<div>In this study, three ducts have been built in Herrick Labs, Purdue University, West Lafayette, representing the real HVAC systems. Different types of filters have been tested in each duct, including MERV8, MERV14 mechanical filters, and MERV13 electret filter. One of this study's main objectives is to compare in-situ filter performance with the MERV rating, which comes from laboratory testing. Eventually, we can explain the variations and have a better understanding of the in-situ filter performance. Another primary objective is to evaluate the aging process of tested filters. Typically, HVAC filters will not be replaced or maintained frequently, so they tend to stay in HVAC systems for an extended period. In this study, the evolution of filter aging performance is tested continuously for the experiment's entire duration, including temporal evolution of pressure drops, filtration efficiencies, and loaded particulate mass on the filter media.</div><div><br></div><div>This study will continue for 52 full weeks. This thesis is a part of the on-going study, including the data up to the first 18 weeks so far. As a result, the pressure drops are steadily increasing over time for most filters due to the natural filter loading process, except for the MERV13 electret filter, which shows no significant change at all. In terms of the filtration efficiencies, two efficiency categories are included: mass-based efficiencies (ePM x ) for sizeintegrated particulate mass (PM) and size-resolved efficiencies. It can be seen that there is no significant change in ePM x for MERV8 and MERV14 filters, MERV13 electret filter whereas shows a degradation in ePM x efficiencies. Size-resolve efficiencies provide additional filtration efficiencies as a function of particle sizes, therefore more comprehensive. It can be found that for MERV8 and MERV14 filters, the efficiencies are slowly increasing for particles above 300 nm, with some variations. MERV13 electret filter has an explicitly decreasing trend for efficiencies across all particle size ranges.</div><div><br></div><div>Besides the filter loading process, another component affecting the filter performance is the environmental factor, such as temperature, relative humidity (RH), and precipitation events, including rainfall and snowfall. As a result, it can be observed that when precipitation events, the pressure drops trend to decrease for that period. It is also evident that decreasing temperature tends to promote pressure drops.</div>

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Este trabalho consiste na avaliação do desempenho de uma instalação piloto de dupla filtração no tratamento de água superficial, apresentando turbidez entre 8,5 e 21 uT. A instalação piloto constituída de um sistema de filtração de duas fases, com filtração direta ascendente em areia grossa seguida da filtração rápida descendente em areia fina. A taxa de filtração variou de 120 a 360 m3/m2.dia no filtro ascendente e de 200 a 400 m3/m2.dia no filtro ascendente. Foram executadas descargas de fundo intermediários no filtro ascendente durante a carreira de filtração para avaliar a instalação piloto. Além disso, simulou pico de turbidez, para avaliar as condições. Baseado no trabalho experimental concluiu-se que: (i) a eficiência global do sistema de dupla filtração ascendente em areia grossa foi satisfatória, apresentando efluente final com turbidez inferior a 1 uT e cor verdadeira inferior a 1 uH; (ii) a distribuição da perda de carga nas camadas do meio granular do FAAG não apresentou diferenças significativas para as variadas taxas de filtração e modo de operação (com e sem execução de DIFs); (iii) os ensaios que foram realizados com a execução de DIFs apresentaram carreiras de filtração mais longas. / This work concerns the study of the performance of a double filtration pilot plant whom treating surface water, presenting turbidity between 8,5 and 21,0 NTU. The pilot plant consisted of a two-stage filtration system, with an upflow coarse sand direct filtrer followed by a dowflow fine sand filter. Filtration rats varied from 120 to 360 m/day in the upflow filter and from 200 to 400 m/day in the downflow filter. Intermediate downflow in the upflow filter were performed during the run length do evaluate the performance of the pilot plant in addition, a peak of turbidity in the for influent selected filter operating varabile, was studied here in. Based on the experimental work carried out, it was concluded that: (i) the global efficiency of the system of double filtration with upflow filtration in coarse sand was satisfactory, presenting final efflents with inferior turbidity to 1,0 NTU and inferior true color to 1 uH; (ii) the distribution of the load loss in the layers of the granular middle of FAAG didn\'t present significant differences for the varied filtration taxes and operation way (with and without execution of DFIs); (iii) the rehearsals that were accomplished with the execution of DFIs presented longer filtration runs.

