of water distribution on the evaporation surface, surface heat transfer dirt removal and the like.
The air conditioner is energy-saving and the exhaust part is recycled to reduce fresh air cooling load or adopt measures (Xu Qian and the like) such as the recovery of exhaust air cooling capacity of a rotary wheel, diagnosis and modification of an anti-virus-based mail wheel air conditioner ventilation system, jiangsu ships, 2022, v39/n2, but the problem of air pollutant diffusion in public space is caused by the air conditioner ventilation system, and the air conditioner ventilation system is more and more forbidden.
The principle of the energy-saving measure of the air conditioner is that the cooling capacity (cold energy) of normal-temperature air is utilized, especially when the air is in contact with the water surface, latent heat of water is carried away in a mode of absorbing water vapor, no temperature difference or even negative temperature difference (the air temperature is higher than the water temperature) is realized, the process driving force is from the difference (ps-pw) between the saturated vapor pressure ps on the water surface and the water vapor partial pressure pw of air flow, and the physical essence is that the driving force enables water vapor molecules to continuously migrate from a gas-water interface to an air flow main body and to move along with the air flow, so that water molecules on the interface are enabled to continuously absorb heat and vaporize to generate a cooling effect. According to the principle, the measure of fully utilizing the cold energy of normal-temperature air is firstly that the total water vapor partial pressure pw of the air (hereinafter referred to as working air) is low, and meanwhile, the saturated vapor pressure ps of an air-water interface is high, so that the required process driving force (ps-pw) is obtained; under certain driving force conditions, the strengthening process has the measures of improving the specific surface area a of the direct contact of gas and water and the mass transfer coefficient kp so as to improve the vaporization strength mw=a.kp. (ps-pw). Therefore, the invention provides a fluidization method for comprehensively utilizing cold energy of normal-temperature air, so that the vaporization and mass transfer process is carried out on the surface of fluidized gas-solid particles, and the specific surface area a and the mass transfer coefficient kp of the fluidization gas-solid particles are higher than those of common fillers by more than one order of magnitude; meanwhile (aiming at application occasions), the normal-temperature air fluidization system absorbs heat and heats up by utilizing waste heat transfer, so that the interface saturated vapor pressure ps is improved, the process driving force (ps-pw) is improved, the application effect of normal-temperature air cold energy is strengthened in various aspects, and the refrigeration intensity calculated according to the surface area of equipment is improved by a plurality of times compared with the IEC technology. In addition, because the heat absorption, vaporization and mass transfer process mainly occurs on the surface of fluidized moving particles, the problem of uneven water distribution is solved, the surface of equipment is prevented from being influenced by dirt, and the operation reliability of the equipment is improved. The method has wide application occasions, such as 92-95 ℃ solar hot water auxiliary refrigeration air conditioner, realizes full fresh air conditioner refrigeration with the temperature of 26 ℃ and the relative humidity below 60% under the condition that the temperature of the dry bulb of the summer ambient air in a damp and hot area is 38 ℃, and the comprehensive energy efficiency coefficient (converted into cold energy/electric energy) is more than 3.1; the method is applied to replace an air cooling technology, waste heat at 60 ℃ is utilized to carry out wastewater vaporization regeneration, and water resource recycling is realized on the premise of not increasing comprehensive energy consumption of a factory.
Disclosure of Invention
The invention discloses a fluidization method for comprehensively utilizing cold energy of normal-temperature air. The method is suitable for various occasions such as fresh air clean refrigeration air conditioner, turbine exhaust steam condensation, waste water regeneration and recycling. As shown in figure 1, the fresh air clean refrigeration air conditioner uses the air conditioner exhaust of the public space as working air, cools and dehumidifies fresh air (clean atmosphere), and provides dry bulb temperature 23-25 ℃ and relative humidity 50-60% (moisture content 11.5-12.5 g/kg-DA, DA represents dry air and the same as the following) fresh air conditioner air supply for the public space. Firstly, the air-conditioning exhaust and the sanitary disinfection are used as a mode for utilizing air cooling energy, as shown in figure 1, the air-conditioning exhaust and the sanitary disinfection aqueous solution are sprayed and mixed, the air-conditioning exhaust and the sanitary disinfection aqueous solution uniformly flow into each descending pipe from the top pipe box of the exhaust humidifying/fresh air cooling heat exchanger 1 to form two-phase flow of air-mist with the flow rate of 8-10 m/s, the pipe wall absorbs heat to enable mist drops in the air flow to be vaporized, and fresh air passes over the fin surface from top to bottom outside the pipe to release heat and cool. And separating the gas-fog mixture in the pipe from a bottom pipe box, cooling the exhaust gas to 23-25 ℃, increasing the moisture content to 18.5-19.2 g/kg-DA, and cooling the fresh air outside the pipe to 26-27 ℃ corresponding to the gas-fog mixture. The separated fog drops are condensed and sent back to the top pipe box through a micro pressurizing circulating pump 6 below the bottom pipe box to be combined with newly-added sanitary disinfectant solution for spraying circulation, the ratio of the mass flow of the circulating solution to the mass flow of air-conditioning exhaust is 1:50-60, and the amount of the newly-added sanitary disinfectant solution is equal to the sum of the vaporization amount of exhaust humidification and the blowdown amount of the disinfectant solution of the bottom pipe box (the blowdown amount is 50-60% of the vaporization amount).
