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 PDF

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CN117989627A
CN117989627A CN202211322685.2A CN202211322685A CN117989627A CN 117989627 A CN117989627 A CN 117989627A CN 202211322685 A CN202211322685 A CN 202211322685A CN 117989627 A CN117989627 A CN 117989627A
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water
air
gas
heat
working
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朱家骅
夏素兰
李季
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Sichuan University
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    • FMECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F24HEATING; RANGES; VENTILATING
    • F24FAIR-CONDITIONING; AIR-HUMIDIFICATION; VENTILATION; USE OF AIR CURRENTS FOR SCREENING
    • F24F5/00Air-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
    • F24F5/0007Air-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
    • F24F5/0035Air-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
    • FMECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F24HEATING; RANGES; VENTILATING
    • F24FAIR-CONDITIONING; AIR-HUMIDIFICATION; VENTILATION; USE OF AIR CURRENTS FOR SCREENING
    • F24F13/00Details common to, or for air-conditioning, air-humidification, ventilation or use of air currents for screening
    • F24F13/30Arrangement or mounting of heat-exchangers
    • FMECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F24HEATING; RANGES; VENTILATING
    • F24FAIR-CONDITIONING; AIR-HUMIDIFICATION; VENTILATION; USE OF AIR CURRENTS FOR SCREENING
    • F24F8/00Treatment, e.g. purification, of air supplied to human living or working spaces otherwise than by heating, cooling, humidifying or drying
    • F24F8/20Treatment, e.g. purification, of air supplied to human living or working spaces otherwise than by heating, cooling, humidifying or drying by sterilisation
    • FMECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28HEAT EXCHANGE IN GENERAL
    • F28BSTEAM OR VAPOUR CONDENSERS
    • F28B1/00Condensers in which the steam or vapour is separate from the cooling medium by walls, e.g. surface condenser
    • F28B1/02Condensers 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
    • FMECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28HEAT EXCHANGE IN GENERAL
    • F28BSTEAM OR VAPOUR CONDENSERS
    • F28B7/00Combinations 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

一种流态化利用常温空气冷能的清洁空调及乏汽冷凝方法,使空气与水雾混合蒸发冷却传质过程在流态化气‑固颗粒表面进行、其比表面积和传质系数均比常用填料高一个多数量级且无污垢影响,利用低位废热加热该流态化体系提高饱和蒸汽压从而进一步强化常温空气冷能应用效果,大幅提高设备制冷强度和运行可靠性。应用于公共空间排气流态化吸热辅助太阳能制冷全新风空调,综合能效系数COP>3.1且完全避免供、排风卫生风险;应用于辅助利用低位废热进行工艺废水汽化再生,可使一半以上的废水成为再生冷凝水循环使用,且再生过程不增加车间综合能耗。本发明方法具有突出的低碳、节能和环保特征。

A clean air conditioner and exhaust steam condensation method that utilizes cold energy of normal-temperature air by fluidization, so that the air and water mist mixed evaporative cooling mass transfer process is carried out on the surface of fluidized gas-solid particles, and its specific surface area and mass transfer coefficient are more than one order of magnitude higher than those of commonly used fillers and are not affected by dirt. The fluidized system is heated by low-level waste heat to increase the saturated vapor pressure, thereby further enhancing the application effect of normal-temperature air cold energy, greatly improving the refrigeration intensity and operational reliability of the equipment. It is applied to the exhaust fluidization heat absorption auxiliary solar cooling fresh air air conditioner in public spaces, with a comprehensive energy efficiency coefficient COP>3.1 and completely avoiding the hygienic risks of supply and exhaust air; it is applied to assist in the use of low-level waste heat for the vaporization regeneration of process wastewater, so that more than half of the wastewater can be recycled as regenerated condensed water, and the regeneration process does not increase the comprehensive energy consumption of the workshop. The method of the present invention has outstanding low-carbon, energy-saving and environmentally friendly characteristics.

Description

流态化利用常温空气冷能的清洁空调及乏汽冷凝方法Fluidized clean air conditioning and exhaust steam condensation method using cold energy of normal temperature air

技术领域Technical Field

本发明涉及低位能提取与应用和近室温制冷与清洁空调技术,特别是与废气及废水处理相耦合、高效利用常温空气冷能的多相流传热传质技术领域。The present invention relates to low-potential energy extraction and application and near-room temperature refrigeration and clean air conditioning technology, in particular to the field of multiphase flow heat and mass transfer technology that is coupled with waste gas and wastewater treatment and efficiently utilizes room temperature air cooling energy.

背景技术Background technique

近室温制冷技术目前主要应用于夏季空调制冷领域,应用面非常广泛。通常采用蒸汽压缩排热方法不仅能耗大而且显著加剧城市热岛效应,从低碳节能和人居环境保护两大方面都亟待改善。具有显著节能特性的蒸发式冷气机“通过风机使空气与淋水填料层直接接触,把空气的显热传递给水而实现增湿降温”,规定“显热制冷量”为“通过水分蒸发吸热而使通过的空气显热降低的量值”(GB/T 25860-2010 蒸发式冷气机)。水分蒸发吸热的极限是空气湿含量达饱和状态的温度(湿球温度),干燥地区夏季环境空气湿球温度23℃,比空调设计供风温度(26℃)低、蒸发式冷气机可用;湿热地区夏季环境空气湿球温度本身已达28℃,蒸发式冷气机不适用。国际上最新改进的间接蒸发冷却技术M-Cycle IEC(Indirect evaporative cooling for buildings: A comprehensive patents review,J. of Building Eng.,2022, v50)也不能克服上述环境条件限制,同时IEC技术还存在蒸发面布水均匀性及表面传热污垢清除等问题。Near-room temperature refrigeration technology is currently mainly used in the field of air conditioning and refrigeration in summer, and its application is very wide. The steam compression heat removal method usually used not only consumes a lot of energy but also significantly aggravates the urban heat island effect. It is urgently needed to be improved in terms of low-carbon energy saving and human settlement environment protection. The evaporative air cooler with significant energy-saving characteristics "uses a fan to make the air directly contact with the water-spraying filler layer, transfers the sensible heat of the air to the water to achieve humidification and cooling", and stipulates that "sensible heat cooling capacity" is "the value of the sensible heat reduction of the air passing through by absorbing heat through water evaporation" (GB/T 25860-2010 Evaporative Air Cooler). The limit of water evaporation heat absorption is the temperature (wet bulb temperature) at which the air moisture content reaches the saturated state. In dry areas, the wet bulb temperature of the ambient air in summer is 23℃, which is lower than the air conditioning design supply air temperature (26℃), and the evaporative air cooler can be used; in humid and hot areas, the wet bulb temperature of the ambient air in summer has reached 28℃, and the evaporative air cooler is not applicable. The latest internationally 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 above-mentioned environmental conditions. At the same time, IEC technology also has problems such as uniformity of water distribution on the evaporation surface and removal of surface heat transfer dirt.

