Simultaneous saccharification and extractive fermentation of lignocellulosic materials into lactic acid in a two-zone fermentor-extractor system

Simultaneous saccharification and extractive fermentation of lignocellulosic materials into lactic acid was investigated using a two-zone bioreactor. The system is composed of an immobilized cell reactor, a separate column reactor containing the lignocellulosic substrate and a hollow-fiber membrane. It is operated by recirculating the cell free enzyme (cellulase) solution from the immobilized cell reactor to the column reactor through the membrane. The enzyme and microbial reactions thus occur at separate locations, yet simultaneously. This design provides flexibility in reactor operation as it allows easy separation of the solid substrate from the microorganism, in situ removal of the product and, if desired, different temperatures in the two reactor sections. This reactor system was tested using pretreated switchgrass as the substrate. It was operated under a fed-batch mode with continuous removal of lactic acid by solvent extraction. The overall lactic acid yield obtainable from this bioreactor system is 77% of the theoretical.     

阴极冷却反应器电合成乙醛酸

以过饱和草酸水深液为阴极液 ,盐酸溶液为阳极液 ,在阴极冷却电化学反应器内草酸电解合成乙醛酸 .考察了电极温度、电解液温度、电流密度和电极材料对合成乙醛酸的时空产率和电流效率的影响 .结果表明 ,阴极冷却反应器既节省能耗 ,又可使电解过程在较高草酸浓度下进行 ,提高电流效率和时空产率 .用石墨板做阳极 ,铅做阴极 ,电流密度为 4 0 9.4 6A·m-2 ,阴极液流速 μ=1 .0 8m·s-1,电解温度为 2 0℃左右时 ,电解 3 .70h ,可得到质量分数为 3 .52 %的乙醛酸溶液 ,平均时空产率为 0 .0 3 2kg·dm-3·h     

阴极冷却固定床电合成乙醛酸的连续过程模拟

联用反应动力学、电荷衡算和物料衡算建立阴极冷却固定床草酸电合成乙醛酸反应器模型方程.针对反应器连续化操作过程,用正交配置法数值求解该模型方程.结果表明,在连续化操作的反应初期,反应液中的乙醛酸能够较快地达到预定浓度,但继续增加反应器的长度,反应的效果不明显.该模型还模拟了分段温控和部分回流对反应的影响.结果表明,分段温控和部分回流均可较好地提高乙醛酸在阴极液中的浓度.计算结果与试验操作基本相符.该结果对阴极冷却固定床草酸电合成乙醛酸的连续化操作工艺和反应器的优化具有重要的参考意义.     

Modeling of a continuous pretreatment reactor using computational fluid dynamics

Computational fluid dynamic simulations are employed to predict flow characteristics in a continuous auger driven reactor designed for the dilure acid pretreatment of biomass. Slurry containing a high concentration of biomass solids exhibits a high viscosity, which poses unique mixing issues within the reactor. The viscosity increases significantly with a small increase in solids concentration and also varies with temperature. A well-mixed slurry is desirable to evenly distribute acid on biomass, prevent buildup on the walls of the reactor, and provides an uniform final product. Simulations provide flow patterns obtained over a wide range of viscosities and pressure distributions, which may affect reaction rates. Results provide a tool for analyzing sources of inconsistencies in product quality and insight into future design and operating parameters.     

Initial design of a dilute sulfuric acid pretreatment process for aspen wood chips

A preliminary process design for dilute sulfuric acid pretreatment of aspen wood chips in order to obtain fermentable sugars has been prepared and subjected to an economic evaluation. The process design was prepared according to experimental data on the kinetics of dilute sulfuric acid prehydrolysis and particle size effects obtained in this study and our previous work. The initial economic evaluation shows woodchips are 56% of the cost of production, whereas the reactor is only 4%, and the comminution operation is just under 10%, indicating that the process economics are extremely vulnerable to feedstock costs and are thus yield-sensitive. Although chances for major cost improvements by modification of the reactor design and finding alternatives to dry milling of aspen chips to small (20–80 mesh) particles needed for acid penetration and enzymatic saccharification are not great, design improvements of the process will necessitate development of a cheaper acid resistant pretreatment reactor and a less energy intensive comminution system. Experimental results on effects of particle size on the dilute acid pretreatment design are presented.     