The fresh air cooled to 26-27 ℃ continuously passes through the surface heat release, cooling and dehumidifying of the outer fin of the tube of the falling film evaporation/fresh air cooling dehumidifier 2, heat is transferred to the pure water falling film evaporation in the tube through the tube wall, the heat transfer temperature difference between the surface fresh air cooling and dehumidifying heat release of the outer fin of the tube and the heat transfer temperature difference between the heat absorption of the pure water falling film evaporation in the tube is 2-3 ℃, and the evaporation strength is not lower than 4.5kg/h.m 2. And cooling the fresh air outside the pipe to 17-18 ℃ at the bottom of the dehumidifier 2, and reducing the moisture content to 11.5-12.5 g/kg-DA, and pressurizing the fresh air by a blower to enter a fresh air conveying and distributing main pipe of the clean air conditioner. The falling film evaporation in the pipe generates low-pressure water vapor with the temperature not lower than 15 ℃ and the pressure not lower than 1.74kPa (absolute pressure, the same applies below), and after the bottom pipe box is separated from the falling film liquid, the low-pressure water vapor is sucked into the steam ejector 3 through the low-pressure water vapor outlet control valve 12; the falling film liquid is pressurized by a falling film circulating pump 7 and returns to the top pipe box of the falling film circulating pump 2 for circulation, and the circulating mass flow is 15-20 times of the falling film evaporation capacity.
The working steam of the steam ejector 3 is provided by a multi-layer coil evaporator 4, the temperature of the working steam is 85-90 ℃, the pressure is 58-68 kPa (absolute pressure, the same applies below), the heat energy for generating the working steam is from circulating hot water of a flat-plate solar water heater at 92-95 ℃, heat release is generated by spirally flowing from the uppermost layer to the lower layer in a multi-layer coil 4-2 horizontally arranged in the evaporator 4 at a flow speed of 2.0-2.5 m/s, and the temperature of circulating backwater at the outlet of the lowermost layer coil is not lower than 86 ℃. Pure water is uniformly distributed on the surfaces of the uppermost two layers of coils through the coil surface water distributors 4-1, and drops to the surface of the next coil arranged in a staggered manner while absorbing heat and vaporizing, and unvaporized pure water drops to the liquid surface at the bottom, wherein the liquid level is just enough to enable the lowermost two layers of coils to be completely immersed below the liquid surface, so that the water replenishing added in the uppermost two layers of coils is heated by the coils to be heated to above 85 ℃, and then is pressurized and conveyed to the water distributors 4-1 for circulation through the coil evaporator circulating pump 9; the water distribution amount pressurized by the circulating pump 9 is 5-10 times of the working steam amount generated by the evaporator 4. The generated working steam is accelerated into supersonic airflow with the pressure lower than 1.7kPa by the ejector 3, and the low-pressure water steam obtained by suction falling film evaporation is mixed with the supersonic airflow with the pressure lower than 1.7kPa to be mixed steam with the temperature higher than 36 ℃ and the pressure higher than 6kPa, and is sent to the fluidization condensing combination 5 for condensation.
The fluidization condensing combination 5 comprises a fin tube bundle 5-2 immersed in the particle layer of the gas-solid fluidized bed and a gas distribution plate 5-1 at the bottom of the fluidized bed; the positions of the fin tube bundles are arranged according to the height of one end and the height of the other end, the included angle between the tube axes and the horizontal is 5-8 degrees, water vapor to be condensed uniformly distributes and flows into each tube through a distributor connected with the high ends of the fin tube bundles to form inclined convection condensation heat release in the tubes, heat is transferred to fluidized particle layers outside the tubes through fins on the tube walls, condensate and uncondensed water vapor flowing in the tubes flow into a condensation space of an auxiliary condenser 5-3 connected with the condensation space from the tube openings at the low ends of the tube bundles, and heat release is continuously carried out on the fins outside cooling water tubes (below 35 ℃) arranged in the condensation space to be completely condensed; condensed water accumulated in the auxiliary condenser 5-3 is pressurized by a water return pump 8 and is supplemented with water to the top of the falling film evaporation/fresh air cooling dehumidifier 2 and the bottom of the multi-layer coil evaporator 4 respectively by a low-pressure water return control valve 10 and a coil evaporator water return control valve 11 according to the ratio of the low-pressure water vapor quantity to the working vapor quantity; the non-condensable gas in the condensing space is periodically pumped out by a non-condensable gas pumping control valve 5-4 connected with the condensing space to keep the ratio of the partial pressure of the non-condensable gas to the partial pressure of the water vapor in the condensing space to be less than (0.5/1000). The fully closed pure water and water vapor circulation space is divided into a low-pressure area and a variable pressure working area by a low-pressure backwater control valve 10 and a low-pressure water vapor outlet control valve 12, the valves 10 and 12 are closed in a stop period and a start period, all devices (including 4,4-1,4-2,9,3,5,5-1,5-2,5-3,5-4 and 8) in the variable pressure working area are operated normally in the start period, and then the valves 10 and 12 are synchronously opened.