空调节能还有排气部分循环回用以减少新风冷负荷、或采用转轮回收排气冷量等措施(徐谦等. 基于防病毒的邮轮空调通风系统诊断和改装,江苏船舶,2022,v39/n2),但由此带来空气污染物在公共空间扩散问题,越来越受到禁止。Air conditioning energy saving also includes measures such as recycling part of the exhaust gas to reduce the fresh air cooling load, or using a rotary wheel to recover the exhaust cooling capacity (Xu Qian et al. Diagnosis and modification of cruise air conditioning ventilation system based on antivirus, Jiangsu Shipbuilding, 2022, v39/n2), but the resulting problem of air pollutants spreading in public spaces is increasingly prohibited.

上述空调节能措施的原理是利用常温空气本身具有的冷却能力(冷能)、特别当与水面接触时以吸纳水蒸汽的方式带走水的潜热,实现无温差甚至负温差(空气温度高于水温)传热,过程推动力来自水面上的饱和蒸汽压ps与空气流中水蒸汽分压pw之差(ps-pw),其物理本质是该推动力使水蒸汽分子源源不断从气-水界面向气流主体迁移并随气流而去,由此促使界面上水分子不断吸热汽化而产生降温效应。据此原理,充分利用常温空气冷能的措施,首先该空气(以下称工作空气)总体水蒸汽分压pw要低,同时气-水界面饱和蒸汽压ps要高,以获得所需的过程推动力(ps-pw);推动力一定的条件下,强化过程的措施是提高气-水直接接触比表面积a和传质系数kp,以提高汽化强度mw=akp•(ps-pw)。为此,本发明提出了综合利用常温空气冷能的流态化方法,使该汽化传质过程在流态化气-固颗粒表面进行、其比表面积a和传质系数kp均比常用的填料高一个数量级以上;同时(针对应用场合)利用废热传递使该常温空气流态化体系吸热升温提高界面饱和蒸汽压ps从而提高过程推动力(ps-pw),多方面强化常温空气冷能的应用效果,使按设备表面积计算的制冷强度比上述IEC技术提高数倍。并且,由于吸热汽化传质过程主要发生在流态化运动颗粒表面,不仅克服了布水不均问题、还使设备表面免受污垢影响、提高了装备运行可靠性。该方法应用场合广泛,如92~95℃太阳能热水辅助制冷空调,在湿热地区夏季环境空气干球温度38℃条件下,实现26℃、相对湿度60%以下的全新风空调制冷,综合能效系数(折算为冷能/电能)超过3.1;应用于替代空冷技术,利用60℃废热进行废水汽化再生,在不增加工厂综合能耗前提下实现水资源循环利用。The principle of the above air conditioning energy-saving measures is to utilize the cooling capacity (cold energy) of normal temperature air itself, especially when it contacts the water surface, it absorbs water vapor to take away the latent heat of water, so as to achieve heat transfer without temperature difference or even negative temperature difference (air temperature is higher than water temperature). The driving force of the process comes from the difference between the saturated vapor pressure ps on the water surface and the water vapor partial pressure pw in the air flow ( ps - pw ). Its physical essence is that this driving force causes water vapor molecules to migrate continuously from the air-water interface to the main body of the air flow and go with the air flow, thereby prompting the water molecules on the interface to continuously absorb heat and vaporize to produce a cooling effect. According to this principle, measures to fully utilize the cold energy of normal temperature air are, first, the overall water vapor partial pressure pw of the air (hereinafter referred to as working air) should be low, and the saturated vapor pressure ps of the air-water interface should be high, so as to obtain the required process driving force ( ps - pw ); under the condition of a certain driving force, the measures to strengthen the process are to increase the air-water direct contact specific surface area a and the mass transfer coefficient kp , so as to increase the vaporization intensity mw = akp • ( ps - pw ). To this end, the present invention proposes a fluidization method that comprehensively utilizes the cold energy of normal temperature air, so that the vaporization mass transfer process is carried out on the surface of fluidized gas-solid particles, and its specific surface area a and mass transfer coefficient kp are more than one order of magnitude higher than those of commonly used fillers; at the same time (for application occasions), waste heat transfer is used to make the normal temperature air fluidization system absorb heat and increase the interface saturated vapor pressure ps , thereby increasing the process driving force ( ps - pw ), and strengthening the application effect of normal temperature air cold energy in many aspects, so that the refrigeration intensity calculated by the surface area of the equipment is several times higher than the above-mentioned IEC technology. In addition, since the endothermic vaporization mass transfer process mainly occurs on the surface of fluidized moving particles, it not only overcomes the problem of uneven water distribution, but also protects the surface of the equipment from the influence of dirt, and improves the reliability of equipment operation. This method has a wide range of applications, such as 92~95℃ solar hot water assisted refrigeration and air conditioning. In hot and humid areas in summer, under the condition of an ambient air dry bulb temperature of 38℃, it can achieve fresh air air conditioning at 26℃ and a relative humidity of less than 60%, with an overall energy efficiency coefficient (converted to cooling energy/electric energy) exceeding 3.1. It can also be used to replace air cooling technology, using 60℃ waste heat to vaporize and regenerate wastewater, thereby achieving water resource recycling without increasing the overall energy consumption of the factory.

发明内容Summary of the invention

本发明公开一种综合利用常温空气冷能的流态化方法。本发明方法适用于全新风清洁制冷空调、汽轮机乏汽冷凝和废水再生循环利用等多种场合。如附图1所示全新风清洁制冷空调,以公共空间的空调排气为工作空气,对新风(洁净大气)进行降温除湿,为公共空间提供干球温度23~25℃、相对湿度50%~ 60%(湿含量11.5~12.5g/kg-DA,DA代表干空气、下同)全新风空调供风。首先把空调排气卫生消毒作为利用空气冷能的一种方式,如附图1所示,空调排气与卫生消毒水溶液喷雾混合、从排气增湿/新风降温换热器1的顶部管箱均匀分布流入各下降管内形成流速8~10m/s的气-雾两相流、从管壁吸热使气流中的雾滴汽化,新风在管外自上而下掠过翅片表面放热、降温。管内气-雾混合物流至底部管箱分离,排气降温到23~25℃、湿含量增加到18.5~19.2g/kg-DA,与之对应管外新风则被冷却到26~27℃。分离的雾滴凝聚通过底部管箱下方微型加压循环泵6送返顶部管箱、与新补入的卫生消毒水溶液汇合喷雾循环,循环溶液质量流量与空调排气质量流量之比为1:50~60,新补入的卫生消毒水溶液量等于排气增湿汽化量与底部管箱消毒液排污量之和(排污量为汽化量的50~60%)。The present invention discloses a fluidization method for comprehensively utilizing the cold energy of normal temperature air. The method of the present invention is applicable to various occasions such as fresh air clean refrigeration and air conditioning, turbine exhaust steam condensation and wastewater regeneration and recycling. As shown in FIG1, the fresh air clean refrigeration and air conditioning uses the air conditioning exhaust of the public space as the working air, cools and dehumidifies the fresh air (clean air), and provides the public space with a dry bulb temperature of 23~25℃ and a relative humidity of 50%~60% (moisture content 11.5~12.5g/kg-DA, DA represents dry air, the same below) fresh air air conditioning air supply. First, the sanitation and disinfection of the air conditioning exhaust is used as a way to utilize the cold energy of air. As shown in FIG1, the air conditioning exhaust is sprayed and mixed with the sanitary disinfection aqueous solution, and evenly distributed from the top pipe box of the exhaust humidification/fresh air cooling heat exchanger 1 into each downcomer to form a gas-fog two-phase flow with a flow rate of 8~10m/s, and the heat is absorbed from the pipe wall to vaporize the droplets in the air flow. The fresh air passes over the fin surface from top to bottom outside the pipe to release heat and cool down. The gas-mist mixture in the pipe flows to the bottom pipe box for separation, the exhaust temperature is reduced to 23~25℃, and the moisture content is increased to 18.5~19.2g/kg-DA, and the corresponding fresh air outside the pipe is cooled to 26~27℃. The separated droplets are condensed and sent back to the top pipe box through the micro-pressurized circulation pump 6 under the bottom pipe box, and merged with the newly added sanitary disinfection water solution for spray circulation. The ratio of the circulating solution mass flow rate to the air conditioning exhaust mass flow rate is 1:50~60, and the newly added sanitary disinfection water solution is equal to the sum of the exhaust humidification vaporization amount and the bottom pipe box disinfection liquid sewage discharge amount (the sewage discharge amount is 50~60% of the vaporization amount).

