Дисертації з теми "Functional Continuous Flow Reactors"
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Lange, David M. "Emulsion copolymerization with functional monomers in continuous reactors." Diss., Georgia Institute of Technology, 1991. http://hdl.handle.net/1853/11867.
Повний текст джерелаBaker, Alastair. "Flow reactors for the continuous synthesis of garlic metabolites." Thesis, Cardiff University, 2015. http://orca.cf.ac.uk/86704/.
Повний текст джерелаSkillinghaug, Bobo. "Palladium(II)-Catalysed Heck and Addition Reactions : Exploring Decarboxylative and Desulfitative Processes." Doctoral thesis, Uppsala universitet, Avdelningen för organisk farmaceutisk kemi, 2016. http://urn.kb.se/resolve?urn=urn:nbn:se:uu:diva-304746.
Повний текст джерелаKoc, Yasemin. "Optimization of continuous flow polymerase chain reaction with microfluidic reactors." Thesis, Imperial College London, 2008. http://hdl.handle.net/10044/1/8184.
Повний текст джерелаYucel, Cakal Gaye O. "Dynamic Behavior Of Continuous Flow Stirred Slurry Reactors In Boric Acid Production." Phd thesis, METU, 2005. http://etd.lib.metu.edu.tr/upload/12605047/index.pdf.
Повний текст джерелаs) in series system. In this reaction system there are at least three phases, one liquid and two solid phases (colemanite and gypsum). In a batch reactor all the phases have the same operating time (residence time), whereas in a continuous reactor all the phases may have different residence time distributions. The residence time of both the reactant and the product solids are very important because they affect the dissolution conversion of colemanite and the growth of gypsum crystals. The main aim of this study was to investigate the dynamic behavior of continuous flow stirred slurry reactors. By obtaining the residence time distribution of the solid and liquid components, the non-idealities in the reactors can be found. The experiments performed in the continuous flow stirred slurry reactors showed that the reactors to be used during the boric acid production experiments approached an ideal CSTR in the range of the stirring rate (500-750 rpm) studied. The steady state performance of the continuous flow stirred slurry reactors (CFSSR&rsquo
s) in series was also studied. During the studies, two colemanites having the same origin but different compositions and particle sizes were used. The boric acid production reaction consists of two simultaneous reactions, dissolution of colemanite and crystallization of gypsum. The dissolution of colemanite and the gypsum formation was followed from the boric acid and calcium ion concentrations, respectively. The effect of initial CaO/ SO42- molar ratio (1.00, 1.37 and 2.17) on the boric acid and calcium ion concentrations were searched. Also, at these initial molar ratios the colemanite feed rate was varied (5, 7.5, 10 and 15 g/min) to change the residence time of the slurry. Purity of the boric acid solution was examined in terms of the selected impurities, which were the magnesium and sulfate ion concentrations. The concentrations of them were compared at the initial molar ratios of 1.00 and 1.37 with varying colemanite feed rates. It was seen that at high initial CaO/ SO42- molar ratios the sulfate and magnesium ion concentrations decreased but the calcium ion concentration increased. The gypsum crystals formed in the reaction are in the shape of thin needles. These crystals, mixed with the insolubles coming from the mineral, are removed from the boric acid slurry by filtration. Filtration of gypsum crystals has an important role in boric acid production reaction because it affects the efficiency, purity and crystallization of boric acid. These crystals must grow to an appropriate size in the reactor. The growth process of gypsum crystals should be synchronized with the dissolution reaction. The effect of solid hold-up (0.04&ndash
0.09), defined as the volume of solid to the total volume, on the residence time of gypsum crystals was investigated and the change of the residence time (17-60 min) on the growth of the gypsum was searched. The residence time at each reactor was kept constant in each experiment as the volumes of the reactors were equal. The growth of gypsum was examined by a laser diffraction particle size analyzer and the volume weighted mean diameters of the gypsum crystals were obtained. The views of the crystals were taken under a light microscope. It was observed that the high residence time had a positive effect on the growth of gypsum crystals. The crystals had volume weighted mean diameters of even 240 µ
m. The gypsum crystal growth model was obtained by using the second order crystallization reaction rate equation. The residence time of the continuous reactors are used together with the gypsum growth model to simulate the continuous boric acid reactors with macrofluid and microfluid models. The selected residence times (20-240 min) were modeled for different number of CSTR&rsquo
s (1-8) and the PFR. The simulated models were, then verified with the experimental data. The experimentally found calcium ion concentrations checked with the concentrations found from the microfluid model. It was also calculated that the experimental data fitted the microfluid model with a deviation of 4-7%.