The heat absorption process of the fluidized particle layer outside the fin tube bundle is realized by the following steps: in the fluidized bed with the rectangular cross section shown in fig. 1, the particle layer is composed of spherical wear-resistant particle groups uniformly stacked outside the fin tube bundles, the particle size of the particle groups is 0.8-1.2 mm, the density is 550-650 kg/m 3, the initial fluidization speed is 0.3-0.5 m/s, and the stacking height of the particle layer (i.e. the distance from the gas distribution plate 5-1 to the upper surface of the particle layer in a static state) is 0.3-0.5 m; the air conditioning exhaust (working air) at the temperature of 23-25 ℃ from the exhaust humidifying/fresh air cooling heat exchanger 1 uniformly passes through the gas distribution plate 5-1 with the aperture of not more than 0.6mm at the initial fluidization speed of 2-5 times, fully fluidizes the particle layer above the gas distribution plate to form a fluidized bed layer, and the upper surface of the fluidized bed layer rises to the stacking height of more than 2 times of the static particle layer and completely floods the fin tube bundles; the lowest point of the fins below the low end of the fin tube bundle is 35-50 mm away from the upper surface of the distribution plate, and working water (wastewater or tap water meeting the environmental emission standard) is sprayed and introduced into the fluidized bed layer from the high end side of the fin tube bundle, wherein the ratio of the mass flow of the working water to the mass flow of the working air is not more than 1/30; the working air drives the water mist and the fluidized particle groups to be vigorously stirred and mixed and to continuously collide with the outer surface of the tube bundle and the surfaces of the fins for heat transfer, the temperature is raised from 23-25 ℃ while absorbing heat and vaporizing to not more than 5 ℃ with the temperature difference of a heat release medium in the fin tube, a high-strength condensation effect is formed on the water vapor at 33-36 ℃ flowing in the fin tube bundle, and the condensation strength calculated according to the inner surface area of the fin tube is not lower than 6.1kg/h.m 2; the working air absorbs heat in the fluidized bed, heats and humidifies to the saturated vapor pressure, leaves the upper surface of the bed, continuously flows in the free space at the upper part of the bed for 0.2-0.3 m, and finally passes through a screen with the aperture not more than 0.2mm arranged at the top of the fluidization condensing combination 5 to be discharged.
The auxiliary flat plate type solar heat collection clean refrigeration all fresh air conditioning system for the air conditioning exhaust fluidization cold energy completely avoids the problem of public space air conditioning air supply sanitation risk, and the comprehensive refrigeration coefficient of performance COP (sum of refrigeration load/consumed electric energy and solar energy calculation equivalent electric energy) is more than 3.1, which is superior to the specified value (table 4.2.10) of the refrigeration coefficient of performance of an evaporative cooling compression type cold water (heat pump) unit in GB50189-2015 public building energy-saving design standard.
The method for realizing the exhaust steam condensation and the wastewater regeneration by using the fluidized air cooling is shown in the attached figure 2: the low-pressure saturated water vapor with the temperature not exceeding 45 ℃ is any one of steam turbine final-stage exhaust steam or waste water vaporization regeneration steam, the working gas is waste gas meeting the atmospheric emission standard or directly adopts ambient air, and the working water is any one of waste water or regenerated water meeting the environmental emission standard. The low-pressure steam enters the fluidization condensing combination 5 through the inlet control valve 12, flows into each tube of the fin tube bundle 5-2 immersed in the gas-solid fluidization bed through the distributor connected with the high end of the fin tube bundle to form oblique convection condensation heat release in the tube, heat is transferred to the outside of the tube through the tube wall and the fins to fully fluidize the particle layer, the low-pressure steam in the tube is completely condensed, condensed water and noncondensable gas flow into the end cover 5-5 connected with the tube bundle from the low end tube opening of the tube bundle, condensed water is pressurized by the water return pump 8 to be sent out for recycling, and the noncondensable gas is periodically pumped out through the noncondensable gas pumping control valve 5-4 connected with the space to ensure that the partial pressure ratio occupied by the noncondensable gas in the condensing space is less than 0.5/1000.