被冷却降温到26~27℃的新风继续通过降膜蒸发/新风降温脱湿器2的管外翅片表面放热降温脱湿,热量通过管壁传递给管内的纯水降膜蒸发,管外翅片表面新风降温脱湿放热与管内纯水降膜蒸发吸热的传热温差2~3℃、蒸发强度不低于4.5kg/h.m2。在脱湿器2底部,管外新风降温至17~18℃、湿含量下降至11.5~12.5g/kg-DA,通过送风机增压进入洁净空调新风输配总管。管内降膜蒸发产生温度不低于15℃、压力不低于1.74kPa(绝对压力,下同)的低压水蒸汽,在底部管箱与降膜液分离后,通过低压水蒸汽出口控制阀12被抽吸进入蒸汽喷射器3;降膜液通过降膜循环泵7加压返回2的顶部管箱循环,循环质量流量是降膜蒸发量的15~20倍。The fresh air cooled to 26~27℃ continues to release heat and cool down and dehumidify through the outer fin surface of the tube of the falling film evaporator/fresh air cooling and dehumidifier 2. The heat is transferred to the pure water falling film evaporation in the tube through the tube wall. The heat transfer temperature difference between the fresh air cooling and dehumidification heat release on the outer fin surface of the tube and the pure water falling film evaporation heat absorption in the tube is 2~3℃, and the evaporation intensity is not less than 4.5kg/ hm2 . At the bottom of the dehumidifier 2, the fresh air outside the tube is cooled to 17~18℃, and the moisture content is reduced to 11.5~12.5g/kg-DA, and it is pressurized by the blower and enters the fresh air distribution main pipe of the clean air conditioner. The falling film evaporation in the tube generates low-pressure water vapor with a temperature not lower than 15°C and a pressure not lower than 1.74 kPa (absolute pressure, the same below). After being separated from the falling film liquid in the bottom tube box, it is sucked into the steam ejector 3 through the low-pressure water vapor outlet control valve 12; the falling film liquid is pressurized by the falling film circulation pump 7 and returned to the top tube box 2 for circulation, and the circulation mass flow rate is 15 to 20 times the falling film evaporation amount.

水蒸汽喷射器3的工作蒸汽由多层盘管蒸发器4提供,工作蒸汽温度85~90℃、压力58~68kPa(绝对压力,下同),产生工作蒸汽的热能来自92~95℃的平板式太阳能热水器循环热水、在蒸发器4内水平布置的多层盘管4-2内从最上层往下层盘旋流动放热、流速2.0~2.5m/s、最下层盘管出口循环回水温度不低于86℃。蒸发器4内,纯水通过盘管表面布水器4-1均匀分布在最上两层盘管表面、一边吸热汽化一边滴落到错位布置的下一层盘管表面继续吸热汽化、未汽化的纯水落入底部液面,液面高度正好使最下两层盘管被完全浸没液面以下、使加入该处的补水被盘管加热升温到85℃以上再通过盘管蒸发器循环泵9加压输送到布水器4-1循环;通过循环泵9加压的布水量是蒸发器4产生工作蒸汽量的5~10倍。产生的工作蒸汽通过喷射器3加速为超音速气流、压力低于1.7kPa、抽吸降膜蒸发来的低压水蒸汽并与之混合为温度高于36℃、压力大于6kPa的混合蒸汽,送往流态化冷凝组合5进行冷凝。The working steam of the water vapor ejector 3 is provided by the multi-layer coil evaporator 4, the working steam temperature is 85~90℃, the pressure is 58~68kPa (absolute pressure, the same below), the heat energy for generating the working steam comes from the circulating hot water of the flat plate solar water heater at 92~95℃, the multi-layer coil 4-2 arranged horizontally in the evaporator 4 spirally flows from the top layer to the bottom layer to release heat, the flow rate is 2.0~2.5m/s, and the circulating return water temperature at the outlet of the bottom coil is not less than 86℃. In the evaporator 4, pure water is evenly distributed on the surface of the top two layers of coils through the coil surface water distributor 4-1, while absorbing heat and evaporating, it drips to the surface of the next layer of coils arranged in a staggered manner to continue absorbing heat and evaporating, and the unevaporated pure water falls into the bottom liquid surface, the liquid level is just high enough to completely immerse the bottom two layers of coils below the liquid surface, so that the makeup water added there is heated by the coils to above 85°C and then pressurized and transported to the water distributor 4-1 for circulation through the coil evaporator circulation pump 9; the amount of pressurized water distributed by the circulation pump 9 is 5 to 10 times the amount of working steam generated by the evaporator 4. The generated working steam is accelerated to a supersonic airflow with a pressure lower than 1.7 kPa through the ejector 3, and the low-pressure water vapor from the falling film evaporation is sucked and mixed with it to form a mixed steam with a temperature higher than 36°C and a pressure greater than 6 kPa, and then sent to the fluidized condensation assembly 5 for condensation.