Selective Oxidation of Propane by Lattice Oxygen of Vanadium-Phosphorous Oxide in a Pulse Reactor

Selective oxidation of propane by lattice oxygen of vanadium-phosphorus oxide (VPO) catalysts was investigated with a pulse reactor in which the oxidation of propane and the re-oxidation of catalyst were implemented alternately in the presence of water vapor. The principal products are acrylic acid (AA),acetic acid (HAc), and carbon oxides. In addition, small amounts of C1 and C2 hydrocarbons were also found, molar ratio of AA to HAc is 1.4-2.2. The active oxygen species are those adsorbed on catalyst surface firmly and/or bound to catalyst lattice, i.e. lattice oxygen; the selective oxidation of propane on VPO catalysts can be carried out in a circulating fluidized bed (CFB) riser reactor. For propane oxidation over VPO catalysts, the effects of reaction temperature in a pulse reactor were found almost the same as in a steady-state flow reactor. That is, as the reaction temperature increases, propane conversion and the amount of C1 C2 hydrocarbons in the product increase steadily, while selectivity to acrylic acid and to acetic acid increase prior to 350℃ then begin to drop at temperatures higher than 350℃, and yields of acrylic acid and of acetic acid attained maximum at about 400℃. The maximum yields of acrylic acid and of acetic acid for a single-pass are 7.50% and 4.59% respectively, with 38.2% propane conversion. When theamount of propane pulsed decreases or the amount of catalyst loaded increases, the conversion increases but the selectivity decreases. Increasing the flow rate of carrier gases causes the conversion pass through a minimum but selectivity and yields pass through a maximum. In a fixed bed reactor, it is hard to obtainhigh selectivity at a high reaction conversion due to the further degradation of acrylic acid and acetic acid even though propane was oxidized by the lattice oxygen. The catalytic performance can be improved inthe presence of excess propane. Propylene can be oxidized by lattice oxygen of VPO catalyst at 250℃, nevertheless, selectivity to AA and to HAc are even lower, much more acetic acid was produced (molar ratio of AA to HAc is 0.19:1-0.83:1) though the oxidation products are the same as from propane.     

A flow-injection system based on immobilized penicillinase and a linear pH-buffer for potentiometric determination of penicillin

Penicillin is determined in a flow-injection manifold by hydrolysis of the β-lactam ring by means of an on-line reactor containing immobilized penicillinase with detection of the produced acid by a glass electrode. The penicillin concentration is calculated as the difference in response between a sample passing through the enzyme reactor and a sample flowing directly to the glass electrode. The pH signal is made linearly dependent on the acid concentration by using a buffer mixture of constant buffer capacity and the reactor is designed so that hydrolysis of the penicillin is essentially complete in the reactor. The linear range is 0.1–15 mM penicillin and the sensitivity is 0.056 pH mM^?1. The sample throughput is 60 h^?1 and the relative standard deviation < 1%. The proposed method is primarily intended for the analysis of purified potassium salts of penicillins in pharmaceutical preparations.     

Use of computational fluid dynamics simulations for design of a pretreatment screw conveyor reactor

Computational fluid dynamics simulations were employed to compare performance of various designs of a pretreatment screw conveyor reactor. The reactor consisted of a vertical screw used to create cross flow between the upward conveying solids and the downward flow of acid. Simulations were performed with the original screw design and a modified design in which the upper flights of the screw were removed. Results of the simulations show visually that the modified design provided favorable plug flow behavior within the reactor. Pressure drop across the length of the reactor without the upper screws in place was predicted by the simulations to be 5 vs 40 kPa for the original design.     

