Atom transfer radical polymerisation - towards the synthesis of a fully-functional photorefractive polymer

Atom transfer radical polymerisation (ATRP) of styrene in xylene solution initiated with 1-phenylethyl bromide and mediated by CuBr/N-propyl-2- pyridinemethanimine catalyst complex was studied. The polymerisation was ill-controlled, yielding polymers with broad molecular weight distributions and values of number average molecular weight considerably higher than the theoretical values calculated from 100% initiator efficiency. The degree of control afforded over the polymerisation was enhanced by use of a more soluble catalyst complex, CuBr/N-octyl-2-pyridinemethanimine. Furthermore, the use of a more polar solvent, diglyme, generated a homogeneous catalyst complex that facilitated the production of polymers having narrow molecular weight distributions (1.10 < PDi < 1.20). The kinetics of the atom transfer radical polymerisation of methyl methacrylate at 90°C in diglyme solution initiated with ethyl-2-bromoisobutyrate and mediated by CuBr/N-octyl-2-pyridinemethanimine was studied and the orders of the reaction were established. The effect on the rate of polymerisation of the ratio of CuBr:N-octyl-2-pyridinemethanimine was also determined. The temperature dependencies of the rate of polymerisation of methyl methacrylate in diglyme solution and xylene solution were studied, and were found to be non-linear and dependent upon the polarity of the solvent. The use of highly polar aprotic solvents, such as N,N-dimethylformamide and dimethylsulphoxide, was found to be detrimental to the degree of control afforded over the polymerisation of methyl methacrylate. This was circumvented by use of a 5-fold excess, over that conventionally used, of catalyst complex. The atom transfer radical polymerisation of (4-nitrophenyl)-[3-[N-[2- (methacryloyloxy)ethyl]carbazolyl]]diazene in dimethyl sulphoxide solution was studied. Although homopolymerisation yielded only oligomers, copolymerisation of this monomer with methyl methacrylate was found to be readily achievable. Keywords: ATRP, Styrene; Methyl methacrylate; Polar solvents; Fully-functional photorefractive polymer. 2

Investigation of the metabolism of N, N-Dimethylformamide and its metabolites

The industrial solvent N, N-dimethylformamide (DMF) causes liver damage in humans. The hepatotoxicity of N-alkylformamides seems to be linked to their metabolism to N-alkylcarbamic acid thioesters. To clarify the role of metabolism in DMF hepatotoxicity, the metabolic fate of DMF was investigated in rodents. DMF was rapidly metabolised and excreted in the urine as N-hydroxymethyl-N-methyl-formamide (HMMF), N-acetyl-S-(N-methylcarbamoyl) cysteine (AMCC) and a metabolite measured as formamide by GLC. At high doses (0.7 and 7.0mmo1/kg) a small proportion of the dose was excreted unchanged. AMCC, measured by GLC after derivatisation to ethyl N-methylcarbamate, was a minor metabolite. Only 5.2% of the dose (0.1mmo1/kg) in rats or 1.2% in mice was excreted as AMCC. The minor extent of this metabolic pathway in rodents might account for the marginal liver damage induced by DMF in these species. In a collaborative study, volunteers were shown to metabolise DMF to AMCC to a greater extent than rodents. Nearly 15% of the inhaled dose (0.049mmo1/kg) was excreted as AMCC. This result suggests that the metabolic pathway leading to AMCC is more important in humans than in rodents. Consequently the risk associated with exposure to DMF might be higher in humans than in rodents. The metabolism of formamides to S-(N-alkylcarbamoyl) glutathione, the metabolic precursor of the thioester mercapturates, was studied using mouse, rat and human hepatic microsomes. The metabolism of NMF (10mM) to S-(N-methylcarbanoyl)glutathione (SMG) required the presence of GSH, NADPH and air. Generation of S-(N-methyl-carbamoyl)glutathione (SMG) was inhibited when incubations were conducted in an atmosphere of CO:air (1:1) or when SKF 525-A (3.0mM) was included in the incubations. Pre-treatment of mice with phenobarbitone (PB, 80mg/kg for 4 days) or beta-naphthoflavone (BNF, 50mg/kg for 4 days) failed to increase the microsomal formation of SMG from NMF. This result suggests that the oxidation of NMF is catalysed by a cytochrome P-450 isozyme which is unaffected by PB or BNF. Microsomal incubations with DMF (5 or 10mM) failed to generate measurable amounts of SMG although DMF was metabolised to HMMF. Incubations of microsomes with HMMF resulted in the generation of a small amount of SMG which was affected by inhibitors of microsomal enzymes in the same way as in the case of NMF. HMMF was metabolised to AMCC by rodents in vivo. This result suggests that HMMF is a major intermediate in the metabolic activation of DMF.