The external gas-solid fluidized bed of the finned tube bundle and the heat absorption thereof are realized according to the following method: the working gas at the temperature of 20-35 ℃ uniformly passes through a gas distribution plate 5-1 with the aperture not exceeding 0.6mm at the flow rate of 2-5 times of the initial fluidization speed of particles (the particle size is 0.8-1.2 mm, the density is 550-650 kg/m 3 and the initial fluidization speed is 0.3-0.5 m/s), so that the height of a gas-solid fluidized bed formed by fully fluidizing the wear-resistant particle groups with the stacking height of 0.3-0.5 m is increased to be more than 2 times of the stacking height of the particles and the fin tube bundles are completely submerged; the arrangement method of the fin tube bundles is the same as that described above, and the working water spray is introduced into the fluidized particle layer from the high end side thereof, and the ratio of the mass flow rate of the working water to the mass flow rate of the working gas is 1: 20-50, wherein the working gas drives water mist and fluidized particle groups to be vigorously stirred and mixed and continuously scour the outer surface of a tube bundle and the surfaces of fins, so that the cooling effect of absorbing heat and vaporizing and humidifying at the same time is formed to strengthen the condensation of water vapor with the temperature of not more than 45 ℃ in the fin tubes, and the condensation strength calculated according to the inner surface area of the fin tubes is not lower than 15kg/h.m 2; the working gas absorbs heat through the fluidized bed particle layer, is heated to not more than 42 ℃ and is humidified to not more than 55g/kg-DA, continuously flows for 0.2-0.3 m in the upper space after flowing out of the fluidized bed, and finally passes through a screen with the aperture below 0.2mm arranged at the top of the fluidized condensation combination 5 to be discharged.
Drawings
Fig. 1 is a schematic diagram of the method for comprehensively utilizing normal-temperature air cold energy to fluidize and refrigerate fresh air clean air conditioner and fig. 2 is a schematic diagram of the method for realizing exhaust steam condensation and wastewater regeneration by using fluidization air cooling.
Fig. 1 and 2: 1-an exhaust humidifying/fresh air cooling heat exchanger; 2-falling film evaporation/fresh air cooling dehumidifier; 3-a steam ejector; 4-multilayer coil evaporator; 4-1-coil surface water distributor; 4-2-multilayer coil; 5-fluidization condensing combination; 5-1-a gas distribution plate; 5-2-fin tube bundles; 5-3-secondary condenser; 5-4-pumping non-condensable gas control valve; 5-5-end caps; 6-a micro pressurized circulation pump; 7-a falling film liquid circulating pump; 8-a condensate water return pump; 9-coil evaporator circulation pump; 10-a low-pressure backwater control valve; 11-coil evaporator backwater control valve; 12-low pressure water vapor outlet/inlet control valve.
Figures 1 and 2 are further described below in conjunction with the examples.
Detailed Description
The following describes embodiments of the invention in connection with, but not limited to, examples
Example 1: the full fresh air conditioner in the public space 10000m 3/h uses the air cooling energy of the air conditioner to cool in a fluidization way.
Ambient air conditions: the dry bulb temperature was 38℃and the moisture content was 21.2g/kg-DA. The refrigerating and air supplying conditions of the fresh air conditioner are as follows: the dry bulb temperature is 23-25 ℃, the moisture content is 11.5-12.5 g/kg-DA (relative humidity is 50% -60%). Meanwhile, the public space air conditioner exhaust (dry bulb temperature 26 ℃ C., moisture content 12.5 g/kg-DA) is required to be fully sterilized and then is intensively discharged. The public space roof flat plate type solar water heater is used for heating 60m 3/h circulating hot water from 88 ℃ to 93 ℃ to be used as a low-level heat refrigerating heat source.
As shown in the figure 1, an exhaust fan with 9.0kW power is used for pressurizing air-conditioning exhaust 9000m 3/h at 26 ℃ to 2.0-2.5 kPa, the air-conditioning exhaust 9000m 3/h enters a top pipe box of an exhaust humidifying/fresh air cooling heat exchanger 1, and is sprayed and mixed with 230kg/h sanitary disinfectant aqueous solution to form an aerosol-aerosol two-phase flow, the aerosol-aerosol two-phase flow flows into pipes at a flow rate of 10m/s uniformly distributed, the exhaust self-cooling and heat release and the heat absorption from pipe walls are carried out to enable fog drops to be vaporized, and the aerosol drops flow to a bottom outlet temperature of 24 ℃ and are humidified to 17.8g/kg-DA; and 10000m 3/h of fresh air which is correspondingly led to pass through the surface of the fin from top to bottom outside the pipe is discharged and cooled to the outlet temperature of 28 ℃, and the moisture content is unchanged. The gas-fog flow is separated in the bottom pipe box, 133kg/h of fog drops which are not vaporized are circularly sent back to the top pipe box through the micro pressure pump 6 and are converged with 97kg/h of newly-added sanitary disinfectant water solution to enter the spraying circulation, and 35kg/h of fog drops are discharged from the bottom pipe box.
The fresh air cooled to 28 ℃ by the process is continuously discharged, cooled and dehumidified from top to bottom through the surfaces of the outer fins of the pipes of the falling film evaporation/fresh air cooling dehumidifier 2, cooled and dehumidified to 18 ℃ at the outlet, and conveyed to a public space below 12.5g/kg-DA, so that the cooling capacity loss temperature in the air conveying and distributing process is allowed to rise by 4-5 ℃, and the clean fresh air obtained by a user meets the air supply condition of a comfortable air conditioner.
Sensible heat and latent heat released by fresh air in the cooling dehumidifier 2 are transmitted to a pure water falling film evaporation process with the temperature in the pipe not lower than 15 ℃ through the outer surface of the finned pipe, the evaporation intensity is not lower than 5.0kg/h.m 2, low-pressure steam 175 kg/h with the pressure not lower than 1.7kPa is generated, and the low-pressure steam is sucked into the steam injector 3 through the low-pressure steam outlet control valve 12; the falling film circulating pump 7 conveys 2500-3000 kg/h pure water from the bottom pipe box of the 2 to the top pipe box of the 2 for circulation.