流态化冷凝组合5包括浸没在气-固流化床颗粒层内的翅片管束5-2和流化床底部的气体分布板5-1;翅片管束的方位按一头高一头低布置、使其管轴线与水平夹角5°~8°,待冷凝的水蒸汽通过与翅片管束高端连接的分布器均匀分配流进各管内、形成管内倾斜的对流冷凝放热、热量通过管壁上的翅片传递给管外流态化颗粒层,管内流动的冷凝液及未冷凝的水蒸汽从管束低端管口流入与之连接的副冷凝器5-3的冷凝空间、且在布置于其中的冷却水管外(35℃以下)翅片上继续放热完全冷凝;副冷凝器5-3内聚集的冷凝水、通过回水泵8加压并按低压水蒸汽量与工作蒸汽量之比、通过低压回水控制阀10和盘管蒸发器回水控制阀11分别向降膜蒸发/新风降温脱湿器2的顶部和多层盘管蒸发器4的底部补水;冷凝空间内的不凝气则通过连接于该空间的不凝气抽排控制阀5-4定期抽除以保持冷凝空间不凝气分压与水蒸汽分压之比小于(0.5/1000)。通过低压回水控制阀10和低压水蒸汽出口控制阀12把完全密闭的纯水及水蒸汽循环空间分隔为低压区和变压工作区,停运期及启动期将阀10和阀12均关闭、启动期先使变压工作区所有装置(包括4,4-1,4-2,9,3,5,5-1,5-2,5-3,5-4和8)运行正常后,再同步开启阀10和阀12。The fluidized condensation assembly 5 includes a finned tube bundle 5-2 immersed in the gas-solid fluidized bed particle layer and a gas distribution plate 5-1 at the bottom of the fluidized bed; the orientation of the finned tube bundle is arranged with one end high and the other end low, so that the tube axis is at an angle of 5° to 8° with the horizontal, and the water vapor to be condensed is evenly distributed through a distributor connected to the high end of the finned tube bundle and flows into each tube, forming an inclined convection condensation heat release in the tube, and the heat is transferred to the fluidized particle layer outside the tube through the fins on the tube wall, and the condensate flowing in the tube and the uncondensed water vapor flow from the tube port at the low end of the tube bundle into the condensation space of the auxiliary condenser 5-3 connected thereto, and in the distribution The fins outside the cooling water pipe (below 35°C) placed therein continue to release heat and completely condense; the condensed water gathered in the auxiliary condenser 5-3 is pressurized by the return water pump 8 and replenished to the top of the falling film evaporator/fresh air cooling and dehumidifier 2 and the bottom of the multi-layer coil evaporator 4 through the low-pressure return water control valve 10 and the coil evaporator return water control valve 11 respectively according to the ratio of the low-pressure water vapor to the working steam; the non-condensable gas in the condensation space is regularly extracted through the non-condensable gas extraction control valve 5-4 connected to the space to keep the ratio of the non-condensable gas partial pressure to the water vapor partial pressure in the condensation space less than (0.5/1000). The completely enclosed pure water and water vapor circulation space is separated into a low-pressure area and a transformer working area by the low-pressure return water control valve 10 and the low-pressure water vapor outlet control valve 12. Valve 10 and valve 12 are closed during the shutdown period and startup period. During the startup period, all devices in the transformer working area (including 4, 4-1, 4-2, 9, 3, 5, 5-1, 5-2, 5-3, 5-4 and 8) are first made to operate normally, and then valve 10 and valve 12 are opened synchronously.

翅片管束外的流态化颗粒层吸热过程按以下方法实现:在图1所示矩形横截面的流态化床内、颗粒层由均匀堆积在翅片管束外的球型耐磨颗粒群构成,颗粒群粒径0.8~1.2mm、密度550~650kg/m3、初始流态化速度0.3~0.5m/s,颗粒层的堆积高度(即从气体分布板5-1算起、到静止状态颗粒层上表面的距离)0.3~0.5m;从排气增湿/新风降温换热器1来的23~25℃的空调排气(工作空气),以2~5倍初始流态化速度均匀穿过开孔孔径不超过0.6mm的气体分布板5-1、并使其上方的颗粒层充分流态化而成为流化床层、其上表面上升到静止颗粒层堆积高度2倍以上并将翅片管束完全淹没;翅片管束低端下方翅片最低点位置距离分布板上表面35~50mm,从翅片管束的高端侧将工作水(符合环境排放标准的废水或自来水)喷雾引入流化床层、工作水质量流量与工作空气质量流量之比不超过1/30;工作空气带动水雾与流态化颗粒群激烈翻腾混合并与管束外表面及翅片表面不断碰撞传热,从23~25℃开始边吸热边汽化边升温至与翅片管内放热介质温差不超过5℃,对翅片管束内流动的33~36℃水蒸汽形成高强度冷凝效果,按翅片管内表面积计算的冷凝强度不低于6.1kg/h.m2;工作空气在流化床层中吸热升温增湿至其饱和蒸汽压,离开床层上表面并继续在其上部自由空间流动0.2~0.3m、最后穿过流态化冷凝组合5顶部设置的孔径不超过0.2mm的筛网排放。The heat absorption process of the fluidized particle layer outside the finned tube bundle is realized in the following way: in the fluidized bed with a rectangular cross section as shown in FIG. 1 , the particle layer is composed of a spherical wear-resistant particle group uniformly piled outside the finned tube bundle, the particle group has a particle size of 0.8-1.2 mm, a density of 550-650 kg/m 3 , an initial fluidization velocity of 0.3-0.5 m/s, and a particle layer accumulation height (i.e., the distance from the gas distribution plate 5-1 to the upper surface of the static particle layer) of 0.3-0.5 m; the air-conditioned exhaust gas (working air) of 23-25° C. from the exhaust humidification/fresh air cooling heat exchanger 1 uniformly passes through the gas distribution plate 5-1 with an opening diameter of no more than 0.6 mm at 2-5 times the initial fluidization velocity, and the particle layer above it is fully fluidized to become a fluidized bed layer, the upper surface of which rises to more than twice the accumulation height of the static particle layer and completely submerges the finned tube bundle; the lowest point position of the fin below the lower end of the finned tube bundle is 100 m away from the gas distribution plate 5-1. The upper surface of the cloth plate is 35~50mm, and working water (wastewater or tap water that meets environmental emission standards) is sprayed into the fluidized bed from the high end side of the finned tube bundle, and the ratio of the working water mass flow rate to the working air mass flow rate does not exceed 1/30; the working air drives the water mist and the fluidized particle group to churn and mix violently, and continuously collide and transfer heat with the outer surface of the tube bundle and the fin surface, absorbing heat while vaporizing and heating from 23~25℃ to a temperature difference of no more than 5℃ with the heat release medium in the finned tube, forming a high-intensity condensation effect on the 33~36℃ water vapor flowing in the finned tube bundle, and the condensation intensity calculated based on the inner surface area of the finned tube is not less than 6.1kg/ hm2 ; the working air absorbs heat in the fluidized bed, heats up and humidifies to its saturated vapor pressure, leaves the upper surface of the bed and continues to flow 0.2~0.3m in the upper free space, and finally passes through the screen with an aperture of no more than 0.2mm set on the top of the fluidized condensation combination 5 for discharge.

