吸收式除湿工艺研究
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摘要
溶液吸收式除湿系统,可以利用50℃～80℃的低品位热源作为再生能源,所用除湿剂对环境友好,同时能除去空气中的尘埃、细菌、霉菌及其他有害物,提高空气品质。从保护环境、节约能源等方面来看是一种很有竞争力的除湿技术。
本文针对LiCl溶液吸收式除湿工艺系统的关键过程——溶液吸收除湿与溶液解吸再生以及系统整体,开展了实验研究、模拟分析与系统工艺设计工作。
利用流程模拟软件ASPEN PLUS,选择NRTL电解质溶液活度系数模型,并选择CaCl_2溶液作为除湿剂,吸收器和再生器分别选用RadRrac和Flash2模块,建立了溶液吸收式除湿循环的系统模拟。根据灵敏度分析,其空气除湿性能系数可达0.7以上,优于现有LiCl溶液除湿装置的0.65的水平,并表明提浓稀溶液的有效性,据此确定了实验设计参考的循环操作条件。
进一步,分析比较了逆流绝热填料塔与内冷型除湿塔的优缺点,选择比表面积大、结构紧凑、空气处理能力大的填料塔作为吸收器。本研究填料塔塔体采用有机玻璃板,塔高1.2m,填料层高度为60cm,规格为20×20×20cm~3立方型不锈钢孔板波纹的规整填料。同时,提出了结构简单、空气压降小、动力部件少的雾化闪蒸喷淋再生器新型结构。本研究再生塔塔体采用有机玻璃,塔高1.0m,喷嘴采用实心锥形喷头,有效喷淋高度为40cm。
进行了逆流绝热吸收实验和模拟分析。考察了内部因素(液气比、溶液浓度与溶液温度)和外部因素(空气入口温度、湿度)对除湿量的影响规律。实验数据表明,在上述实验条件下,吸收器最大除湿量达到0.443g·s~(-1),平均除湿量达到0.368g·s~(-1),证明了本装置有很好的除湿效果。改变吸收器内部因素对除湿效果有较大的影响,如溶液质量浓度由0.322增加到0.363,空气出口含湿量相应地由13.9g·kg~(-1)降到12.2g·kg~(-1),下降幅度比较明显;而外部因素的改变对除湿效果影响较弱,如当空气温度由33.5℃降到26.4℃时,空气出口含湿量仅由10.9g·kg~(-1)下降到10.5g·kg~(-1)。根据实验结果,将除湿器的除湿量与除湿器入口各参数进行拟和,得到如下关联式:m=3697h~(2.022)t_a~(-0.498)G~(0.666)x_i~(3.471)t_1~(-2.223)L~(0.114)其中:m为除湿量,kg·s~(-1)。
建立了除湿过程的传热传质模型。模型计算值与实验结果趋势一致。分析了除湿器的出口空气含湿量、空气温度、溶液浓度、溶液温度参数随塔高的变化关系。从模型分析得出低温高浓的入口溶液对吸收除湿过程有强化作用,而空气入口温度的变化对吸收除湿过程影响较弱。本实验装置的最佳液气比约为3.0。
进行了雾化喷淋再生实验和模拟分析。基于喷淋量21.61·h~(-1),再生器入口空气温度为28℃,相对湿度为45%的实验条件,选择溶液入口温度和再生风机电压分别为80℃/100V、90℃/100V、80℃/100V的三组因素,测得溶液浓度变化率分别为0.82%、1.33%、1.23%。实验结果表明雾化喷淋再生与采用填料塔和管式降膜塔的再生效果相同。建立了雾化喷淋再生过程的数学模型,分析了再生器的出口空气含湿量、空气温度、溶液浓度、溶液温度参数随塔高的变化关系。从模型分析得出高温入口溶液对雾化喷淋再生过程有强化作用,而空气入口温度的变化对雾化喷淋再生过程影响较弱。
Solution absorption dehumidification system, which use the low-temperature heat sources between 50°C to 80°C such as solar energy、industrial waste heat to regenerate, can remove the dust in the air、bacteria、fungi and other harmful substances, improve the air quality. From the protection of the environment and energy, it is a competitive dehumidifying technology.