Up to date, sludge filterability has been characterized by the Ruth&rsquo / s classical filtration theory and quantified by the well-known parameter specific cake resistance (SCR). However, the complexity of the actual phenomenon is clearly underestimated by the classical filtration theory and SCR is often not satisfactory in describing filterability. Although many scientific studies were conducted for a better analysis and understanding of the filtration theory, still a practically applicable solution to replace the classical theory for a better description of filterability has not been proposed yet. In the present study, blocking filtration laws proposed by Hermans and Bred&eacute / e, dating back to 1936, which have been extensively used in the membrane literature for the analysis of fouling phenomenon and the multiphase filtration theory developed by Willis and Tosun (1980) highlighting the importance of the cake-septum interface in determining the overall filtration rate have been adopted for the analysis of filterability of sludge systems. Firstly, the inadequacy of the classical filtration theory in characterizing the filterability of real sludge systems and also the lack of the currently used methodology in simulating filtration operation was highlighted. Secondly, to better understand the effect of slurry characteristics and operational conditions on filtration, model slurries of spherical and incompressible Meliodent particles were formed. Finally, a methodology was developed with the gathered filtration data to assess the filterability of the sludge systems by both theories. The results clearly show that both approaches were superior to the classical approach in terms of characterizing the filterability of sludge systems. While blocking laws yielded a slurry specific characterization parameter to replace the commonly used SCR, the multiphase theory provided a better understanding of the physical reality of the overall process.

Made available in DSpace on 2016-06-02T19:56:43Z (GMT). No. of bitstreams: 1 3602.pdf: 6626298 bytes, checksum: 37082215cbad7185dd94995afede1d94 (MD5) Previous issue date: 2010-03-31 / Universidade Federal de Sao Carlos / A study on the compressibility of gas filtration cakes through their porosity investigation is presented in this work. The experimental unit consisted of a circular filter with a filtration area of 249 cm2 and a data acquisition system; mass flow rate and relative air humidity were controlled. The filter media used were a polyester felt (weighing 600 g/cm2) and an acrylic felt (weighing 550 g/cm2). A phosphate concentrate phosphate (&#961;p = 3.20 g/cm3 and dSt = 5.6 &#956;m) and a magnesium silicate (talc) (&#961;p = 3.09 g/cm3 and dSt = 2.5 &#956;m) were used as powder materials. Superficial filtration velocity was kept constant at 10 cm/s during phosphate concentrate filtration trials and five maximum pressure drops were set (100, 300, 600, 900 and 1200 mmH2O) at constant mass flow rate. Superficial filtration velocity was kept constant at 10 cm/s during talc filtration trials and four maximum pressure drops were set (300, 600, 900 and 1200 mmH2O) at constant mass flow rate. Trials at different filtration velocities (7.5 cm/s, 10 cm/s, 12.5 cm/s and 15.0 cm/s) were also performed. Initially, porosity data as a function of pressure drop per time were obtained. Each cake underwent a process to acquire the necessary resistance to be cut and embedded and then analyzed by a Scanning Electron Microscope. The obtained images were treated and analyzed in an image analyzing software which provided cakes porosity values. Afterwards, the influence of gas superficial velocity on average porosity was evaluated for cakes formed by talc powder. The porosity values obtained with the SEM images were compared to those obtained with equations found in the literature. A difference of 20 to 48% between experimental average porosity and estimated porosity was found for the phosphate concentrate cakes and of less than 13% for the talc cakes obtained at constant velocity. The average porosity values found for talc cakes were higher than those found for phosphate concentrate cakes, which was probably due to the fact that talc particles shape is extremely different from the spherical shape. A compressibility behavior for cakes of the two materials was possible to be observed. Talc cake porosity decreased with the increase of superficial filtration velocity. / Nesse trabalho apresenta-se um estudo da compressibilidade de tortas de filtração de gases através da investigação de sua porosidade. A unidade experimental consistiu de um filtro circular com área livre de filtração de 249 cm2, com vazão mássica e umidade relativa do ar controladas e um sistema de aquisição de dados. Os meios filtrantes utilizados foram um feltro de poliéster (gramatura 600 g/cm2) e um de acrílico (gramatura 550 g/cm2). Os materiais pulverulentos usados foram um concentrado fosfático (&#961;p = 3.20 g/cm3 e dSt = 5,6 &#956;m) e um silicato de magnésio (talco) (&#961;p = 3,09 g/cm3 e dSt = 2,5 &#956;m). Para os ensaios de filtração com a rocha fosfática foi fixada a velocidade superficial de filtração em 10 cm/s e cinco quedas de pressão máximas (100, 300, 600, 900 e 1200 mmH2O) à vazão mássica constante. Para os ensaios de filtração com o talco foi fixada a velocidade em 10 cm/s e quatro quedas de pressão máximas (300, 600, 900 e 1200 mmH2O) à vazão mássica constante. Também foram realizados ensaios para o talco a diferentes velocidades (7,5 cm/s, 10 cm/s, 12,5 cm/s e 15,0 cm/s). Inicialmente, obtiveram-se dados experimentais de porosidade em função da queda de pressão por tempo de filtração. Cada torta obtida passou por um tratamento para adquirir resistência necessária e ser analisada em um Microscópio Eletrônico de Varredura. As imagens obtidas foram tratadas e analisadas em um programa de análise de imagem fornecendo o valor da porosidade da torta. Posteriormente, analisou-se a influência da velocidade superficial de filtração na porosidade média de tortas de filtração formadas pelo talco. Compararam-se os valores de porosidade obtidos pelas imagens geradas no MEV com os obtidos por equações da literatura. Encontrou-se uma diferença de 20 a 48% entre os valores de porosidade média experimental e estimada para as tortas de rocha fosfática e de menos de 13% para o talco a velocidade constante. Os valores de porosidade média encontrados para o talco foram maiores que os encontrados para a rocha, provavelmente devido ao fato de que o formato das partículas de talco se distancia muito do formato esférico. Foi possível detectar um comportamento de compressibilidade para as tortas dos dois materiais. A porosidade das tortas de talco tendeu a diminuir com o aumento da velocidade superficial de filtração.

