Evaluation of ADA, IL-6 and TNF-alpha level in type 2 diabetes mellitus: with -and without hypoglycemic drugs.

Diabetes mellitus(DM) is a major worldwide  health problem leading to markedly increase mortality and serious morbidity. Immunological disturbances involving the cell mediated immune system and improper T-lymphocyte function also contribute to the path physiology of type 2 DM.It has been reported that ADA,IL-6,and TNF-α levels  were a good marker for immunological disturbance in type 2 DM  patients.This study aims to assess and compare the level of serum ADA, IL-6 ,and TNF-α in patient of type 2 DM with and without oral hypoglycamic drugs.The study population consist of 150 subjects divided in to 3 groups:group I (50normal health controls),group II (45 type 2 DM patients with no on hypoglycemic drugs),and group Ш (55 type 2 DM patients on hypoglycemic drugs).There were a significant(p<0.001) tremendous increase in ADA,IL-6,and TNF-α levels (47.32 U/L ,29.04 pg/ml ,and 98.23 pg/ml, respectively ) in group II  than group I and group Ш. also, ADA,IL-6,and TNF-α levels were significantly(p<0.001) higher in group Ш than group I.As conclusion ,the increase in ADA,IL-6,and TNF-α levels  is a good glycemic  markers associated with type 2 DM .The intake of hypoglycaemic drugs  decrease the levels of these markers. Key words: ADA activity , IL-6 , TNF-α , type 2 diabetes mellitus

Trends in Minimizing and Treating Industrial Wastes for Sustainable Environment

While treating the industrially produced wastes through various processes such as physical, chemical, biological and radiation processes have been implemented on various scales and is the focus of various studies and development, the trend of minimizing and/or eliminating the pollutions at the source via developing and selecting proper catalytic multiphase reactors is worth to be given proper attention and consideration which is the focus of this manuscript beside outlining the processes used for treating the wastes. In order to achieve such goal in minimizing the wastes, these multiphase reactors must be well understood, studied, scaled up and designed. This can be only achieved by developing and implementing advanced measurement and computing techniques which have been developed in our research laboratory and are briefly outlined here with selected results

Flow regime identification in fluidized beds by analysing pressure fluctuations signal based on kolomogrov entropy approch

The investigation of flow regime in gas-solid fluidized bed reactors is very important for their design and scale-up as well as effective operation. In addition, the degrees of mixing, mass and heat transfer in these reactors depending strongly on the common flow regime. In the present work, pressure transducer technique has been used to generate pressure fluctuations signal in gas-solid fluidized bed of 13.97 cm ID. Different static bed heights, different particles size and particles density of both Geldart A and B as well as a range of superficial gas velocity (15-100) cm/s have been used to study the flow regime identification. The Kolmogorov entropy (KE) approach analysis has been applied to pressure fluctuations signal recorded in fluidized bed. The (KE) is considered as a universal tool for the accurate identification of the boundaries of the main hydrodynamic regimes in multiphase reactors. It has been shown that this approach leads to successful identification of the main flow regimes in fluidized bed reactors with different operating conditions. REFERENCES 1- Nedeltchev, S., Aradhya, S., Zaid, F., & Al-Dahhan, M. (2012). Flow regime identification in three multiphase reactors based on Kolmogorov entropies derived from gauge pressure fluctuations. Journal of Chemical Engineering of Japan, 45(9), 757-764. 2- Nedeltchev, S. (2015). New methods for flow regime identification in bubble columns and fluidized beds. Chemical Engineering Science, 137, 436-446. 3- Nedeltchev, S., Ahmed, F., & Al-Dahhan, M. (2012). A new method for flow regime identification in a fluidized bed based on gamma-ray densitometry and information entropy. Journal of chemical engineering of Japan, 45(3), 197-205. 4- Johnsson, F., Zijerveld, R. C., Schouten, J. C., Van den Bleek, C. M., & Leckner, B. (2000). Characterization of fluidization regimes by time-series analysis of pressure fluctuations. International journal of multiphase flow, 26(4), 663-715. 5- Bi, H. T. (2007). A critical review of the complex pressure fluctuation phenomenon in gas–solids fluidized beds. Chemical Engineering Science,62(13), 3473-3493. 6- van Ommen, J. R., Sasic, S., Van der Schaaf, J., Gheorghiu, S., Johnsson, F., & Coppens, M. O. (2011). Time-series analysis of pressure fluctuations in gas–solid fluidized beds–A review. International Journal of Multiphase Flow,37(5), 403-428. 7- Nedeltchev, S., Jordan, U., Lorenz, O., & Schumpe, A. (2007). Identification of various transition velocities in a bubble column based on Kolmogorov entropy.Chemical engineering & technology, 30(4), 534-539. 8- Nedeltchev, S., Shaikh, A., & Al‐Dahhan, M. (2011). Flow regime identification in a bubble column via nuclear gauge densitometry and chaos analysis.Chemical engineering & technology, 34(2), 225-233. Muzen, A., & Cassanello, M. C. (2007). Flow regime transition in a trickle bed with structured packing examined with conductimetric probes. Chemical engineering science, 62(5), 149