The low-pressure steam is sprayed and sucked into the steam sprayer 3 by working steam with the temperature of 480 kg/h not lower than 87 ℃ and the pressure not lower than 62kPa, and the working steam are mixed into 655kg/h of saturated steam with the temperature of 37 ℃ and sent to the fluidization condensing combination 5 for condensation. The working steam is generated by the following steps: circulating hot water heated to 93 ℃ by a flat plate type solar collector is 60m 3/h, convection heat is released from the inside of a multilayer coil 4-2 pipe at a flow rate of 2.2m/s from top to bottom, 2800 kg/h pure water uniformly distributed on the surface of the coil through a coil surface water distributor 4-1 is partially vaporized to generate 480 kg/h working steam, unvaporized pure water drops into a liquid phase outside the two lowest layers of coils 4-2, and the unvaporized pure water is converged with 37 ℃ condensed water 480 kg/h sent by a water return pump 8 and heated to above 87 ℃ and then pressurized by a coil evaporator circulating pump 9 to be sent to the coil surface water distributor 4-1 above the top coil for circulation; the hot water in the coil pipe circularly flows to release heat until the return water temperature at the outlet of the lowest coil pipe is reduced to 88 ℃, and the return water is sent to the flat-plate solar water heater to reheat to 93 ℃ and returned to the 4-2 circulating hot water inlet.
The 37 ℃ saturated steam condensing process sent from the steam ejector 3 to the fluidization condensing combination 5 is as follows: the water vapor flows into each tube through the distributor at the high end of the fin tube bundle 5-2, forms oblique convection condensation heat release in the tubes, the condensed liquid and the uncondensed water vapor flow into the auxiliary condenser 5-3 connected with the tube bundle 5-2 from the low end tube orifice, are completely condensed and converged into 655kg/h pure water, the pure water is pressurized by the water return pump 8, 175 kg/h is distributed to the falling film evaporation/fresh air cooling and dehumidifying device 2 through the low-pressure water return control valve 10, and 480 kg/h is supplemented to the bottom of the multi-layer coil evaporator 4 through the coil evaporator water return control valve 11. The condensation heat of the auxiliary condenser 5-3 is taken away by 60m 3/h cooling water (at the temperature of 29 ℃ and the temperature of 34 ℃) through convection heat absorption in the finned tube, and noncondensable gas is periodically pumped out through the noncondensable gas pumping control valve 5-4 so as to keep the ratio of partial pressure of noncondensable gas to partial pressure of water vapor in the condensation space smaller than (0.5/1000).
The process and method for absorbing condensation heat by the fluidized particle layer outside the fin tube bundles 5-2 of the fluidized condensation combination 5 are as follows: the particle group is hollow ceramic microbeads screened from fly ash, the particle size is 1.1-1.2 mm, the density is 600kg/m 3, the initial fluidization speed is 0.42m/s, and the stacking height of a particle layer is 0.35m; the air-conditioning exhaust gas at 24 ℃ after being cooled and humidified by the heat exchanger 1 uniformly passes through a gas distribution plate 5-1 with the aperture of 0.5mm at the speed of 1.6 m/s to enable the particle layer to be fully fluidized, and the height is increased to 0.8m to enable the fin tube bundles to be completely submerged; 130 kg/h tap water spray is introduced into the fluidized particle layer from the high end side of the fin tube bundle 5-2, is mixed with the fluidized particle group in a fierce stirring way, collides with the outer surface of the fin tube bundle, absorbs heat while vaporizing, ensures that the condensation intensity of low-pressure water vapor at 37 ℃ flowing in the fin tube bundle is not lower than 10kg/h.m 2, and air-conditioning exhaust is heated to 31 ℃ through the heat absorption of the fluidized particle layer and humidified to 29g/kg-DA and discharged from a position 0.2m above the particle layer through a screen mesh with the aperture of 0.2 mm.
The example fluidization utilizes 9000m 3/h air conditioner exhaust cooling, assists the flat plate type solar heat collector to supply heat, and water vapor jet refrigeration 10000m 3/h fresh air cleaning air conditioner has the beneficial effects that the solar refrigeration air conditioner only uses air and water as working media, completely avoids the public space air conditioner air supply sanitary risk, the refrigeration load is 160kW, the power consumption is 15.2kW, the flat plate type solar heat collector converts equivalent electric power into 34.8kW, the comprehensive refrigeration performance coefficient is COP=160/(15.2+34.8) =3.2, and the air conditioner has excellent low-carbon cooling characteristics.
Example 2: fluidization is carried out on 40 ℃ process wastewater by utilizing workshop ventilation and exhaust cold energy and 60 ℃ process waste heat.