Este trabalho consiste na avaliação do desempenho de uma instalação piloto de dupla filtração no tratamento de água superficial, apresentando turbidez entre 8,5 e 21 uT. A instalação piloto constituída de um sistema de filtração de duas fases, com filtração direta ascendente em areia grossa seguida da filtração rápida descendente em areia fina. A taxa de filtração variou de 120 a 360 m3/m2.dia no filtro ascendente e de 200 a 400 m3/m2.dia no filtro ascendente. Foram executadas descargas de fundo intermediários no filtro ascendente durante a carreira de filtração para avaliar a instalação piloto. Além disso, simulou pico de turbidez, para avaliar as condições. Baseado no trabalho experimental concluiu-se que: (i) a eficiência global do sistema de dupla filtração ascendente em areia grossa foi satisfatória, apresentando efluente final com turbidez inferior a 1 uT e cor verdadeira inferior a 1 uH; (ii) a distribuição da perda de carga nas camadas do meio granular do FAAG não apresentou diferenças significativas para as variadas taxas de filtração e modo de operação (com e sem execução de DIFs); (iii) os ensaios que foram realizados com a execução de DIFs apresentaram carreiras de filtração mais longas. / This work concerns the study of the performance of a double filtration pilot plant whom treating surface water, presenting turbidity between 8,5 and 21,0 NTU. The pilot plant consisted of a two-stage filtration system, with an upflow coarse sand direct filtrer followed by a dowflow fine sand filter. Filtration rats varied from 120 to 360 m/day in the upflow filter and from 200 to 400 m/day in the downflow filter. Intermediate downflow in the upflow filter were performed during the run length do evaluate the performance of the pilot plant in addition, a peak of turbidity in the for influent selected filter operating varabile, was studied here in. Based on the experimental work carried out, it was concluded that: (i) the global efficiency of the system of double filtration with upflow filtration in coarse sand was satisfactory, presenting final efflents with inferior turbidity to 1,0 NTU and inferior true color to 1 uH; (ii) the distribution of the load loss in the layers of the granular middle of FAAG didn\'t present significant differences for the varied filtration taxes and operation way (with and without execution of DFIs); (iii) the rehearsals that were accomplished with the execution of DFIs presented longer filtration runs.