Bennett, Samuel. "The production of biofuel from waste oil using continuous microwave flow reactors." Thesis, Liverpool John Moores University, 2012. http://ethos.bl.uk/OrderDetails.do?uin=uk.bl.ethos.582852.
Повний текст джерелаSun, Xiaoyan. "Comparative study on substrate removal kinetics for continuous flow and sequencing batch reactors." Thesis, University of Ottawa (Canada), 1993. http://hdl.handle.net/10393/6944.
Повний текст джерелаWang, Yantao. "Synthesis and conversion of furfural-batch versus continuous flow." Thesis, Compiègne, 2019. http://www.theses.fr/2019COMP2474/document.
Повний текст джерелаFurfural, which has been identified as one of top 30 bio-based chemicals, is an important green platform molecule, The aim of this PhD work is to realize the synthesis and conversion of furfural in batch and continuous flow. Here, we developed sorne greener methods for furfural synthesis, and valorized furfural into high value-added products, such as 2-furonitrile, furfuryl alcohol etc. Several keys issues were identified in order to design processes greener than the current ones. ln detail, experiments for furfural synthesis were performed in water or in water and organic solvent when co-solvents (green or eco-friendly) are necessary. Microwave irradiation has been chosen as the heating method to accelerate the dehydration process, and microwave continuous flow reactor was also applied to improve furfural productivity. When starting from furfural to produce high value-added chemicals, efficient flow reactors, suc as Pheonix, H-cube Pro as well as microwave continuous flow With micro-reactor, were also identified as interesting alternatives to improve the productivities of target compounds. As a result, some promising results were obtained in the viewpoint of industry
Thompson, Lisa Alice. "Chemo- and bio-catalysis for the synthesis of chiral amines in continuous flow reactors." Thesis, University of Leeds, 2017. http://etheses.whiterose.ac.uk/18514/.
Повний текст джерелаGruar, R. I. J. "Synthesis and characterisation of nanomaterials produced using laboratory and pilot scale continuous hydrothermal flow reactors." Thesis, University College London (University of London), 2013. http://discovery.ucl.ac.uk/1386635/.
Повний текст джерелаSchmiegel, Carsten Janis [Verfasser]. "Continuous flow investigation of organocatalyzed reactions using gel-bound catalysts inside microfluidic reactors / Carsten Janis Schmiegel." Paderborn : Universitätsbibliothek, 2021. http://d-nb.info/1236630033/34.
Повний текст джерелаMongeon, Sébastien. "Active and Passive Mixing for Immiscible Liquid-Liquid Systems: A Performance Evaluation of Novel Micro-Reactors." Thesis, Université d'Ottawa / University of Ottawa, 2018. http://hdl.handle.net/10393/37089.
Повний текст джерелаZhao, Deyang. "Insights into the biomass based compounds valorization in batch versus continuous flow." Thesis, Compiègne, 2020. http://www.theses.fr/2020COMP2551.
Повний текст джерелаFurfural (FF) and 5-hydroxymethylfurfural (HMF) have been identified as important bio-based versatile chemicals, their oxidation, reduction, hydrolysis and polymerization products attracted more interests for the high value and Wide applications. The aim of this PhD work is to realize the conversion of FF and HMF into high value downstream products in both conventional and intensification processes. Therefore, the comparation between conventional heating and microwave heating method, batch With continuous flow regime was explored regarding FF derivatives and HMF valorization reaction in my work. The development of greener, durable and efficient catalysts to realize the conversion of bio-based compounds has been employed. Target compounds such as methyl levulinate (ML), gamma-valerolactone (GVL), 5-hydroxymethyl-2-furancarboxylic acid (HMFCA), 2,5-furandicarboxylic acid (FDCA) were investigated. At the same time, the application of FDCA was also performed, the production of three differen kinds of furan-based polyesters: polyethylene-2,5-furandicarboxylate (PEF), polyhydropropyl-2,5furandicarboxylate (PHPF) and polydiglycerol-2,5-furandicarboxylate (PDGF) were realized through polytransesterification between diethyl furan-2,5-dicarboxylate (DEFDC) and a defined diol furan-based prepolyme or pure diglycerol. Several important issues were identified in order to design processes greener than the current ones. For instance, the experiments for HMF oxidation were performed in water. Microwave irradiation has been chosen as the heating method to accelerate the reaction. Continuous flow reactors, such as Pheonix, H-cube Pro as well as microwave continuous flow were identified as interesting alternatives to improve the productivities of target compounds. As a result, some promising results were obtained in the viewpoint of industry
CHI, LEE WEI, and 李偉齊. "Optimal Conditions for Synthesizing N-Butyl Phenyl Ether by Liquid-Liquid-Solid Phase Transfer Catalysis with Batch and Continuous Flow Reactors." Thesis, 2000. http://ndltd.ncl.edu.tw/handle/25201430084062512813.