This paper points to the key process of solution absorption dehumidification system, the absorption、the regeneration and the whole process, does the experimental research、simulation analysis and process design. ASPEN PLUS was used to simulate the system, and according to the simulate result, pulverization spray regenerator was effective for concentrating the solution. Further, choose the packed tower as the absorber based on the analysis and comparison between the packed tower and the cooled tower.
As for the absorber, the internal factors (liquid gas ratio, the concentration and temperature of the solution) and external factors (the temperature of air, humidity) on the humidity of outlet air was inspected. Experimental data showed that the device had very good performance. The changes of internal factors have greater effect on the desiccant compare to the external factors. The mathematic model of the packed tower was established, and the simulation accorded with the experimental data. The model was used to analysis the outlet parameters of the air humidity, air temperature, solution concentration and temperature varieties alongside the tower. Low temperature and high concentration of the inlet solution can strengthen the dehumidification, while for the experimental device, the best mass flow of solution to air ratio is about 3.0.
As for the regeneration experiment with the pulverization spray regenerator, tested the regeneration capacity on different inlet solution temperature and air flow. Experimental data show that use the simple structure, low pressure drop pulverization spray regenerator to renew the dilute solution is totally feasible. The model of the regenerator was built to analysis the distribution of the outlet solution concentration and temperature. High inlet solution temperature can strengthen the regeneration, which was consistent to experimental data, while the inlet air temperature and humidity effects weakly.
本文针对LiCl溶液吸收式除湿工艺系统的关键过程——溶液吸收除湿与溶液解吸再生以及系统整体,开展了实验研究、模拟分析与系统工艺设计工作。
利用流程模拟软件ASPEN PLUS,选择NRTL电解质溶液活度系数模型,并选择CaCl_2溶液作为除湿剂,吸收器和再生器分别选用RadRrac和Flash2模块,建立了溶液吸收式除湿循环的系统模拟。根据灵敏度分析,其空气除湿性能系数可达0.7以上,优于现有LiCl溶液除湿装置的0.65的水平,并表明提浓稀溶液的有效性,据此确定了实验设计参考的循环操作条件。
进一步,分析比较了逆流绝热填料塔与内冷型除湿塔的优缺点,选择比表面积大、结构紧凑、空气处理能力大的填料塔作为吸收器。本研究填料塔塔体采用有机玻璃板,塔高1.2m,填料层高度为60cm,规格为20×20×20cm~3立方型不锈钢孔板波纹的规整填料。同时,提出了结构简单、空气压降小、动力部件少的雾化闪蒸喷淋再生器新型结构。本研究再生塔塔体采用有机玻璃,塔高1.0m,喷嘴采用实心锥形喷头,有效喷淋高度为40cm。
进行了逆流绝热吸收实验和模拟分析。考察了内部因素(液气比、溶液浓度与溶液温度)和外部因素(空气入口温度、湿度)对除湿量的影响规律。实验数据表明,在上述实验条件下,吸收器最大除湿量达到0.443g·s~(-1),平均除湿量达到0.368g·s~(-1),证明了本装置有很好的除湿效果。改变吸收器内部因素对除湿效果有较大的影响,如溶液质量浓度由0.322增加到0.363,空气出口含湿量相应地由13.9g·kg~(-1)降到12.2g·kg~(-1),下降幅度比较明显;而外部因素的改变对除湿效果影响较弱,如当空气温度由33.5℃降到26.4℃时,空气出口含湿量仅由10.9g·kg~(-1)下降到10.5g·kg~(-1)。根据实验结果,将除湿器的除湿量与除湿器入口各参数进行拟和,得到如下关联式:m=3697h~(2.022)t_a~(-0.498)G~(0.666)x_i~(3.471)t_1~(-2.223)L~(0.114)其中:m为除湿量,kg·s~(-1)。
建立了除湿过程的传热传质模型。模型计算值与实验结果趋势一致。分析了除湿器的出口空气含湿量、空气温度、溶液浓度、溶液温度参数随塔高的变化关系。从模型分析得出低温高浓的入口溶液对吸收除湿过程有强化作用,而空气入口温度的变化对吸收除湿过程影响较弱。本实验装置的最佳液气比约为3.0。
进行了雾化喷淋再生实验和模拟分析。基于喷淋量21.61·h~(-1),再生器入口空气温度为28℃,相对湿度为45%的实验条件,选择溶液入口温度和再生风机电压分别为80℃/100V、90℃/100V、80℃/100V的三组因素,测得溶液浓度变化率分别为0.82%、1.33%、1.23%。实验结果表明雾化喷淋再生与采用填料塔和管式降膜塔的再生效果相同。建立了雾化喷淋再生过程的数学模型,分析了再生器的出口空气含湿量、空气温度、溶液浓度、溶液温度参数随塔高的变化关系。从模型分析得出高温入口溶液对雾化喷淋再生过程有强化作用,而空气入口温度的变化对雾化喷淋再生过程影响较弱。