GAS PHASE MIXING IN BUBBLE COLUMNS WITH INTERNALS

The use of renewable energy sources is becoming increasingly necessary, if we are to achieve the changes required to address the impacts of global warming. Biomass is the most common form of renewable energy, widely used in the third world but until recently, less so in the Western world. Latterly much attention has been focused on the conversion of biomass to liquid fuels; a process which would greatly increases the potential usefulness of biomass as a renewable resource. Conversion of biomass to liquid is carried out by first gasification of biomass to yield synthetic gas. The synthetic gas can then be converted to liquid fuels using Fischer Tropsch process or transformed to methanol for subsequent use as a chemical, solvent or fuel. For large-scale FT / methanol synthesis the slurry bubble column reactor is the best choice. These reactors offer high conversion and high volumetric productivity when operated in the heterogeneous or churn turbulent regime. Notwithstanding the presence of large diameter bubbles and their short residence time in the liquid, gas–liquid mass transfer is quite fast in this regime due to the effective interaction between bubbles of various sizes. However, despite the simple construction and operation of bubble columns, their scale-up is very difficult due to complex interrelations among the many parameters that determine the behavior of bubble columns. In addition the complexity increases with the presence of cooling internals that affect the hydrodynamics and mixing behavior in bubble columns. Gas phase backmixing is one of the important hydrodynamic parameters to be considered in the scale-up of bubble columns as it can adversely affect the reaction rates and product selectivity. The present investigation focuses on studying the effect of the cooling internals on gas phase mixing behavior. The percentage of internals used in this study is the same percentage used industrially for methanol synthesis (5 % internals) and FT synthesis (25% internals)

Mixing characteristics of bubble columns with internals for Biomass to liquid synthesis [abstract]

Only abstract of poster available.Track II: Transportation and BiofuelsThe use of renewable energy sources is becoming increasingly necessary, if we are to achieve the changes required to address the impacts of global warming. Biomass is the most common form of renewable energy, widely used in the third world but until recently, less so in the Western world. Latterly much attention has been focused on the conversion of biomass to liquid fuels; a process which would greatly increases the potential usefulness of biomass as a renewable resource. Conversion of biomass to liquid is carried out by first gasification of biomass to yield synthetic gas. The synthetic gas can then be converted to liquid fuels using Fischer Tropsch process or transformed to methanol for subsequent use as a chemical, solvent or fuel. For large-scale FT / methanol synthesis the slurry bubble column reactor is the best choice. These reactors offer high conversion and high volumetric productivity when operated in the heterogeneous or churn turbulent regime. Notwithstanding the presence of large diameter bubbles and their short residence time in the liquid, gas-liquid mass transfer is quite fast in this regime due to the effective interaction between bubbles of various sizes. However, despite the simple construction and operation of bubble columns, their scale-up is very difficult due to complex interrelations among the many parameters that determine the behavior of bubble columns. In addition the complexity increases with the presence of cooling internals that affect the hydrodynamics and mixing behavior in bubble columns. Gas phase backmixing is one of the important hydrodynamic parameters to be considered in the scale-up of bubble columns as it can adversely affect the reaction rates and product selectivity. The present investigation focuses on studying the effect of the cooling internals on gas phase mixing behavior. The percentage of internals used in this study is the same percentage used industrially for methanol synthesis (5 % internals) and FT synthesis (25% internals)

Liquid Phase Mixing in Trayed Bubble Column Reactors

The Compartmentalization of Conventional Bubble Columns by Perforated Trays Constitutes a Very Effective Method to Reduce the Liquid Back mixing. the Effect of Tray Design and Operating Conditions on the overall Liquid Mixing Was Studied in a Bench-Scale Trayed Bubble Column. the Extent of Liquid Back mixing in the Column Was Investigated in Light of Liquid-Phase Tracer Response Experiments. in Average, a Three-Fold Reduction in the Liquid Back mixing Was Achieved in the Trayed Column as Compared to the Column Without the Trays. Moreover, the Tray Open Area and the Superficial Liquid Velocity Were Found to Have the Strongest Effects on the Liquid Back mixing. the N-CSTR with Back mixing Model Was Found to Match the Experimental Tracer Response Curves Better Than the Axial Dispersion Model. © 2005 Elsevier Ltd. All Rights Reserved

Gas-Liquid Mass Transfer in a High Pressure Bubble Column Reactor with Different Sparger Designs

The Gas-Liquid Mass Transfer in a 0.162 M High-Pressure Stainless-Steel Bubble Column Was Investigated using Three Different Gas Sparger Designs. an Oxygen-Enriched-Air Dynamic Method and an Optical Oxygen Probe Technique Were Implemented to Measure K1 a Values in the Bubble Column Reactor. using the Interfacial Area (A) Values Measured by a Four-Point Optical Probe Technique at Similar Conditions (Xue, 2004), the K1 Values Were Estimated. Axial Dispersion Model (ADM) and Continuous Stirred Tank Reactor (CSTR) Model Were Used to Calculate K1 a as a Fitted Parameter with the Measured Data. the ADM Gave Better Fits to the Experimental Data Than the CSTR Model, Especially at High Axial Locations for the Bubble Column Used with a Large L / Dc Ratio. the Sparger Design Was Found to Have a Noticeable Effect on K1 a in the Low Gas Velocity Range (Ug \u3c 0.15 M / S) But Only a Slight Effect in the High Gas Velocity Range (Ug \u3e 0.20 M / S). the Sparger Design Showed Almost No Effect on the Liquid Side Mass Transfer Coefficient, K1, at High Gas Velocity (Ug = 0.30 M / S), Where No Significant Variations of the Bubble Size Distribution and Hydrodynamics Were Obtained using Different Sparger Designs. Although the K1 a Values Increased with the Operating Pressure, the Pressure Change from 0.1 to 0.4 MPa Yielded Lower K1 Values, as a Result of the Reduced Bubble Size. However, as the Pressure Further Increased to 1.0 MPa, the a and K1 a Values Increased, While the K1 Values Negligibly Decreased. in Addition to the Pressure and Sparger Design Effects, the Superficial Gas Velocity Had Effect of Increasing the K1 Values, While Such Effect Became Small and Flattened Out at High Superficial Gas Velocities. © 2006 Elsevier Ltd. All Rights Reserved