An acidic layered clay is combined with a basic layered clay for one-pot sequential reactions

A Ti4+-exchanged montmorillonite (Ti4+-mont) and a hydrotalcite (HT) are strong solid Br?nsted acid and base, and these two clay catalysts could be used in a single reactor without neutralization of active sites. Because the Ti4+-mont have active acid site in the narrow interlayers, the base sites of large HT particles show no interaction with the acid sites. A variety of acid and base reactions, such as esterification, acetalization, deacetalization, aldol reaction, Michael reaction, and epoxidation, proceeded using both the Ti4+-mont and the HT in a single reactor.     

草酸电解合成乙醛酸连续化工艺研究

针对传统草酸电解生产乙醛酸工艺只能间歇循环的缺陷,本文提出模拟连续化实验方案,并分别设计阴极冷却反应器和阴极冷却固定床反应器,探讨连续化实验的可行性.另外还考察了草酸饱和度和温度工艺参数对反应的影响.实验表明,保持草酸过饱和和利用变温操作可在反应停留时间(30m in)内于连续化反应过程中得到分别含有3.76%和3.66%乙醛酸的反应液,因此阴极冷却固定床反应器可望实现草酸电解还原乙醛酸的连续化生产.     

Polymeric substitution in a pH oscillator

The iodate pH oscillator, which oscillates between pH 6.5 and 4.0, is reproducible in a semibatch reactor. pH oscillations of similar period and amplitude were observed when poly(2-acrylamido-2-methyl-1-propanesulfonic acid) was substituted for sulfuric acid. Therefore, a polymer may be used as an alternative reagent, where the polymer actively participates in the reaction instead of serving as an inert reaction medium.     

Uric acid determination using an aldehyde dehydrogenase and a uricase-aldehyde dehydrogenase nylon-tube reactor

Summary The preparation of a coimmobilized uricase-aldehyde dehydrogenase nylon-tube reactor is described and the reactor is characterized. Routine estimation of uric acid by use of a continuous-flow system can be performed with either an aldehyde dehydrogenase nylon-tube reactor aided by catalase and uricase in solution or a uricase-aldehyde dehydrogenase coupled-enzyme reactor, with only catalase in solution. The methods have been rigorously tested by inter-method comparison, precision analysis, recovery, interferences, and cofactor requirement. More than 5000 tests can be carried out with one coupled-enzyme reactor, which reduces the cost of enzymes in analysis to a negligible amount.Part of this paper was presented as poster at the Tagung für Biochemische Analytik, Munich 1980. [Abstract in this Journal 301, 161 (1980)]     

Microwave heating of heterogeneously catalysed Suzuki reactions in a micro reactor

The Suzuki cross-coupling reaction of aryl halides with phenylboronic acid to form biaryls has been used to illustrate the development of a microwave based technique capable of delivering heat locally to a heterogeneous Pd-supported catalyst located within a micro reactor device. A 10-15 nm gold film patch, located on the outside surface of the base of a glass micro reactor, was found to efficiently assist in the heating of the catalyst when irradiated with 5-7 W of microwave power at 2.45 GHz. Using a hydrodynamically pumped system, reactant-catalyst contact times of less than 60 s were found to give conversions for different substrates which were in the range 50-99%. Two methods of loading catalysts into the micro reactor were investigated which required either 1.5 or 6 mg of material.     

Determination of fructosyl amino acids and fructosyl peptides in protease-digested blood sample by a flow-injection system with an enzyme reactor.