1100Kg/h of process wastewater, and the water quality meets the environmental emission standard. The workshop sanitary ventilation is 10000m 3/h, the temperature is 20 ℃, and the moisture content is 8.5g/kg-DA. The process waste heat at 60 ℃ is obtained from the evaporation and concentration waste steam in a chemical workshop, and the waste steam saturation temperature is 60 ℃ through connecting the inlet of a water jet condenser with a main pipe.
The saturated steam with the temperature of 60 ℃ is shunted from the evaporation concentration waste steam header pipe to be 650kg/h, the saturated steam with the temperature of 60 ℃ is used as a heat source to heat and vaporize the process waste water, the regenerated steam with the temperature of 45 ℃ is generated 620 kg/h, the process waste water is led into the fluidization condensation combination 5 through a low-pressure steam inlet control valve shown in the attached drawing figure 2, the heat is transferred to the fluidization particle layer outside the tube through the fins on the tube wall by convection condensation in the inclined tube of the fin tube bundle 5-2 which is immersed in the gas-solid fluidization particle layer, the low-pressure steam in the tube is completely condensed, the condensed water and the non-condensable gas flow into the end cover 5-5 connected with the tube bundle from the low-end pipe orifice of the tube bundle, the regenerated condensed water is pressurized and sent 620 kg/h for process circulation use through the water return pump 8, and the non-condensable gas is periodically pumped out through the non-condensable gas pumping control valve 5-4 connected with the space. The heat absorption process of the fluidized particle layer outside the pipe is realized by the following steps: the hollow ceramic microbeads screened from the fly ash are piled up on the particle layer above the gas distribution plate 5-1, the particle size is 1.1-1.2 mm, the density is 600kg/m 3, the initial fluidization speed is 0.42m/s, and the piling height of the particle layer is 0.35m; the sanitary ventilation exhaust of the workshop at 20 ℃ is pressurized to 1.5kPa as working air by a fan at 10000m 3/h, uniformly passes through a gas distribution plate 5-1 with the aperture of 0.5mm at the speed of 1.6 m/s, so that the particle layer is fully fluidized, and the height of the upper surface of the particle layer is raised to 0.8m, so that the fin tube bundles are completely submerged; 480 kg/h of process wastewater is sprayed into a fluidized particle layer from the high end side of a fin tube bundle 5-2, working air drives the water mist to be strongly stirred and mixed with the fluidized particle group, the water mist is continuously contacted with the outer surface of the tube bundle and the surface of the fin, the temperature is raised when the water mist is absorbed from 20 ℃ and is vaporized, the condensation effect of not less than 16kg/h.m 2 is formed on regenerated water vapor at 45 ℃ flowing in the fin tube bundle, the temperature is raised to 40 ℃ when the working air is absorbed, the working air is humidified to 45.7g/kg-DA, and the working air leaves the upper surface of the fluidized particle layer and continuously flows for 0.2m in the upper space of the working air and then passes through a screen with the aperture of 0.2mm to be discharged.
The energy saving and emission reduction effect of the method is that 1100kg/h of wastewater regeneration treatment is realized by fluidization using 10000m 3/h of sanitary ventilation and exhaust cold energy (620 kg/h of regenerated condensed water is obtained and 480 kg/h of atmospheric pressure is consumed), the electricity consumption of a sanitary ventilation and exhaust pressurizing fan is 6.5kW.h, the electricity consumption of a small centrifugal water pump and the like is not more than 3.5kW.h, the electricity consumption of a water injection condenser is reduced by 650kg/h of wastewater steam condensation load, 15kW.h of electricity consumption can be saved (including 11kW.h of water pump electricity consumption and 4kW.h of water cooling tower fan electricity consumption), and the comprehensive energy consumption of a workshop can be saved while the fluidization of the method realizes wastewater regeneration by using workshop ventilation and exhaust cold energy and 60 ℃ process waste heat.
The invention is not limited to the embodiments described above, the technical solutions of which have been described in the summary section.
Claims (3)
1. A fluidization method for comprehensively utilizing cold energy of normal-temperature air is characterized in that water mist is sprayed into a fluidization particle layer, vaporization mass transfer process is carried out on the surface of fluidization gas-solid particles, and water vapor molecules are enabled to continuously migrate from a gas-water interface to a gas flow main body and move along with the gas flow, so that water molecules on the interface are enabled to continuously vaporize and absorb heat to generate cooling and refrigerating effects;
heat is transferred to the spray gas-solid fluidized particle layer, so that the spray gas-solid fluidized particle layer absorbs heat and heats up, the saturated water vapor pressure of an interface is improved, the driving force in the vaporization process is improved, the application effect of normal-temperature air cold energy is enhanced, and the refrigeration intensity calculated according to the surface area of equipment is improved by a plurality of times compared with the prior art;
The fluidization particle layer absorbs heat in the following steps: the particle layer in the fluidized bed with the rectangular cross section is composed of spherical wear-resistant particle groups uniformly stacked outside the fin tube bundles, the particle size of the particle groups is 0.8-1.2 mm, the density is 550-650 kg/m 3, the initial fluidization speed is 0.3-0.5 m/s, and the stacking height of the particle layer is 0.3-0.5 m; uniformly passing normal-temperature working air through a gas distribution plate with the aperture of not more than 0.6mm at an initial fluidization speed of 2-5 times to enable a particle layer above the air distribution plate to become a fluidized bed with sufficient fluidization, raising the upper surface of the air distribution plate to be more than 2 times of the stacking height of a static particle layer, and completely submerging a fin tube bundle; enabling the lowest point of the fins of the fin tube bundle to be 35-50 mm away from the distribution plate, and spraying and introducing working water into the fluidized bed from a position higher than the position, wherein the ratio of the mass flow of the working water to the mass flow of working air is not more than 1/30; the working air drives the water mist and the fluidized particle group to be vigorously stirred and mixed and to continuously collide with the outer surface of the tube bundle and the surfaces of the fins for heat transfer, the temperature is raised to be not more than 5 ℃ with the temperature difference of the exothermic medium in the fin tube while absorbing heat, the working air is heated and humidified to the saturated vapor pressure, the working air leaves the upper surface of the bed layer and continuously flows for 0.2-0.3 m in the upper free space of the bed layer, and finally the working air is discharged through a screen with the aperture not more than 0.2mm arranged at the top.