上述空调排气流态化冷能利用辅助平板式太阳能集热清洁制冷全新风空调系统,完全避免了公共空间空调供风卫生风险问题,并且其综合制冷性能系数COP(制冷负荷/消耗的电能及太阳能折算当量电能总合)大于3.1,优于《GB50189-2015 公共建筑节能设计标准》蒸发冷却压缩式冷水(热泵)机组制冷性能系数规定值(表4.2.10)。The above-mentioned air conditioning exhaust fluidization cold energy utilization assisted by flat-plate solar thermal collection clean refrigeration fresh air air conditioning system completely avoids the hygienic risk problem of air supply in public spaces, and its comprehensive refrigeration performance coefficient COP (cooling load/total of consumed electricity and solar energy equivalent electricity) is greater than 3.1, which is better than the specified value of refrigeration performance coefficient of evaporative cooling compression chiller (heat pump) unit in "GB50189-2015 Public Building Energy Saving Design Standard" (Table 4.2.10).

如附图2所示利用流态化空冷实现乏汽冷凝和废水再生的方法:温度不超过45℃的低压饱和水蒸汽是汽轮机末级乏汽或废水汽化再生蒸汽任何一种,工作气是符合大气排放标准的废气或直接采用环境空气,工作水是符合环境排放标准的废水或再生水任何一种。低压水蒸汽通过入口控制阀12进入流态化冷凝组合5,通过与翅片管束高端连接的分布器均匀分配流入浸没于气-固流态化床中的翅片管束5-2各管内,形成管内倾斜的对流冷凝放热,热量通过管壁及翅片传递给管外充分流态化颗粒层,管内低压水蒸汽完全冷凝、冷凝水及不凝气从管束低端管口流入与之连接的端盖5-5,通过回水泵8将凝聚的冷凝水加压送出循环利用、不凝气则通过连接于该空间的不凝气抽排控制阀5-4定期抽除使其在冷凝空间所占分压比小于0.5/1000。As shown in Figure 2, a method for realizing exhaust steam condensation and wastewater regeneration by fluidized air cooling is used: the low-pressure saturated steam with a temperature not exceeding 45°C is either exhaust steam from the last stage of the steam turbine or wastewater vaporization regeneration steam; the working gas is exhaust gas that meets atmospheric emission standards or is directly ambient air; and the working water is either wastewater that meets environmental emission standards or regenerated water. Low-pressure water vapor enters the fluidized condensation combination 5 through the inlet control valve 12, and is evenly distributed through a distributor connected to the high end of the finned tube bundle to flow into each tube of the finned tube bundle 5-2 immersed in the gas-solid fluidized bed, forming inclined convection condensation heat release in the tube, and the heat is transferred to the fully fluidized particle layer outside the tube through the tube wall and the fins. The low-pressure water vapor in the tube is completely condensed, and the condensed water and non-condensable gas flow from the lower end of the tube bundle into the end cover 5-5 connected thereto. The condensed water is pressurized and sent out for recycling by the return pump 8, and the non-condensable gas is regularly extracted through the non-condensable gas extraction control valve 5-4 connected to the space so that its partial pressure ratio in the condensation space is less than 0.5/1000.

翅片管束外气-固流化床及其吸热按以下方法实现:-20~35℃的工作气,以颗粒(粒径0.8~1.2mm、密度550~650kg/m3、初始流态化速度0.3~0.5m/s )初始流态化速度2~5倍的流速均匀穿过孔径不超过0.6mm的气体分布板5-1,使其上堆积高度0.3~0.5m的耐磨颗粒群充分流态化形成的气-固流化床高度上升到颗粒堆积高度2倍以上并完全淹没翅片管束;翅片管束的布置方法与前述相同,从其高端侧将工作水喷雾引入流态化颗粒层,工作水的质量流量与工作气质量流量之比为1:20~50,工作气带动水雾与流态化颗粒群激烈翻腾混合并不断冲刷管束外表面及翅片表面,形成一边吸热一边汽化增湿的冷却效应强化翅片管内温度不超过45℃的水蒸汽冷凝、按翅片管内表面积计算的冷凝强度不低于15kg/h.m2;工作气通过流化床颗粒层吸热、升温至不超过42℃、增湿至不超过55g/kg-DA,流出床层后继续在其上部空间流动0.2~0.3m,最后穿过流态化冷凝组合5顶部设置的0.2mm以下孔径的筛网排放。The gas-solid fluidized bed outside the finned tube bundle and its heat absorption are realized by the following method: -20~35℃ working gas, with particles (particle size 0.8~1.2mm, density 550~650kg/ m3 , initial fluidization velocity 0.3~0.5m/s ) A flow rate of 2 to 5 times the initial fluidization speed uniformly passes through the gas distribution plate 5-1 with a hole diameter not exceeding 0.6 mm, so that the wear-resistant particle group with a stacking height of 0.3 to 0.5 m thereon is fully fluidized to form a gas-solid fluidized bed with a height rising to more than 2 times the particle stacking height and completely submerging the fin tube bundle; The arrangement method of the fin tube bundle is the same as the above, and the working water spray is introduced into the fluidized particle layer from its high end side. The ratio of the mass flow rate of the working water to the mass flow rate of the working gas is 1:20 to 50. The working gas drives the water mist and the fluidized particle group to violently churn and mix and continuously flush the outer surface of the tube bundle and the fin surface, forming a cooling effect of absorbing heat while vaporizing and humidifying, strengthening the condensation of water vapor with a temperature not exceeding 45°C in the fin tube, and the condensation intensity calculated based on the inner surface area of the fin tube is not less than 15kg/ hm2 The working gas absorbs heat through the fluidized bed particle layer, rises in temperature to no more than 42°C, and increases in humidity to no more than 55g/kg-DA. After flowing out of the bed, it continues to flow in the upper space for 0.2~0.3m, and finally passes through the screen with a pore size of less than 0.2mm set on the top of the fluidized condensation combination 5 for discharge.

附图说明BRIEF DESCRIPTION OF THE DRAWINGS

附图1是本发明提供的综合利用常温空气冷能流态化制冷全新风清洁空调方法、附图2是利用流态化空冷实现乏汽冷凝和废水再生方法示意图。1 is a diagram of a method for clean air conditioning by fluidized cooling using cold energy of normal temperature air provided by the present invention, and 2 is a schematic diagram of a method for realizing exhaust steam condensation and wastewater regeneration using fluidized air cooling.