Повний текст джерела國立成功大學
化學工程學系
88
In this study, tributylamine was immobilized on chloromethylated poly-styrene polymer which was utilized as a support to prepare the triphase catalysts. All of the prepared triphase catalysts were then used to catalyze the ether reaction of n-bromobutane (the organic reactant) with sodium phenolate (the aqueous reactant) for synthesizing n-butyl phenyl ether. The feasibility of carrying out this triphase catalytic reaction by employing a continuous-flow stirred vessel reactor(CFSVR)was also investigated. The dissertation is divided into three parts. The first part relates to the conditions for immobilizing tributylamine on chloromethylated polystyrene polymeric supports. The second part presents the results and discussion of triphase catalysis by the prepared triphase catalysts in a batch reactor. The third part deals with the triphase catalysis in a continuous flow stirred vessel reactor, which was designed by our laboratory, operated under the conditions determined by referring to the results obtained in the second part. In the first part, the variables including the properties of polymeric support(extent of chloromethylation, degree of crosslinking, particle size), temperature, kinds of organic solvents and the concentration of tributylamine affecting the immobilization reaction were investigated. From the experimental results, it is found that the reaction is a limiting step in the immobilization process. Besides, high extent of chloromethylation, high reaction temperature, high molar ratio of tributylamine to chloromethyl group in supports(6:1)and aprotic solvent are beneficial to immobilization reaction rate and the amount of tributylamine immobilized on the support. In the second part, the factors influencing the conversion of n-bromobutane and the fractional yield of n-butyl phenyl ether were investi-gated. The factors include the order of solvent addition, agitation speed, volumetric ratio of organic solvent and water, the amount of catalyst, reaction temperature, the kinds of organic solvents, the concentration of reactant in organic or aqueous phase, and the kinds and amounts of salts. The experimental results show that the supported catalyst prepared from the first part has good catalytic activity for the reaction between n-bromobutane and sodium phenolate. The mass transfer resistance can be neglected when the agitation speed is beyond 200 rpm. A higher conversion of n-bromobutane can be obtained when the volumes of organic solvent and water are equal. The increases in the amount of catalyst and temperature will enhance the reaction rate, but a high concentration of reactant in organic or aqueous phase and the addition of salts lowers the conversion of n-bromobutane. However, the existence of salts benefits the fractional yield of the main product(n-butyl-phenyl-ether). When a nonpolar solvent such as n-heptane is utilized, a higher conversion of n-bromobutane can be obtained at a sacrifice of the fractional yield of the main product. The order of solvent addition has less effect on the conversion of n-bromobutane. A triphase catalyst will have a higher catalytic activity when it is provided with an appropriate lipophilicity. In the third part, the above three-phase reaction was carried out in a continuous-flow stirred vessel reactor under the conditions determined by referring the results obtained from a batch reactor. The effects of variables, including agitation speed, catalyst deactivation, the amount of catalyst, concentrations of reactants in organic and aqueous phases, reaction temperature and the volumetric flow rate of organic and aqueous phase on the reaction were investigated. The experimental results reveal that the conversion of n-bromobutane maintains a constant value when the agitation speed is over 400 rpm. The reaction rate increases with the increasing amount of catalyst and temperature. The conversion of n-bromobutane decreases with the increase of the volumetric flow rate of the organic and aqueous phases. With the increase of the reactant concentration(n-bromobutane)in the organic phase, the conversion of n-bromobutane will at first maintain a fixed value (< 0.018mole)and then decreases. On the other hand, with the increase of the reactant concentration(sodium phenolate)in the aqueous phase, the conversion of n-bromobutane will increase first and then decreases, and an optimum value exists. As to the stability, the triphase catalyst slightly loses its activity during a long-time operation.
Chang, Wang Min, and 王敏昌. "Synthesis of Allyl Phenyl Ether by Tri-Liquid and Liquid-Liquid-Solid Phase Transfer Catalysis with Continuous Flow Stirred Vessel Reactors." Thesis, 2001. http://ndltd.ncl.edu.tw/handle/98025539407520349827.