Solution absorption dehumidification system, which use the low-temperature heat sources between 50°C to 80°C such as solar energy、industrial waste heat to regenerate, can remove the dust in the air、bacteria、fungi and other harmful substances, improve the air quality. From the protection of the environment and energy, it is a competitive dehumidifying technology.
This paper points to the key process of solution absorption dehumidification system, the absorption、the regeneration and the whole process, does the experimental research、simulation analysis and process design. ASPEN PLUS was used to simulate the system, and according to the simulate result, pulverization spray regenerator was effective for concentrating the solution. Further, choose the packed tower as the absorber based on the analysis and comparison between the packed tower and the cooled tower.
As for the absorber, the internal factors (liquid gas ratio, the concentration and temperature of the solution) and external factors (the temperature of air, humidity) on the humidity of outlet air was inspected. Experimental data showed that the device had very good performance. The changes of internal factors have greater effect on the desiccant compare to the external factors. The mathematic model of the packed tower was established, and the simulation accorded with the experimental data. The model was used to analysis the outlet parameters of the air humidity, air temperature, solution concentration and temperature varieties alongside the tower. Low temperature and high concentration of the inlet solution can strengthen the dehumidification, while for the experimental device, the best mass flow of solution to air ratio is about 3.0.
As for the regeneration experiment with the pulverization spray regenerator, tested the regeneration capacity on different inlet solution temperature and air flow. Experimental data show that use the simple structure, low pressure drop pulverization spray regenerator to renew the dilute solution is totally feasible. The model of the regenerator was built to analysis the distribution of the outlet solution concentration and temperature. High inlet solution temperature can strengthen the regeneration, which was consistent to experimental data, while the inlet air temperature and humidity effects weakly.
引文
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[2]张立志.除湿技术.北京:化学工业出版社,2005.
[3]Lazzarin RM,Gasparella A,Longo GA.Chemical dehumidification by liquid desiccants:theory and experiment[J].International Journal of Refrigeration,1999,22(4):334-347.
[4]Gandhidasan P,Uhah U R,Kettleborough C F.Analysis of heat and mass transfer between a desiccant-air system in a packet tower[J].Journal of Solar Energy Engineering,1987,109(5):89-93.
[5]Abul-Wahab S A,Zurigat Y H,AbuArabiM K.Predictions of moisture removal rate and dehumidification effectiveness for structured liquid desiccant air dehumidifier[J].Energy,2004,29(1):19-34.
[6]Fumo N,Gsowami D Y.Study of an aqueous lithium chloride desiccant system:dehumidification and desiccant regeneration[J].Solar Energy,2002,72(4):351-361.
[7]Ertas A.Properties of a new liquid desiccant solution-Lithium chloride and calcium chloride mixture[J].SolarEnergy.1992,49(3):205-212.
[8]Ahmed S Y,Gandhidasan P,AlFarayedhiA A.Thermodynamic analysis of liquid desiccants[J].Solar Energy,1998,62(1):11-18.
[9]Ameel T A,Gee K G,Wood B D.Performance predictions of alternative,low cost absorbents for open cycle absorption solar cooling[J].Solar Energy,1995,54(2):65-73.
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