附图1和附图2中:1–排气增湿/新风降温换热器;2–降膜蒸发/新风降温脱湿器;3–水蒸汽喷射器;4–多层盘管蒸发器;4-1–盘管表面布水器;4-2–多层盘管;5–流态化冷凝组合;5-1–气体分布板; 5-2–翅片管束; 5-3–副冷凝器; 5-4–抽排不凝气控制阀;5-5–端盖;6–微型加压循环泵;7–降膜液循环泵;8–冷凝水回水泵;9 –盘管蒸发器循环泵;10 –低压回水控制阀;11–盘管蒸发器回水控制阀;12–低压水蒸汽出/入口控制阀。In Figures 1 and 2: 1 – exhaust humidification/fresh air cooling heat exchanger; 2 – falling film evaporation/fresh air cooling dehumidifier; 3 – water vapor ejector; 4 – multi-layer coil evaporator; 4-1 – coil surface water distributor; 4-2 – multi-layer coil; 5 – fluidized condensation combination; 5-1 – gas distribution plate; 5-2 – fin tube bundle; 5-3 – auxiliary condenser; 5-4 – non-condensable gas extraction control valve; 5-5 – end cover; 6 – micro pressurized circulation pump; 7 – falling film liquid circulation pump; 8 – condensate return pump; 9 – coil evaporator circulation pump; 10 – low-pressure return control valve; 11 – coil evaporator return control valve; 12 – low-pressure water vapor inlet/outlet control valve.

以下结合实施例对附图1和附图2作进一步阐述。The following further describes the accompanying drawings 1 and 2 in conjunction with the embodiments.

具体实施方式Detailed ways

以下结合但不限于实施例阐述本发明具体实施方式The following is a description of the specific implementation of the present invention in combination with but not limited to the embodiments.

实施例1:公共空间10000m3/h全新风空调,流态化利用空调排气冷能制冷。Example 1: 10000m 3 /h fresh air air conditioning in public space, using fluidized cooling to utilize the cold energy of air conditioning exhaust gas.

环境空气条件:干球温度38℃、湿含量21.2g/kg-DA。全新风空调制冷供风条件:干球温度23~25℃、湿含量11.5~12.5g/kg-DA(相对湿度50%~ 60%)。同时要求对该公共空间空调排气(干球温度 26℃、湿含量12.5g/kg-DA)进行充分的卫生消毒后集中排放。以该公共空间楼顶平板式太阳能热水器将60m3/h 循环热水从88℃加热至93℃作为低位热制冷热源。Ambient air conditions: dry bulb temperature 38℃, moisture content 21.2g/kg-DA. Fresh air conditioning cooling air supply conditions: dry bulb temperature 23~25℃, moisture content 11.5~12.5g/kg-DA (relative humidity 50%~60%). At the same time, it is required that the air conditioning exhaust of the public space (dry bulb temperature 26℃, moisture content 12.5g/kg-DA) be fully disinfected and then discharged centrally. The flat-plate solar water heater on the roof of the public space heats 60m3 /h of circulating hot water from 88℃ to 93℃ as a low-level heat cooling heat source.

如附图1所示,用9.0kW功率排气风机将26℃空调排气9000m3/h加压到2.0~2.5kPa进入排气增湿/新风降温换热器1的顶部管箱,与230kg/h卫生消毒水溶液喷雾混合而成气-雾两相流,以10m/s的流速均匀分布流入各管内,排气自身降温放热以及从管壁吸热使雾滴汽化,流至底部出管口温度24℃、增湿至17.8g/kg-DA;对应使管外自上而下掠过翅片表面的10000m3/h新风放热降温到出口温度28℃、湿含量不变。气-雾流在底部管箱分离,未汽化的雾滴凝聚后133kg/h通过微型加压泵6循环送返顶部管箱并与该处新补入的97kg/h卫生消毒水溶液汇合进入喷雾循环、35kg/h从底部管箱排污。As shown in Figure 1, a 9.0kW exhaust fan is used to pressurize 9000m3 /h of 26℃ air-conditioned exhaust to 2.0~2.5kPa and enter the top pipe box of the exhaust humidification/fresh air cooling heat exchanger 1, and is sprayed with 230kg/h of sanitary disinfection aqueous solution to form a gas-mist two-phase flow, which flows into each pipe at a flow rate of 10m/s. The exhaust itself cools down and releases heat, and absorbs heat from the pipe wall to vaporize the droplets, and flows to the bottom outlet with a temperature of 24℃ and humidification to 17.8g/kg-DA; correspondingly, the 10000m3 /h fresh air passing over the fin surface from top to bottom outside the pipe releases heat and cools to an outlet temperature of 28℃, with unchanged moisture content. The gas-mist flow is separated in the bottom pipe box, and the unvaporized droplets are condensed and 133kg/h is circulated back to the top pipe box through the micro-boosting pump 6 and merged with the newly added 97kg/h sanitary disinfection aqueous solution to enter the spray cycle, and 35kg/h is discharged from the bottom pipe box.

被上述过程冷却降温到28℃的新风继续自上而下通过降膜蒸发/新风降温脱湿器2的管外翅片表面放热降温脱湿,至出口处降温降湿至18℃、12.5g/kg-DA以下向公共空间输送,允许输配风过程冷量损失温升4~5℃,用户得到洁净新风满足舒适空调供风条件。The fresh air cooled to 28°C by the above process continues to release heat, cool and dehumidify from top to bottom through the outer fin surface of the falling film evaporator/fresh air cooling and dehumidifier 2, and is cooled and humidified to 18°C and below 12.5g/kg-DA at the outlet and transported to the public space. The temperature rise of 4~5°C due to the loss of cooling capacity in the air distribution process is allowed, and users get clean fresh air that meets the comfortable air conditioning supply conditions.

新风在降温脱湿器2释放的显热与潜热通过翅片管外表面传递给管内温度不低于15℃的纯水降膜蒸发过程,蒸发强度不低于5.0kg/h.m2,产生压力不低于1.7kPa的低压蒸汽175 kg/h,通过低压水蒸汽出口控制阀12被抽吸进入蒸汽喷射器3;降膜循环泵7从2的底部管箱输送2500~3000 kg/h纯水返回2的顶部管箱循环。The sensible heat and latent heat released by the fresh air in the cooling and dehumidifying device 2 are transferred to the pure water falling film evaporation process with a temperature of not less than 15°C in the tube through the outer surface of the finned tube. The evaporation intensity is not less than 5.0kg/ hm2 , and the low-pressure steam of 175 kg/h with a pressure of not less than 1.7kPa is generated, which is sucked into the steam ejector 3 through the low-pressure water vapor outlet control valve 12; the falling film circulation pump 7 transports 2500~3000 kg/h of pure water from the bottom pipe box of 2 back to the top pipe box of 2 for circulation.