2. The fluidization method for comprehensively utilizing cold energy of normal-temperature air is characterized by taking the exhaust air of a public space air conditioner as working air, cooling and dehumidifying fresh air, providing fresh air conditioner air supply with dry bulb temperature of 23-25 ℃ and relative humidity of 50-60%, and simultaneously carrying out sanitary disinfection on the exhaust air of the air conditioner;
The air conditioner exhaust and the sanitary disinfection are used as a mode of utilizing air cooling energy, the air conditioner exhaust and the sanitary disinfection aqueous solution are sprayed and mixed, an air-fog two-phase flow with the flow speed of 8-10 m/s is formed in a descending pipe of an exhaust humidifying/fresh air cooling heat exchanger, the heat is absorbed from the pipe wall to enable fog drops in the air flow to be vaporized, and fresh air passes through the surface of a fin from top to bottom outside the pipe to release heat and cool; the gas-fog mixture in the pipe flows to a bottom pipe box, the temperature of exhaust is reduced to 23-25 ℃, the temperature is humidified to 18.5-19.2 g/kg-DA, and fresh air outside the pipe is cooled to 26-27 ℃; the sanitary disinfectant after gas-fog separation and condensation is returned to the top pipe box from the bottom pipe box through a micro pressurizing circulation pump, and is combined with newly-added sanitary disinfectant solution for spraying circulation, wherein the ratio of the mass flow of the circulating solution to the mass flow of air-conditioning exhaust is 1:50-60, the amount of the newly-added sanitary disinfectant solution is equal to the sum of the humidification vaporization amount of exhaust and the discharge amount of the disinfectant of the bottom pipe box, and the discharge amount is 50-60% of the vaporization amount;
The fresh air cooled to 26-27 ℃ is continuously subjected to heat release, cooling and dehumidification through the surface of the outer fin of the tube of the falling film evaporation/fresh air cooling dehumidifier, and heat is transferred to pure water falling film evaporation in the tube through the tube wall, the heat transfer temperature difference is 2-3 ℃, and the evaporation intensity is not lower than 4.5kg/h.m 2; the fresh air outside the pipe is cooled to 17-18 ℃ through a cooling dehumidifier, the moisture content is reduced to 11.5-12.5 g/kg-DA, and the fresh air enters a fresh air delivery and distribution main pipe of the clean air conditioner through the pressurization of a blower; the falling film evaporation generates low-pressure water vapor with the temperature not lower than 15 ℃ and the pressure not lower than 1.74kPa, the low-pressure water vapor is pumped into a vapor injector, the falling film liquid circulates through a falling film circulating pump, and the circulating mass flow is 15-20 times of the falling film evaporation capacity;
The multi-layer coil evaporator provides working steam with the temperature of 85-90 ℃ and 58-68 kPa for the steam ejector, heat energy of the working steam is generated from circulating hot water of a flat-plate solar water heater with the temperature of 92-95 ℃, heat is released by spirally flowing from the uppermost layer to the lower layer at a flow rate of 2.0-2.5 m/s in a multi-layer coil horizontally arranged in the evaporator, and the temperature of circulating backwater from the outlet of the lowermost layer coil is not lower than 86 ℃; pure water is uniformly distributed on the surfaces of the uppermost two layers of coils through the coil surface water distributors, and drops to the surface of the next coil arranged in a staggered way while absorbing heat and vaporizing, unvaporized pure water drops to the liquid level at the bottom of the evaporator, the liquid level just enables the lowermost two layers of coils to be completely immersed below the liquid level, the water added in the uppermost two layers of coils is heated by the coils to be heated to more than 85 ℃, and then the water is pressurized and conveyed to the water distributors for circulation through the coil evaporator circulating pump; the circulating water distribution amount is 5-10 times of the working steam amount generated by the evaporator; the generated working steam is accelerated into supersonic airflow with the pressure lower than 1.7kPa through an ejector, and low-pressure water vapor generated by suction falling film evaporation is mixed with the supersonic airflow with the pressure lower than 1.7kPa to form mixed steam with the temperature higher than 36 ℃ and the pressure higher than 6kPa, and the mixed steam is sent to a fluidization condensation combination for condensation;
