Gas holdup in three-phase immobilized-cell bioreactors

A number of studies in the published literature deal with gas holdup in three-phase reactors. However, very few address the cases in which the solid density approaches that of the liquid phases and in which low gas velocities are involved. These conditions are commonly encountered in immobilized-cell bubble columns and in fluidized-bed bioreactors. This paper reports the effect of gas and liquid velocity upon gas holdup and bed expansion in fluidized-bed bioreactors. For liquid-fluidization of low-density alginate beads in the absence of gas, the terminal sedimentation velocity (vT) of the particles is a constant, and expansion of the bed follows Richardson and Zaki’s correlation. In the presence of gas, however, the apparent terminal sedimentation velocity value is affected by the velocity of the gas and liquid phases. For gas velocities above a minimum value, the calculated value of vT depends on liquid velocity only, and a constant bed expansion was observed for a range of gas and liquid flow rates. For the gas-liquid interactions, a modified drift-flux model was found to be valid. For superficial gas velocities between 5 and 17 cm/min, the modified drift-flux velocity was observed to be a function of gas velocity, suggesting the prevalence of a coalescence regime.     

Enantioseparation of 1-phenyl-1-propanol by supercritical fluid-simulated moving bed chromatography

The enantioseparation of 1-phenyl-1-propanol through the supercritical fluid-simulated moving bed (SF-SMB) process is studied. Non-linear isotherms were measured on an analytical column, and used together with the triangle theory for SMB design to select operating conditions for the SF-SMB. Experiments were carried out on a pilot-scale SF-SMB plant at conditions that corresponded to the non-linear range of the isotherm. Under conditions of low feed concentration, complete separation (extract purity = 99.5%; raffinate purity = 98.4%) was achieved. Under conditions of larger feed concentration, the best separation corresponded to an extract purity of 98.0% and a raffinate purity of 94.0%, and yielded a productivity of 110 g of racemate per kg stationary phase per day.     

Modeling, Simulation and Operation Performance of a Simulated Moving Bed for Enantioseparation of Fluoxetine on New β-Cyclodextrin Columns

A Simulated Moving Bed (SMB) setup, including 8 new -cyclodextrin columns, was used to achieve the enantioseparation of fluoxetine. The effects of feed concentration and feed flowrate on the operation performance parameters: purity, enrichment, recovery and productivity were studied. A simulation approach was applied to simulate the operation and performance of the simulated counter-current system. The model predicted the performance of the transient and cyclic steady state behaviour to a reasonably good extent. The adsorption isotherm and parameters determined by pulse experiments and moment analysis seem to be adequate in simulating both the transient and steady state behaviour. Generally, this model can provide guidance for designing operation condition of the SMB system.     

Continuous production of butanol by clostridium acetobutylicum immobilized in a fibrous bed bioreactor

We explored the influence of dilution rate and pH in continuous cultures of Clostridium acetobutylicum. A 200-mL fibrous bed bioreactor was used to produce high cell density and butyrate concentrations at pH 5.4 and 35°C. By feeding glucose and butyrate as a cosubstrate, the fermentation was maintained in the solventogenesis phase, and the optimal butanol productivity of 4.6g/(L h) and a yield of 0.42 g/g were obtained at a dilution rate of 0.9h⁻¹ and pH 4.3. Compared to the conventional acetone-butanol-ethanol fermentation, the new fermentation process greatly improved butanol yield, making butanol production from corn an attractive alternative to ethanol fermentation.     

INVERSE RESPONSE BEHAVIOR OF FIXED-BED REACTOR IN A FISCHER-TROPSCH SYNTHESIS

研究了固定床ＦＴ合成反应器中的动态响应行为。主要研究了当反应器进口气体温度突降后床层中出现的逆响应现象，并探讨了水煤气变换副反应对固定床ＦＴ合成反应器逆响应行为的影响。     

影响混床出水水质因素的研究

混床再生剂的纯度和阴、阳树脂的混合程度会严重影响到混床出水水质.用高纯碱替代工业碱再生混床的阴树脂;采用反常规均粒混床树脂;对混床树脂采用特殊的再生和输送方法等措施均可提高出水水质.     

Mathematical Simulation and Design of Three-Phase Bubble Column Reactor for Direct Synthesis of Dimethyl Ether from Syngas

A three-phase reactor mathematical model was set up to simulate and design a three-phase bubble column reactor for direct synthesis of dimethyl ether (DME) from syngas, considering both the influence of part inert carrier backmixing on transfer and the influence of catalyst grain sedimentation on reaction. On the basis of this model, the influences of the size and reaction conditions of a 100000 t/a DME reactor on capacity were investigated. The optimized size of the 10000 t/a DME synthesis reactor was proposed as follows: diameter 3.2 m, height 20 m, built-in 400 tube heat exchanger (φ38×2 mm), and inert heat carrier paraffin oil 68 t and catalyst 34.46 t. Reaction temperature and pressure were important factors influencing the reaction conversion for different size reactors. Under the condition of uniform catalyst concentration distribution, higher pressure and temperature were proposed to achieve a higher production capacity of DME. The best ratio of fresh syngas for DME synthesis was 2.04.     

Simulated moving bed technology: old and new

The Simulated Moving Bed (SMB) concept has been applied to the separation of different mixtures as a continuous counter current separation process, avoiding several problems related with solid motion. The aim of this work is to present some relevant examples of SMB separations corresponding to the two major ages in the use of the SMB concept, here named “old” and “new” applications. The “old” applications of SMB technology in the petrochemical industry are still important, with large and highly productive units; and the “new” applications of the second “age” of SMB concept are from the fine chemical, pharmaceutical and biochemistry areas, associated with the demand of high purity products during the last 10 years. Different examples are presented for different ages: a UOP Parex ^® process for the “old”, modelled with the equivalent True Moving Bed (TMB) approach; and a chiral resolution for the “new”, modelled by the real SMB model. Some of the latest developments are also mentioned: the non conventional techniques as the Varicol ^® process, PowerFeed, Modicon, M3C or Enriched Extract-SMB (EE-SMB), MultiFeed (MF), Outlet Streams Swing (OSS) or Pseudo-SMB, involving considerable changes in the SMB concept itself. The use of the last optimization/modelling packages for the development of design techniques, either at the conception stage as well as for performance improvements of existing units is emphasized.     

Design of a fluidized bed reactor for microencapsulated urease

A fluidized bed reactor was designed, constructed, and tested for handling microencapsulated urease. The working volume of the reactor was 10 mL, with a minimum fluidization velocity of 7.7×10⁻⁵ m/s. An even suspension of the microcapsules was obtained at fluid velocities between 1.5×10⁻⁴ and 6.0×10⁻⁴ m/s without breakage of the shear-sensitive microcapsules. The mixing behavior in the reactor was evaluated using pulse input tracer experiments and the hydrolysis rates of urea in continuous flow experiments were evaluated under various operating conditions.