上述低压蒸汽被480 kg/h温度不低于87℃、压力不低于62kPa的工作蒸汽喷射抽吸进入蒸汽喷射器3,二者混合成37℃的饱和水蒸汽655kg/h送往流态化冷凝组合5进行冷凝。工作蒸汽的产生过程是:由平板式太阳能集热器加热到93℃的循环热水60m3/h,以2.2m/s的流速自上而下通过多层盘管4-2管内对流放热、使通过盘管表面布水器4-1均匀分布在盘管表面的2800 kg/h纯水部分汽化产生480 kg/h工作蒸汽、未汽化的纯水滴落于4-2最下两层盘管外的液相中、与通过回水泵8送来的37℃冷凝水480 kg/h汇合并被加热至87℃以上再通过盘管蒸发器循环泵9加压送往位于顶部盘管以上的盘管表面布水器4-1循环;盘管内热水循环流动放热至最下层盘管出口回水温度下降到88℃,送往平板式太阳能热水器复热至93℃返回4-2循环热水入口。The above low-pressure steam is jet-drawn into the steam ejector 3 by 480 kg/h of working steam with a temperature not lower than 87°C and a pressure not lower than 62 kPa, and the two are mixed into 655 kg/h of saturated water vapor at 37°C and sent to the fluidized condensation assembly 5 for condensation. The process of generating working steam is as follows: 60m3 /h of circulating hot water heated to 93℃ by the flat plate solar collector releases heat by convection from top to bottom through the multi-layer coil 4-2 at a flow rate of 2.2m/s, so that 2800kg/h of pure water evenly distributed on the coil surface through the coil surface distributor 4-1 is partially vaporized to generate 480kg/h of working steam, and the unvaporized pure water drops into the liquid phase outside the two lowest layers of coils of 4-2, merges with 480kg/h of 37℃ condensed water sent by the return pump 8, is heated to above 87℃, and then is pressurized by the coil evaporator circulation pump 9 and sent to the coil surface distributor 4-1 located above the top coil for circulation; the hot water in the coil circulates and releases heat until the return water temperature at the outlet of the lowest coil drops to 88℃, and is sent to the flat plate solar water heater for reheating to 93℃ and returns to the circulating hot water inlet of 4-2.

从水蒸汽喷射器3送往流态化冷凝组合5的37℃饱和水蒸汽冷凝过程是:水蒸汽通过翅片管束5-2高端的分布器均匀分配流进各管内、形成管内倾斜的对流冷凝放热、冷凝液及未冷凝的水蒸汽从管束5-2低端管口流入与之连接的副冷凝器5-3完全冷凝汇聚成655kg/h纯水,由回水泵8加压,通过低压回水控制阀10向降膜蒸发/新风降温脱湿器2分送175 kg/h、通过盘管蒸发器回水控制阀11向多层盘管蒸发器4底部补水480 kg/h。副冷凝器5-3的冷凝热由60 m3/h冷却水(29℃进、34℃出)通过翅片管内对流吸热带走、不凝气通过不凝气抽排控制阀5-4定期抽除,以保持冷凝空间不凝气分压与水蒸汽分压之比小于(0.5/1000)。The condensation process of 37℃ saturated water vapor sent from the water vapor ejector 3 to the fluidized condensation combination 5 is as follows: the water vapor is evenly distributed into each tube through the distributor at the high end of the finned tube bundle 5-2, forming inclined convection condensation heat release in the tube, and the condensate and uncondensed water vapor flow from the low end pipe port of the tube bundle 5-2 into the auxiliary condenser 5-3 connected thereto, and are completely condensed and gathered into 655kg/h of pure water, which is pressurized by the return water pump 8, and 175 kg/h is distributed to the falling film evaporator/fresh air cooling and dehumidifier 2 through the low-pressure return water control valve 10, and 480 kg/h of water is replenished to the bottom of the multi-layer coil evaporator 4 through the coil evaporator return water control valve 11. The condensation heat of the auxiliary condenser 5-3 is taken away by 60 m3 /h cooling water (29℃ inlet, 34℃ outlet) through convection absorption in the finned tubes, and the non-condensable gas is regularly extracted through the non-condensable gas extraction control valve 5-4 to keep the ratio of the non-condensable gas partial pressure to the water vapor partial pressure in the condensation space less than (0.5/1000).

流态化冷凝组合5的翅片管束5-2外流态化颗粒层吸收冷凝热的过程与方法是:颗粒群是从粉煤灰中筛选的空心陶瓷微珠、粒径1.1~1.2mm、密度600kg/m3、初始流态化速度0.42m/s,颗粒层堆积高度0.35m;经换热器1降温增湿后的24℃空调排气,以1.6 m/s的速度均匀穿过孔径0.5mm的气体分布板5-1使颗粒层充分流态化、高度上升至0.8m使翅片管束完全淹没;从翅片管束5-2的高端侧将130 kg/h自来水喷雾引入流态化颗粒层、与流态化颗粒群激烈翻腾混合、碰撞管束外表面及翅片表面、边汽化边吸热、使翅片管束内流动的37℃低压水蒸汽冷凝强度不低于10kg/h.m2,空调排气通过流态化颗粒层吸热升温至31℃、增湿至29g/kg-DA,从颗粒层上方0.2m处穿过孔径0.2mm的筛网排放。The process and method of the fluidized particle layer outside the finned tube bundle 5-2 of the fluidized condensation combination 5 to absorb condensation heat are as follows: the particle group is hollow ceramic microspheres selected from fly ash, with a particle size of 1.1-1.2 mm, a density of 600 kg/m 3 , an initial fluidization speed of 0.42 m/s, and a particle layer stacking height of 0.35 m; the 24°C air-conditioned exhaust gas after cooling and humidification by the heat exchanger 1 evenly passes through the gas distribution plate 5-1 with a hole diameter of 0.5 mm at a speed of 1.6 m/s to fully fluidize the particle layer, and the height rises to 0.8 m to completely submerge the finned tube bundle; 130 kg/h of tap water spray is introduced into the fluidized particle layer from the high end side of the finned tube bundle 5-2, and violently churns and mixes with the fluidized particle group, collides with the outer surface of the tube bundle and the fin surface, and absorbs heat while vaporizing, so that the condensation intensity of the 37°C low-pressure water vapor flowing in the finned tube bundle is not less than 10 kg/hm 2 The air-conditioning exhaust absorbs heat through the fluidized particle layer and rises in temperature to 31°C and humidifies to 29g/kg-DA, and is discharged from a screen with a pore size of 0.2mm at 0.2m above the particle layer.

本例流态化利用9000m3/h空调排气冷却、辅助平板式太阳能集热器供热、水蒸汽喷射制冷10000m3/h全新风清洁空调的有益效果是,仅以空气和水为工质的太阳能制冷空调、完全避免了公共空间空调供风卫生风险,制冷负荷160kW,耗电功率15.2kW、平板太阳能集热器折算当量电功率34.8kW,综合制冷性能系数COP=160/(15.2+34.8)=3.2,具有优良的低碳供冷特性。The beneficial effect of fluidized utilization of 9000m3 /h air conditioning exhaust cooling, auxiliary flat-plate solar collector heating, and water vapor jet cooling of 10000m3 /h fresh air clean air conditioning in this case is that the solar refrigeration air conditioning with only air and water as working fluids completely avoids the hygienic risks of air supply in public spaces. The cooling load is 160kW, the power consumption is 15.2kW, the flat-plate solar collector is converted to an equivalent electric power of 34.8kW, and the comprehensive refrigeration performance coefficient COP=160/(15.2+34.8)=3.2, which has excellent low-carbon cooling characteristics.

实施例2:流态化利用车间通风排气冷能和60℃工艺废热,对40℃工艺废水进行再生处理。Example 2: Fluidized bed utilizes workshop ventilation exhaust cooling energy and 60°C process waste heat to regenerate 40°C process wastewater.