Повний текст джерела國立成功大學
化學工程學系
89
In this study, the feasibilities of using tri-liquid-phase and liquid-liquid-solid phase transfer catalysis techniques for synthesizing allyl phenyl ether by etherification of allyl bromide (the organic reactant) and sodium phenolate (the aqueous reactant) were evaluted and compared. Tetrabutylammonium bromide, a soluble catalyst, was used in the tri-liquid-phase catalysis while the supported tributylamine, which was immobilized on the chloromethylated styrene-DVB copolymer, was employed as the triphase catalyst. Both catalytic reactions were carried out in a continuous-flow stirred vessel reactor (CFSVR). This dissertation consists of four parts. In the first part, the experimental results of the tri-liquid phase catalysis in a CFSVR were explained and discussed. The second part deals with the liquid-liquid-solid phase transfer catalysis in a batch reactor, while the third part presents the results of the liquid-liquid-solid phase transfer catalysis in a CFSVR, which was operated under the conditions determined by referring to the results obtained in the second part. The performances of these two techniques, tri-liquid and liquid-liquid-solid phase transfer catalysis, were compared in the fourth part. In the first part, the effects of operating variables including mole fraction of QBr, inlet reactant mole ratio, agitation speed, operating temperature, reactant volumetric flow rate, stability of catalysts and the installation of baffles in the bottom of reactor on the performance of the tri-liquid phase catalytic system were investigated. Experimental results indicate that increasing the amount of salts and utilizing non-polar organic solvent will enhance the formation of third-liquid phase. To concentrate catalysts in the third-liquid phase and to save the dosage of catalysts, appropriate mole fraction of QBr should be between 0.3 and 0.5. Feed with equal organic-to-aqueous reactant molar ratio will reduce the catalyst loss rate. The interfacial mass transfer resistance can be neglected when the agitation speed is beyond 300 rpm. However, catalyst loss rate would rise up when the agitation speed exceeded 800 rpm. Therefore, agitation speed was fixed at 800 rpm in this study. The installation of baffles improves the separation of third-liquid phase and aqueous phase, hence reduce catalysts loss rate effectively. High temperatures will lower catalyst loss rate, while low temperatures reduces stability of third-liquid phase. Therefore, a high temperature is preferred, the reasonable operating temperature is 50℃. For finding proper operating conditions for the continuous operation of the liquid-liquid-solid system, in the second part, the effects of the operating variables, including agitation speed, volumetric ratio of organic solvent and water, kinds of organic solvents, amount of catalysts, operating temperature, kinds and amounts of salts, on the performance of a batch reactor were studied first. The experimental results show that: The interfacial mass transfer resistance can be neglected when the agitation speed is fixed at 600 rpm. Higher conversion of allyl bromide and fraction yield of allyl phenyl ether will be obtained when the volumes of organic solvent and water are equal. Kinds of organic solvent have little effect on the fraction yield of main product when no catalyst is used. However, organic solvent of higher polarity increases not only the conversion of allyl bromide but also the fraction yield of allyl phenyl ether when 3g of catalysts are employed. A high temperature will induce more side-reactions while a low temperature results in water solvation, appropriate temperature is 40℃. Existence of salts restrains the activity and selectivity of catalysts. The extent of inhibition depends on the amount of salts added but is nearly independent on the kinds of salts. The third part presents the results of the reaction carried out in a CFSVR under the conditions determined by referring to the results obtained in the second part. The variables investigated include agitation speed, amount of catalysts, reactant volumetric flow rate, operating temperature and catalysts deactivation. Experimental results reveal that catalyst decays obviously under high temperatures. To prevent evaporation, the proper temperature is 40℃. Increasing the amount of catalyst will give a higher reaction rate, however, excess catalysts will cause coagulation and the catalyst particles would not be well scattered in agitation. Because etherification reaction in this experiment is irreversible pseudo-first-order, increasing the inlet aqueous or organic reactant concentration will have little effect on the conversion of allyl bromide. As to the stability, catalyst obviously loses its activity during a long-time operation. The inlet dispersion phase can not mix well immediately with another dispersion phase primarily existing in the CFSVR, therefore, the observed outlet concentration of allyl bromide is higher than the predicted value. In turn, both the reaction rate and the conversion are higher than the value predicted from the model for the batch reactor. The performances of the tri-liquid-phase and liquid-liquid-solid systems are compared in the final part. The comparison is based on five items namely, activity, selectivity, stability, the operation of continuous-flow reactor and the procedure of preparing catalysts. (1). Because of the hydrophobic property of polymer-supported catalysts, the aqueous