The fluidization condensation combination comprises a fin tube bundle immersed in the particle layer of the gas-solid fluidized bed with a rectangular cross section and a gas distribution plate at the bottom of the fluidized bed; the method comprises the steps that a fin tube bundle is arranged, one end of the fin tube bundle is high, the other end of the fin tube bundle is low, the included angle between the tube axis and the horizontal angle is 5-8 degrees, water vapor to be condensed flows into each tube through a distributor connected with the high end of the fin tube bundle, oblique convection condensation releases heat, heat is transferred to a fluidized particle layer outside the tube through fins on the tube wall, condensate and uncondensed water vapor flow into an auxiliary condenser connected with the tube bundle from the tube orifice at the low end of the tube bundle, heat is continuously released and fully condensed on the fins at the temperature below 35 ℃ outside a cooling water tube in the auxiliary condenser, the condensed water is pressurized through a water return pump, and water is supplemented to a falling film evaporation/fresh air cooling dehumidifier and a multi-layer coil evaporator through a low-pressure water return control valve and a coil evaporator water return control valve respectively according to the ratio of low-pressure water vapor quantity to working vapor quantity; the non-condensable gas in the condensation space is periodically pumped out after passing through a non-condensable gas pumping control valve to keep the ratio of the partial pressure of the non-condensable gas to the partial pressure of the water vapor less than 0.5/1000; the low-pressure backwater control valve and the low-pressure water vapor outlet control valve divide the completely sealed pure water and water vapor circulation space in the fluidization condensation combination into a low-pressure area and a pressure-changing working area, the two valves are closed in the stopping period and the starting initial period, and after the two valves are started, all devices in the pressure-changing working area are normally operated, and then the two valves are synchronously opened;
The fluidization is implemented by the steps, the exhaust cold energy is used for assisting the flat plate type solar heat collection refrigeration, the comprehensive refrigeration coefficient of performance COP of the public space fresh air cleaning air conditioner is more than 3.1, the air supply hygienic risk is completely avoided, and the air conditioner exhaust is intensively discharged after being subjected to hygienic disinfection.
3. The fluidization method for comprehensively utilizing cold energy of normal-temperature air according to claim 1, wherein the method is characterized in that the waste steam condensation and the wastewater regeneration are realized by utilizing fluidization air cooling; the low-pressure saturated water vapor with the temperature not exceeding 45 ℃ is any one of steam turbine final stage exhaust steam or waste water vaporization regeneration steam, the working gas is waste gas meeting the atmospheric emission standard or directly adopts ambient air, and the working water is any one of waste water or regenerated water meeting the environmental emission standard; the low-pressure steam enters a fluidization condensation combination through an inlet control valve, flows into each tube of a fin tube bundle immersed in a gas-solid fluidization bed through a distributor connected with the high end of the fin tube bundle to form oblique convection condensation heat release in the tube, heat is transferred to the outside of the tube through the tube wall and the fins to fully fluidize a particle layer, so that the low-pressure steam in the tube is completely condensed, condensed water and noncondensable gas flow into an end cover connected with the low-end tube opening of the tube bundle from the low-end tube opening of the tube bundle, the condensed water is pressurized and sent out for recycling through a water return pump, and the noncondensable gas is periodically pumped out through a noncondensable gas pumping control valve to ensure that the partial pressure ratio of the noncondensable gas in a condensation space is less than 0.5/1000;
The method for absorbing heat of the gas-solid fluidized bed outside the finned tube bundle comprises the following steps: the method comprises the steps that the wear-resistant particles of a gas-solid fluidized bed have a particle size of 0.8-1.2 mm, a density of 550-650 kg/m 3 and an initial fluidization speed of 0.3-0.5 m/s, working gas at the temperature of-20-35 ℃ uniformly passes through gas distribution with the aperture not exceeding 0.6mm at a flow rate which is 2-5 times of the initial fluidization speed of the particles, so that the height of the gas-solid fluidized bed formed by fully fluidizing the particle groups with the stacking height of 0.3-0.5 m on the gas-solid fluidized bed is increased to be more than 2 times of the stacking height and completely submerge fin tube bundles; introducing working water spray into the fluidized particle layer from the high end side of the fin tube bundle, wherein the ratio of the mass flow of the working water to the mass flow of the working gas is 1: 20-50, wherein the working gas drives the water mist and fluidized particle groups to continuously wash the outer surface of the tube bundle and the surface of the fins, and the cooling effect of absorbing heat and vaporizing simultaneously strengthens the condensation of water vapor with the temperature not exceeding 45 ℃ in the fin tubes, and the condensation strength is not lower than 15kg/h.m 2 calculated according to the inner surface area of the fin tubes; the working gas absorbs heat through the fluidized bed particle layer, is heated to not more than 42 ℃, is humidified to not more than 55g/kg-DA, and finally passes through a screen with the aperture below 0.2mm arranged at the top of the fluidization condensing combination to be discharged.
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