The role of metabolism in the toxicity of N-alkylformamides

Using ionspray tandem mass spectrometry the glutathione conjugate SMG was identified as a biliary metabolite of DMF in rats (0.003% of a dose of 5OOmg/kg DMF i.p.). Formation of this metabolite was increased five fold after induction of CYP2E1 by acetone, and was inhibited to 20% of control values following pretreatment with disulfrram. Generation of SMG from DMF in vivo was shown to exhibit a large kinetic deuterium isotope effect (KWKD=10.1 ± 1.3), which most likely represents the product of 2 discrete isotope effects on N-demethylation and formyl oxidation reactions.The industrial solvent N,N-dimethylformamide (DMF) and the investigational anti-tumour agent N-methylformamide (NMF) cause liver damage in rodents and humans. The hepatotoxicity of N-alkylformamides is linked to their metabolism to N-alkylcarbamic acid thioesters. The enzymatic details of this pathway were investigated. Hepatocytes isolated from BALB/c mice which had been pretreated with acetone, an inducer of the cytochrome P-450 isozyme CYP2E1, were incubated with NMF (10mM). NMF caused extensive toxicity (> 90% ) as determined by lactate dehydrogenase (LDH) release, compared to cells from untreated animals. Incubation of liver cells with NMF for 6 hrs caused 60±17% LDH release whilst in the presence of DMSO (10mM), an alternative substrate for CYP2E1, LDH release was reduced to 20±10% . The metabolism of NMF to S-(N-methylcarbamoyl)glutathione (SMG) was measured in incubates with liver microsomes from mice, rats or humans. Metabolism of NMF was elevated in microsomes isolated from rats and mice pretreated with acetone, by 339% and 183% respectively. Pretreatment of animals with 4-methylpyrazole induced the metabolism of NMF to 280% by rat microsomes, but was without effect on NMF metabolism by mouse microsomes. The CYP2E1 inhibitors or alternative substrates diethyl dithiocarbamate (DEDTC), p-nitrophenol (PNP) and dimethyl sulphoxide (DMSO) strongly inhibited the metabolism of NMF in suspensions of rat liver microsomes, at concentrations which did not effect aminopyrine N-demethylation. The rate of metabolism of NMF to SMG in human microsomes correlated (r> 0.8) with the rate of metabolism of chlorzoxazone, a CYP2E1 probe. A polyclonal antibody against rat CYP2E1 (10mg/nmol P-450) inhibited NMF metabolism in microsomes from rats and humans by 75% and 80% , respectively. The amount of immunoblottable enzyme in human microsomes, determined using an anti-rat CYP2E1 antibody, correlated with the rate of NMF metabolism (r> 0.8). Purified rat CYP2E1 catalysed the generation of SMG from NMF. Formation of the DMF metabolite N-hydroxymethyl-N-methylformamide (HMMF) in incubations with rat liver microsomes was elevated by 200% following pretreatment of animals with acetone. Co-incubation with DEDTC (100μM) inhibited HMMF generation from DMF by 88% . Co-incubation of DMF (10mM) with NMF (1mM) inhibited the formation of SMG by 95% . A polyclonal antibody against rat CYP2E1 (10mg/nmol P-450) inhibited generation of HMMF in incubates with rat and human liver microsomes by 68.4% and 67.5% , respectively. Purified rat CYP2E1 catalysed the generation of HMMF from DMF. Using ionspray tandem mass spectrometry the glutathione conjugate SMG was identified as a biliary metabolite of DMF in rats (0.003% of a dose of 5OOmg/kg DMF i.p.). Formation of this metabolite was increased five fold after induction of CYP2E1 by acetone, and was inhibited to 20% of control values following pretreatment with disulfrram. Generation of SMG from DMF in vivo was shown to exhibit a large kinetic deuterium isotope effect (KHKD=10.1 ± 1.3), which most likely represents the product of 2 discrete isotope effects on N-demethylation and formyl oxidation reactions.