reactant is hard to diffuse into the active sites inside the catalysts, the reaction of liquid-liquid-solid catalytic system only proceeds on the external surface of catalyst particles. Therefore, the catalytic activity in the tri-liquid phase catalysis is much better than that in the liquid-liquid-solid phase transfer catalysis under the same amount of catalysts. (2). The third-liquid phase is more stable than the polymer-supported catalyst, but the third-liquid phase might be dissolved slightly in the water. (3). The fraction yield of main product obtained by the tri-liquid phase transfer catalysis is higher than that with the liquid-liquid-solid phase transfer catalysis. Oxygen-allylation is the main reaction in the tri-liquid phase catalysis. However, side-reactions may take place in carbon-allylation pathway within liquid-liquid-solid phase transfer catalysis. (4). Both of tri-liquid and liquid-liquid-solid phase transfer catalysis can recover catalysts easily but excessive concentration of salts in the tri-liquid phase catalytic system may result in the formation of salt crystals and the loss of catalysts. (5). The procedure of preparing polymer-supported catalysts is complicated and the reproducibility is not as well as the formation of a third liquid phase in the tri-liquid phase system. 1-1 傳統的兩液相反應系統---------------------------------------------------1 1-2 相間轉移觸媒的種類------------------------------------------------------2 1-3 液-液-固三相催化反應----------------------------------------------------4 1-3-1 液-液-固三相觸媒-------------------------------------------------4 1-3-2 續流式液-液-固三相催化反應----------------------------------6 1-4 三液相催化反應------------------------------------------------------------7 1-4-1 三液相催化反應系統---------------------------------------------7 1-4-2 第三液相觸媒的重複使用性------------------------------------8 1-5丙烯基苯基醚的合成-------------------------------------------------------8 1-6本論文的研究內容--------------------------------------------------------10 第二章 實驗--------------------------------------------------------------------------12 2-1 實驗藥品-------------------------------------------------------------------12 2-2 實驗方法-------------------------------------------------------------------13 2-3 分析方法-------------------------------------------------------------------16 2-3-1 固體觸媒中氯離子含量(活性基)之分析---------------------16 2-3-2 四正丁基銨離子濃度的分析------------------------------------18 2-3-3 氣相層析法(G.C.)分析-------------------------------------------18 2-4 校正曲線-------------------------------------------------------------------19 2-5 反應物轉化率與主產物生成分率的定義----------------------------20 第三章 續流式三液相反應--------------------------------------------------------25 3-1 形成第三液相之適當條件--------------------------------------27 3-2 適當操作條件之分析-------------------------------------------29 3-3 不同流率下反應器所需穩定時間-------------------------------29 3-4擋板效應對轉化率與觸媒流失率的影響-----------------------30 3-5 攪拌速率的效應--------------------------------------------------------30 3-6反應溫度與進料流率的效應------------------------------------------31 3-7 不同莫耳比進料的效應-------------------------------------------32 3-8 三液相觸媒的穩定性-------------------------------------------------33 第四章 批式液-液-固三相反應---------------------------------------------------44 4-1攪拌速率對反應的影響--------------------------------------------------46 4-2 油、水體積比對反應的影響---------------------------------------------47 4-3 有機溶劑種類對反應的影響-------------------------------------------48 4-4 觸媒添加量對反應的影響----------------------------------------------49 4-5 溫度對反應的影響-------------------------------------------------------50 4-6 丙烯基溴添加量對反應的影響----------------------------------------51 4-7 酚化鈉添加量對反應的影響-------------------------------------------51 4-8鹽類種類與添加量對反應的影響--------------------------------------52 4-9 觸媒重複使用次數對反應的影響-------------------------------------53 4-10 機械攪拌力對觸媒活性的影響---------------------------------------53 4-11 反應速率式的推導-----------------------------------------------------54 第五章 續流式液-液-固三相反應------------------------------------------------75 5-1不同流率下反應器所需穩定時間--------------------------------------75 5-2 攪拌速率的效應----------------------------------------------------------76 5-3 觸媒添加量的效應-------------------------------------------------------76 5-4 反應溫度與進料流率的效應-------------------------------------------77 5-5 三相觸媒的穩定性-------------------------------------------------------77 5-6 酚化鈉濃度效應----------------------------------------------------------78 5-7 丙烯基溴濃度效應-------------------------------------------------------78 5-8 由續流攪拌式反應器推測反應速率式-------------------------------78 5-9續流攪拌式反應器與批式反應器的比較-----------------------------79 第六章 結論與未來研究方向-----------------------------------------------------91 6-1 三液相系統與液-液-固系統之綜合比較-----------------------------91 6-1-1催化活性------------------------------------------------------------91 6-1-2觸媒穩定性---------------------------------------------------------91 6-1-3反應選擇性---------------------------------------------------------92 6-1-4續流式操作的難易度---------------------------------------------93 6-1-5觸媒製備程序------------------------------------------------------93 6-2 結論-------------------------------------------------------------------------93 6-3 對未來研究方向建議----------------------------------------------------97 參考文獻-----------------------------------------------------------------------------100 自述-----------------------------------------------------------------------------------104
(6588797), Joseph A. Oliva. "Process Intensification Techniques for Continuous Spherical Crystallization in an Oscillatory Baffled Crystallizer with Online Process Monitoring." Thesis, 2019.