工艺废水1100kg/h,水质符合环境排放标准。车间卫生通风排气10000m3/h,20℃,湿含量8.5g/kg-DA。60℃工艺废热来自化工车间蒸发浓缩废蒸汽与水喷射冷凝器入口连接总管,废蒸汽饱和温度60℃。Process wastewater is 1100kg/h, and the water quality meets environmental emission standards. Workshop sanitary ventilation exhaust is 10000m3 /h, 20℃, and the moisture content is 8.5g/kg-DA. The 60℃ process waste heat comes from the main pipe connecting the evaporation and concentration waste steam of the chemical workshop and the inlet of the water jet condenser, and the saturated temperature of the waste steam is 60℃.

从上述蒸发浓缩废蒸汽总管分流60℃饱和蒸汽650kg/h,以此为热源使工艺废水加热汽化、产生45℃再生蒸汽620 kg/h,通过附图2所示低压水蒸汽入口控制阀导入流态化冷凝组合5,经翅片管束高端连接的分布器均匀分配流入浸没于气-固流态化颗粒层的翅片管束5-2倾斜管内对流冷凝放热,热量通过管壁上的翅片传递给管外流态化颗粒层,管内低压水蒸汽完全冷凝,冷凝水及不凝气从管束低端管口流入与之连接的端盖5-5,通过回水泵8加压送出620 kg/h再生冷凝水供工艺循环使用,不凝气通过连接于该空间的不凝气抽排控制阀5-4定期抽除。管外流态化颗粒层吸热过程按以下方法实现:气体分布板5-1上方颗粒层堆积从粉煤灰中筛选的空心陶瓷微珠,粒径1.1~1.2mm、密度600kg/m3、初始流态化速度0.42m/s,颗粒层堆积高度0.35m;20℃的车间卫生通风排气10000m3/h通过风机加压到1.5kPa作为工作空气,以1.6 m/s的速度均匀穿过孔径0.5mm的气体分布板5-1,使颗粒层充分流态化、其上表面高度上升到0.8m使翅片管束被完全淹没;从翅片管束5-2的高端侧将工艺废水480 kg/h喷雾引入流态化颗粒层,工作空气带动水雾与流态化颗粒群激烈翻腾混合并与管束外表面及翅片表面不断接触与更新、从20℃开始边吸热边汽化边升温、对翅片管束内流动的45℃再生水蒸汽形成不低于16kg/h.m2的冷凝效果,工作气吸热升温至40℃、增湿至45.7g/kg-DA,离开流态化颗粒层上表面并继续在其上部空间流动0.2m后穿过孔径0.2mm的筛网排放。650 kg/h of 60°C saturated steam is diverted from the above-mentioned evaporation and concentration waste steam main pipe, and used as a heat source to heat and vaporize the process wastewater to generate 620 kg/h of 45°C regeneration steam, which is introduced into the fluidized condensation combination 5 through the low-pressure steam inlet control valve shown in Figure 2, and evenly distributed through the distributor connected to the high end of the finned tube bundle to flow into the inclined tube of the finned tube bundle 5-2 immersed in the gas-solid fluidized particle layer for convection condensation and heat release. The heat is transferred to the fluidized particle layer outside the tube through the fins on the tube wall, and the low-pressure water vapor in the tube is completely condensed. The condensed water and non-condensable gas flow from the lower end of the tube bundle into the end cover 5-5 connected thereto, and 620 kg/h of regeneration condensed water is pressurized and delivered by the return pump 8 for process circulation. The non-condensable gas is regularly extracted through the non-condensable gas extraction control valve 5-4 connected to the space. The heat absorption process of the fluidized particle layer outside the tube is realized by the following method: the particle layer above the gas distribution plate 5-1 is piled with hollow ceramic micro beads selected from fly ash, with a particle size of 1.1~1.2mm, a density of 600kg/ m3 , an initial fluidization speed of 0.42m/s, and a particle layer accumulation height of 0.35m; 10000m3 /h of workshop sanitary ventilation exhaust gas at 20℃ is pressurized to 1.5kPa by a fan as working air, and passes through the gas distribution plate 5-1 with a hole diameter of 0.5mm at a speed of 1.6m/s, so that the particle layer is fully fluidized and its upper surface height rises to 0.8m, so that the finned tube bundle is completely submerged; 480 process wastewater is discharged from the high end side of the finned tube bundle 5-2 to form a heat exchanger, and the heat exchanger is heated to 1.5kPa. kg/h spray is introduced into the fluidized particle layer, and the working air drives the water mist and the fluidized particle group to churn and mix violently, and continuously contact and renew with the outer surface of the tube bundle and the fin surface, absorbing heat while vaporizing and heating from 20℃, and forming a condensation effect of not less than 16kg/ hm2 on the 45℃ regenerated water vapor flowing in the fin tube bundle. The working gas absorbs heat and heats up to 40℃, humidifies to 45.7g/kg-DA, leaves the upper surface of the fluidized particle layer and continues to flow in the upper space for 0.2m before passing through a 0.2mm pore screen for discharge.

本例的节能减排效果是,流态化利用10000m3/h卫生通风排气冷能实现了1100kg/h废水再生处理(其中得到620kg/h再生冷凝水、大气消纳480 kg/h),该过程卫生通风排气加压风机耗电6.5kW.h及小型离心水泵等耗电不超过3.5kW.h、而水喷射冷凝器减少650kg/h废蒸汽冷凝负荷可节约电耗15kW.h(包括水泵电耗11kW.h及凉水塔风机电耗4kW.h),可见本例流态化利用车间通风排气冷能和60℃工艺废热实现废水资源化再生的同时、还可节约车间综合能耗。The energy-saving and emission-reduction effect of this example is that the fluidized bed utilizes 10,000 m 3 /h of sanitary ventilation exhaust cooling energy to achieve 1,100 kg/h of wastewater regeneration treatment (of which 620 kg/h of regenerated condensed water is obtained and 480 kg/h is absorbed by the atmosphere). In this process, the sanitary ventilation exhaust booster fan consumes 6.5 kW.h of electricity and the small centrifugal water pump consumes no more than 3.5 kW.h of electricity. The water jet condenser reduces the waste steam condensation load by 650 kg/h, which can save 15 kW.h of electricity (including 11 kW.h of water pump power consumption and 4 kW.h of cooling tower fan power consumption). It can be seen that the fluidized bed in this example utilizes the workshop ventilation exhaust cooling energy and 60°C process waste heat to achieve wastewater resource regeneration and save the overall energy consumption of the workshop.

本发明不限于上述实施例,其技术方案已在发明内容部分予以说明。The present invention is not limited to the above embodiments, and its technical solutions have been described in the content of the invention.

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.
CN202211322685.2A 2022-10-27 2022-10-27 Clean air conditioner utilizing normal temperature air cold energy in fluidization mode and exhaust steam condensation method Pending CN117989627A (en)

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