Computationsl modelling of dimethyl ether separation and steam reforming in fluidized bed reactors

This study presents a computational fluid dynamic (CFD) study of Dimethyl Ether (DME) gas adsorptive separation and steam reforming (DME-SR) in a large scale Circulating Fluidized Bed (CFB) reactor. The CFD model is based on Eulerian-Eulerian dispersed flow and solved using commercial software (ANSYS FLUENT). Hydrogen is currently receiving increasing interest as an alternative source of clean energy and has high potential applications, including the transportation sector and power generation. Computational fluid dynamic (CFD) modelling has attracted considerable recognition in the engineering sector consequently leading to using it as a tool for process design and optimisation in many industrial processes. In most cases, these processes are difficult or expensive to conduct in lab scale experiments. The CFD provides a cost effective methodology to gain detailed information up to the microscopic level. The main objectives in this project are to: (i) develop a predictive model using ANSYS FLUENT (CFD) commercial code to simulate the flow hydrodynamics, mass transfer, reactions and heat transfer in a large scale dual fluidized bed system for combined gas separation and steam reforming processes (ii) implement a suitable adsorption models in the CFD code, through a user defined function, to predict selective separation of a gas from a mixture (iii) develop a model for dimethyl ether steam reforming (DME-SR) to predict hydrogen production (iv) carry out detailed parametric analysis in order to establish ideal operating conditions for future industrial application. The project has originated from a real industrial case problem in collaboration with the industrial partner Dow Corning (UK) and jointly funded by the Engineering and Physical Research Council (UK) and Dow Corning. The research examined gas separation by adsorption in a bubbling bed, as part of a dual fluidized bed system. The adsorption process was simulated based on the kinetics derived from the experimental data produced as part of a separate PhD project completed under the same fund. The kinetic model was incorporated in FLUENT CFD tool as a pseudo-first order rate equation; some of the parameters for the pseudo-first order kinetics were obtained using MATLAB. The modelling of the DME adsorption in the designed bubbling bed was performed for the first time in this project and highlights the novelty in the investigations. The simulation results were analysed to provide understanding of the flow hydrodynamic, reactor design and optimum operating condition for efficient separation. Bubbling bed validation by estimation of bed expansion and the solid and gas distribution from simulation agreed well with trends seen in the literatures. Parametric analysis on the adsorption process demonstrated that increasing fluidizing velocity reduced adsorption of DME. This is as a result of reduction in the gas residence time which appears to have much effect compared to the solid residence time. The removal efficiency of DME from the bed was found to be more than 88%. Simulation of the DME-SR in FLUENT CFD was conducted using selected kinetics from literature and implemented in the model using an in-house developed user defined function. The validation of the kinetics was achieved by simulating a case to replicate an experimental study of a laboratory scale bubbling bed by Vicente et al [1]. Good agreement was achieved for the validation of the models, which was then applied in the DME-SR in the large scale riser section of the dual fluidized bed system. This is the first study to use the selected DME-SR kinetics in a circulating fluidized bed (CFB) system and for the geometry size proposed for the project. As a result, the simulation produced the first detailed data on the spatial variation and final gas product in such an industrial scale fluidized bed system. The simulation results provided insight in the flow hydrodynamic, reactor design and optimum operating condition. The solid and gas distribution in the CFB was observed to show good agreement with literatures. The parametric analysis showed that the increase in temperature and steam to DME molar ratio increased the production of hydrogen due to the increased DME conversions, whereas the increase in the space velocity has been found to have an adverse effect. Increasing temperature between 200 oC to 350 oC increased DME conversion from 47% to 99% while hydrogen yield increased substantially from 11% to 100%. The CO2 selectivity decreased from 100% to 91% due to the water gas shift reaction favouring CO at higher temperatures. The higher conversions observed as the temperature increased was reflected on the quantity of unreacted DME and methanol concentrations in the product gas, where both decreased to very low values of 0.27 mol% and 0.46 mol% respectively at 350 °C. Increasing the steam to DME molar ratio from 4 to 7.68 increased the DME conversion from 69% to 87%, while the hydrogen yield increased from 40% to 59%. The CO2 selectivity decreased from 100% to 97%. The decrease in the space velocity from 37104 ml/g/h to 15394 ml/g/h increased the DME conversion from 87% to 100% while increasing the hydrogen yield from 59% to 87%. The parametric analysis suggests an operating condition for maximum hydrogen yield is in the region of 300 oC temperatures and Steam/DME molar ratio of 5. The analysis of the industrial sponsor’s case for the given flow and composition of the gas to be treated suggests that 88% of DME can be adsorbed from the bubbling and consequently producing 224.4t/y of hydrogen in the riser section of the dual fluidized bed system. The process also produces 1458.4t/y of CO2 and 127.9t/y of CO as part of the product gas. The developed models and parametric analysis carried out in this study provided essential guideline for future design of DME-SR at industrial level and in particular this work has been of tremendous importance for the industrial collaborator in order to draw conclusions and plan for future potential implementation of the process at an industrial scale.