Знайти повний текст джерелаGuided by the continuous manufacturing paradigm shift in the pharmaceutical industry, the proposed thesis focuses on the implementation of an integrated continuous crystallization platform, the oscillatory baffled crystallizer (OBC), with real time process monitoring. First, by defining an appropriate operating regime with residence time distribution (RTD) measurements, a system can be defined that allows for plug flow operation while also maintaining solid suspension in a two-phase system. The aim of modern crystallization processes, narrow crystal size distributions (CSDs), is a direct result of narrow RTDs. Using a USB microscope camera and principal component analysis (PCA) in pulse tracer experiments, a novel non-contact RTD measurement method was developed using methylene blue. After defining an operating region, this work focuses on a specific process intensification technique, namely spherical crystallization.
Used mainly to tailor the size of a final dosage form, spherical crystallization removes the need for downstream size-control based unit operations (grinding, milling, and granulation), while maintaining drug efficacy by tailoring the size of the primary crystals in the agglomerate. The approach for generating spherical agglomerates is evaluated for both small and large molecules, as there are major distinctions in process kinetics and mechanisms. To monitor the spherical agglomeration process, a variety of Process Analytical Technology (PAT) tools were used and the data was implemented for scale-up applications.
Lastly, a compartmental model was designed based on the experimental RTD data with the intention of predicting OBC mixing and scale-up dynamics. Together, with validation from both the DN6 and DN15 systems, a scale independent equation was developed to predict system dispersion at different mixing conditions. Although it accurately predicts the behavior of these two OBC systems, additional OBC systems of different scale, but similar geometry should be tested for validation purposes.
Wang, Chu-Ming, and 王志民. "Tri-Liquid-Phase Phase Transfer Catalysis-Optimal Operating Conditions for Synthesizing N-Butyl Phenyl Ether from N-Butyl Bromide and Sodium Phenolate in Batch and Continuous-Flow Reactors." Thesis, 1996. http://ndltd.ncl.edu.tw/handle/42064457713580795497.
Повний текст джерела國立成功大學
化學工程學系
84
ABTRACT In a previous study in our laboratory on the reaction between n-butyl bromide (BuBr) and sodium phenolate (NaOPh) with tetrabutylammonium bromide (QBr) as a phase transfer catalyst,we found that a third liquid phase appeared when the aqueous and organic phases with poor catalyst. The reaction rate in such a tri-liquid-phase phase transfer catalysis is faster than the bi-liquid-phase system,and the catalyst can be easily recovered and reused.In this work we try to find the optimal operating conditions for the same reaction in batch and continuous-flow reactors. The experimental results reveal that the reaction rate increases with the amount of QBr. When lesser amount of NaOPh is used,the reaction rate will increase first and then decrease with the addition of NaOH,until it becomes a stale condition.Thougt lift up the reaction temperature will be helpful about the reaction,the catalyst is more easily decomposed. The results of continuous-flow reactor show that the concertration of catalyst,and the conversion of BuBr in turn,will decline slowly with the operation time though the solubilities of catalyst in aqueous and organic solutions are small.This weakness can be overcome by adding a small amount of catalyst in aqueous feed. In the investigation on the main factors affecting the reaction rate,we found that low concertration of NaOPh,and high concertration of QBr and NaOH would benetic the generation of a third liquid phase.Under these operating conditions,high conversion of BuBr can be achieved in less reaction time when a batch reactor is employed,it is also applied to the operation of a continuous-flow reactor. From this study,we can understand more about the optimal operating conditions for the phase transfer catalysis reaction in batch and continuous-flow reactors.