A flow-injection system with an enzyme reactor was proposed for the measurement of fructosyl amino acids and fructosyl peptides in protease-digested blood samples. A fructosyl-amino acid oxidase (FAOX-TE) and two fructosyl-peptide oxidases (FPOX-CE and FPOX-CET) were covalently immobilized onto an inert support. They were used as the enzyme reactor in a FIA system with a hydrogen peroxide electrode. In particular, the FPOX-CET reactor possessed high selectivity for the detection of fructosyl valine (FV) and fructosyl valyl histidine (FVH) and an excellent operational stability. The proposed FIA system with the FPOX-CET reactor responded linearly to the concentration of FV over the dynamic range of 7.8 x 10(-6) to 5.8 x 10(-4) M. The present method could be successfully applied to the assay of FV and FVH in the protease-digested blood samples.     

固定床反应器电合成乙醛酸的研究

以过饱和草酸水溶液为阴极液 ,盐酸为阳极液 ,在固定床电解槽中草酸电还原得到乙醛酸 .考察改变固定床的结构、电解温度及电流密度对生成乙醛酸电流效率和产率的影响 .结果表明 ,以铅粒作阴极 ,石墨板作阳极 ,电流密度 96 .3A·m- 2 ,阴极液空速 0 .5 0 5m·s- 1,电解温度 32℃时 ,在固定床双阳极室内反应 4 5min ,乙醛酸的电流效率仍达到 6 6 .2 % ,浓度 2 .0 2 %     

多相酶膜反应器合成生物活性二肽

生物活性肽;多相酶膜反应器合成生物活性二肽     

Chemiluminescence biosensor chip based on a microreactor using carrier air flow for determination of uric acid in human serum

A chemiluminescence biosensor on a chip coupled to a microfluidic system and a microreactor is described in this paper. The chemiluminescence biosensor measured 25 x 75 x 6.5 mm in dimension, and was readily produced in an analytical laboratory. The sol-gel method is introduced to co-immobilize horseradish peroxidase (HRP) and luminol in the microreactor, and to immobilize uricase in the enzymatic reactor. The main characteristic of the biosensor was to introduce air as the carrier flow instead of the more common solution carrier for the first time. The uric acid was determined by a chemiluminescent (CL) reaction between the hydrogen peroxide produced from the enzymatic reactor and luminol under the catalysis of HRP in the microreactor. The linear range of the uric acid concentration was 1 to 100 mg L(-1) and the detection limit was 0.1 mg L(-1) (3sigma).     

Potentiometric determination of glucose by enzymatic oxidation in a flow system

A potentiometric determination is described for glucose based on oxidation by 1,4-benzoquinone with immobilized glucose oxidase as catalyst in an enzyme reactor. The electrode is preceded by an analytical dialysis unit to remove proteins. The ratio of quinone to hydroquinone was measured with a flow-through gold electrode. Another gold electrode preceded the enzyme reactor to correct for serum components (e.g. ascorbic acid) which can also reduce quinone. The operating range is 0.04–10 × 10^-3 M β-D-glucose. The dialysis proceeds with a linear dependence on glucose concentration, and the dialysis ratio can be adjusted by changing the buffer flow rate.     

Determination of rate constants by a double-line flow injection method incorporating a well-stirred tank reactor

Equations have been derived for the concentration-time profiles of reactants and products in a first order reaction obtained on passage of a reactant plug through a single well-stirred tank reactor. When taken together with the equations for physical dispersion of such a reactor under plug flow conditions, an expression for the reaction rate constant was derived which allowed its experimental determination in a relatively simple fashion. The method was tested for reactions between cerium and oxalic acid and between dichromate and ascorbic acid, for which values of the rate constants of around 2 x 10(2) sec(-1) and 5.5 x 10(3) sec(-1) were obtained. Good agreement with other experimentally determined values was obtained. The scope and the limitations of the proposed method are critically discussed with the aid of some model calculations. The range of values for which the method might be suitable is approximately 10(-3)-10(-1) sec(-1). An equation analogous to a peak-width equation was derived as a further development of this approach. Good agreement with the previously determined values were obtained for both systems. The extension of the method to reactions other than first order is discussed.