Adsorption of dimethyl ether (DME) on zeolite molecular sieves

In recent years there has been growing interest in the use of dimethyl ether (DME) as an alternative fuel. In this study, the adsorption of DME on molecular sieves 4Å (Mol4A) and 5Å (Mol5A) has been experimentally investigated using the volumetric adsorption method. Data on the adsorption isotherms, heats of adsorption, and adsorption kinetic have been obtained and used to draw conclusions and compare the performance of the two adsorbents. Within the conditions considered, the adsorption capacity of Mol5A was found to be around eight times higher than the capacity of Mol4A. Low temperature adsorption and thermal pre-treatment of the adsorbents in vacuum were observed to be favourable for increased adsorption capacity. The adsorption isotherms for both adsorbent were fitted to the Freundlich model and the corresponding model parameters are proposed. The adsorption kinetic analysis suggest that the DME adsorption on Mol5A is controlled by intracrystalline diffusion resistance, while on Mol4A it is mainly controlled by surface layering resistance with the diffusion only taking place at the start of adsorption and for a very limited short time. The heats of adsorption were calculated by a calorimetric method based on direct temperature measurements inside the adsorption cell. Isosteric heats, calculated by the thermodynamic approach (Clasius-Clapeyron equation), have consistently shown lower values. The maximum heat of adsorption was found to be 25.9kJmol-1 and 20.1kJmol-1 on Mol4A and Mol5A, respectively; thus indicating a physisorption type of interactions. © 2014 Elsevier B.V.

Hot-spots during the calcination of MCM-41:a SAXS comparative analysis of a soft mesophase

The phenomenon of microscopic hot-spots, during the calcination of MCM-41, was investigated by quantifying the magnitude of the temperature increase during the calcination of a soft MCM-41 mesophase using a SAXS comparative study. This was performed by thermally treating a soft material that was detemplated via Fenton chemistry followed by equilibrating and drying in a low-surface-tension solvent (n-butanol or N,N-dimethylformamide); these samples have limited structural shrinkage. The resulting samples were thermally treated at increasing temperatures, and the structural shrinkage was compared with that of the directly calcined material. By comparing the structural shrinkage, it was found that the microscopic temperature increase would fall between 190 and 250 C, as deduced from N,N-dimethyl-formamide and n-butanol. The order of magnitude of the temperature increase appears to be consistent with the well-known glow effect. It is, however, substantially higher than the experimentally determined macroscopic temperature increase. Several aspects are discussed to interpret this difference. © 2013 Elsevier B.V.

A computational model of hydrogen production by steam reforming of dimethyl ether in a large scale CFB reactor. Part II:parametric analysis

This study presents a computational parametric analysis of DME steam reforming in a large scale Circulating Fluidized Bed (CFB) reactor. The Computational Fluid Dynamic (CFD) model used, which is based on Eulerian-Eulerian dispersed flow, has been developed and validated in Part I of this study [1]. The effect of the reactor inlet configuration, gas residence time, inlet temperature and steam to DME ratio on the overall reactor performance and products have all been investigated. The results have shown that the use of double sided solid feeding system remarkable improvement in the flow uniformity, but with limited effect on the reactions and products. The temperature has been found to play a dominant role in increasing the DME conversion and the hydrogen yield. According to the parametric analysis, it is recommended to run the CFB reactor at around 300 °C inlet temperature, 5.5 steam to DME molar ratio, 4 s gas residence time and 37,104 ml gcat -1 h-1 space velocity. At these conditions, the DME conversion and hydrogen molar concentration in the product gas were both found to be around 80%.