Die steigende Anzahl an Verfahren, in denen eine Filtration und eine Aufreinigung des gebildeten Filterkuchens durch Waschung notwendig ist, und die Steigerung deren Effizienz und Wirtschaftlichkeit verlangen nach einer Optimierung der Prozesse. Die Erarbeitung eines grundlegenden Verständnisses der Verdrängungsprozesse zwischen polaren und unpolaren Flüssigkeiten in einem Haufwerk schafft Erkenntnisse, die bei der Auswahl der verwendeten Lösungsmittel/Feststoffkombinationen während des Syntheseweges hilfreich sind. Durch die Verwendung von Silanen als Beschichtung kann die Oberflächeneigenschaft der Partikel variiert werden, während granulometrische Eigenschaften konstant bleiben. So dienen die Partikelsysteme als Basis der Untersuchungen zum Einfluss der Benetzungseigenschaften auf die Waschung unter Ausschluss anderer prozessbestimmender Variablen. Bei der Waschung der Partikelsysteme muss die Bedeutung der sich ausbildenden Phasengrenze herausgestellt werden. Sind Wasch- und Porenflüssigkeit nicht mischbar, bestimmt die auftretende Flüssig/Flüssig-Phasengrenze die Phänomenologie und die Effizienz des Prozesses. Das Auftreten einer Phasengrenze zwischen beiden Flüssigkeiten erlaubt die Aufnahme einer Flüssig/Flüssig-Kapillardruckkurve, die als Grenzkurve die zu erwartenden technischen Waschergebnisse darstellt. So kann eine Aussage darüber getroffen werden, welche Austauschverhältnisse und Restgehalte an Verunreinigung im Kuchen bei der Auswaschung mit nichtmischbaren Flüssigkeiten maximal zu erwarten ist.:ABBILDUNGSVERZEICHNIS SYMBOLVERZEICHNIS 1 EINLEITUNG 2 GRUNDLAGEN 2.1 FILTRATION 2.1.1 Kuchenbildung 2.1.2 Entfeuchtung 2.2 FILTERKUCHENWASCHUNG 2.3 SYSTEMEIGENSCHAFTEN 2.3.1 Feststoffe 2.3.2 Flüssigkeiten 2.3.3 Suspension 2.3.4 Haufwerk- und Kuchenstruktur 2.4 GRENZFLÄCHEN UND BENETZUNG DISPERSER SYSTEME 2.4.1 Oberflächenenergie 2.4.2 Benetzung 2.4.3 Kapillarität 2.5 BENETZUNG UND KAPILLARITÄT IN BEZUG ZUR FILTRATION 2.5.1 Die Kapillardruckkurve 2.5.2 Zusammenspiel von Benetzung und Filtration 2.5.3 Die Umnetzungskurve 2.6 SILANE – AUFBAU UND FUNKTION 3 MATERIALIEN UND METHODEN 3.1 STOFFSYSTEME 3.1.1 Partikelsystem 3.1.2 Flüssigkeiten 3.1.3 Silane 3.2 SILANISIERUNG ZUR VARIATION ZUR BENETZUNG 3.3 FESTSTOFFCHARAKTERISIERUNG 3.3.1 Laserbeugung 3.3.2 Statische Bildanalyse 3.3.3 Rasterelektronenmikroskopie 3.3.4 Energiedispersive Röntgenspektroskopie 3.3.5 Stickstoffadsorption 3.3.6 Thermogravimetrische Analyse 3.3.7 Ellipsometrie 3.3.8 Goniometrie 3.4 PROZESSRELEVANTE FLUID- UND SUSPENSIONSCHARAKTERISIERUNG 3.4.1 Tensiometrie 3.4.2 Grenzflächenrheometrie 3.4.3 Sedimentations- und Kompressionsmessung 3.5 VERSUCHSDURCHFÜHRUNG 3.5.1 Filtration 3.5.2 Waschung 3.5.3 Bestimmung Filtrat- und Retentatkonzentration 3.5.4 Kapillardruckkurve 3.5.5 Umnetzungskurve 4 OBERFLÄCHENKONFIGURATION DER PARTIKELSYSTEME MITTELS SILANEN 4.1 VARIATION DER OBERFLÄCHENENERGIE 4.2 AUSBILDUNG DER SILANSCHICHT 4.3 KONSISTENZ DER DISPERSEN FESTSTOFFEIGENSCHAFTEN 5 BENETZUNGSEFFEKTE BEI DER WASCHUNG VON FILTERKUCHEN 5.1 STRUKTURBILDUNG BEI DER FILTRATION 5.1.1 Sedimentationseigenschaften 5.1.2 Filterkuchenbildung 5.2 KUCHENWASCHUNG 5.2.1 Kuchenwaschung mit mischbaren Systemen 5.2.2 Kuchenwaschung mit nichtmischbaren Systemen 5.2.3 Viskositätsdifferenz 5.2.4 Nachweis der aufgestellten Theorien 6 DARSTELLUNG DES WASCHUNGSGLEICHGEWICHTES ÜBER EINE UMNETZUNGSKURVE 6.1 MESSTECHNISCHE ERFASSUNG 6.1.1 Technische Methode 6.1.2 Druckmethode 6.2 HAUPTEINFLUSSPARAMETER AUF DIE UMNETZUNGSKURVE 6.2.1 Variation der Benetzung 6.2.2 Variation der Partikelform 6.2.3 Variation der Partikelgröße 6.3 VERGLEICH: UMNETZUNGS- UND KAPILLARDRUCKKURVEN 7 SCHLUSSWORT LITERATURVERZEICHNIS ANHANG