This paper proposes a 2.4 GHz active MIXER without passive inductor for the transceiver system. Taking into account the design requirements of the MIXER, a double-balanced down-conversion structure with active inductor and negative resistance is designed. The proposed MIXER with 130 nm CMOS technology is designed and simulated using Cadence software at 1.5 V supply voltage. Although we had to compromise conversion gain with linearity, we were able to achieve very high conversion gain with average linearity. Based on the results of post-layout simulations, the conversion gain of 27.57 dB, IIP3 equal to -7.88 dBm, 1-dB compression point equal to -17.34 dBm and IIP2 equal to 44.22 dBm with power consumption of 2.5 mW was obtained for the proposed MIXER. The chip size without input and output pads is 95.18 µm × 117.68 µm, which leads to a chip area of 0.0112mm2.

The laminar flow pattern and mixing behavior of incompressible Newtonian fluids in different modified MIXER ‎configurations were numerically investigated using Computational Fluid Dynamics (CFD) simulations in the range of ‎Re=0. 15-100. The governing equations were solved by ANSYS Fluent 14 using the second-order finite volume method ‎‎(FVM) and the SIMPLE algorithm scheme. The computational model is assessed by comparing the predicted pressure ‎drop results to empirical correlations in the literature. The effects of incorporated helical overlapped MIXER elements and ‎the diameter aspect ratio (C) on the mixing efficiency for different MIXER geometries were examined and evaluated by ‎characteristics measures of Intensity of Segregation (IOS), pressure drop, extensional efficiency, and G-factor. The ‎performance of new modified MIXERs is evaluated via comparison with the standard industrial Kenics static MIXER. The ‎static MIXERs with modified internal geometry achieved fast mixing and better mixing quality than the Kenics MIXER. ‎Besides, an increase in diameter aspect ratio C benefited from a decrease in pressure drop within the static. The ‎modified MIXER: C=1. 5 was found to have the highest mixing efficiency, concerning short mixing length with marginally ‎higher pressure drop than the other MIXERs. In contrast, the MIXER: C=2 is the most efficient based on low pressure drop ‎and energy requirement with slightly greater mixing length‎‎.

Introduction: Today, we are seeing change in the manufacturing process of mechanisms as a multi-purpose device with the dramatic growth of technology. It both helps in saving space and the cost of the product decreases considerably. Today, due to the cost of providing places for jobs, smaller and more compact multifunctional devices are designed. The proposed device is a du-al-use Laboratory MIXER. This device is designed for mixing liquid with determined viscosity, which has various options to enhance the quality and comfort of the operator.Materials & Methods: The device uses a combination of two methods while the process of mixing is separate in other devices, i.e. the MIXER device is either radial or oscillating. One of the importing points in the design of the device is that both systems are combined in one device and it is equipped with control and timing speed system. So far, the roller or Rocker device have not been made and designed in Iran and they are built for the first time. Their main use is for professional mixing experiments in the laboratory of Immunology and medical diagnostics.Findings: The results of the electrical and mechanical performance of the device are acceptable according to the inventions used in various parts and it is economical.Discussion & Conclusion: We could significantly reduce blood clots while it is mixing up by designing the angle of the device. This problem is the result of blood into the vial with the vial cap that causes the so-called "lysis". Another achievement of this device is the combining of both the roller and Rocker devices which provides new mixing methods in the lab for operator.

A numerical model for simulating Residence Time Distribution (RTD) of turbulent flows in helical static MIXERs is proposed and developed to improve the understanding of static MIXERs. The results of this model is presented in terms of different volumetric flow rate to illustrate the complicated flow patterns that drive the mixing process in helical static MIXERs. The computed results are also used to predict the amount of mixing that occurs within a mixing device. Such theoretical estimates need, however, always to be thoroughly checked against observations in static MIXER. To check the reliability of the theoretically estimated RTD from the simulation by the application of the model equation, a comparison of the same with those obtained from observed data experiments in static MIXER using statistical characteristics is done. Comparison between RTD curves shows that motionless mixture can improve the performance of reactor.

In the present work, dispersed phase holdups have been measured in a Hanson MIXER-settler extraction pilot plant with seven stages for two different liquid-liquid systems. The effects of agitation speed, dispersed and continuous phase flow rates have been investigated under a variety of operating conditions. Dispersed phase axial holdup profiles, determined by a sampling method, showed a strong nonuniformity. The results also showed that the dispersed phase holdup changes largely with the direction of mass transfer. Finally, an empirical correlation in terms of physical properties of liquid systems and operating variables was proposed to predict the holdup and good agreement between experimental data and calculated values of holdup was obtained.

Modified active MIXER architecture is presented in this paper which improves the gain and noise figure of the MIXER considerably. The architecture of the MIXER allows wide band operation from very low frequencies up to millimeter – wave regime. Also the proposed architecture makes it possible to use older process options for implementing high frequency MIXERs with acceptable performance. Simulations using 0.18u RF technology files show the efficiency of the MIXER. The technology files are based on BSIM 3 (V3.2).Accurate transistor and passive component models are obtained by augmenting the technology files with the results of Electromagnetic field solvers.

An experimental study has been made of the hydrodynamics of a stage MIXER-settler to obtain appropriate design information. In this paper several tests were done according to full factorial design of experiments with high reliability, since each test recurs seven times and the results of  them are very close to each other(P=1 bar and T=25oC). Sauter diameter in each test is determined with photographing of both MIXER and settler and holdup quantity is measured by vacuum pump at the end of each test. In each test, dispersion height and dispersion length are determined by photographing of settler. Sauter diameter has been compared with Calderbank model and finally, a model has been suggested.

In this study, a dynamic MIXER was designed to mix polymer melts online during extrusion, and the flow of a polymer melt in a MIXER was simulated using Polyflow software. The Orthogonal experiment was conducted to analyze the effects of three geometrical parameters (i. e. the length of entrance zone (Li), the gap between the rotor and wall (g), and the diameter of cone-shaped rotor (d2)) on mixing properties of a dynamic MIXER. The Li, g, and d2 were optimized for the minimum product of segregation scale (S) and power consumption (P). Finally, the mixing properties of the dynamic MIXER were compared with those of SK and SX static MIXERs. The results indicated that among the above-mentioned three parameters, the g was the most important parameter influencing S, and S∙P. The minimum S∙P of 1059 µm·W was obtained when the Li was 16 mm, the g was 1 mm, and the d2 was 24 mm. The S decreased with the increase of the rotation speed from 120 to 360 r/min, and increased with the increase of the flow rate from 15 to 45 mL/min. However, the P increased with the increase of both the rotation speed and flow rate. The maximum shear rate of the melt in the dynamic MIXER was observed in the mixing zone, which was mainly affected by the rotation speed rather than the flow rate. To achieve the S of the same size, the length of the dynamic MIXER was the shortest, and that of the SK static MIXER was the longest. Moreover, to acquire the S of the same size, the dynamic MIXER required the largest P, the SX static MIXER needed a smaller P, and the SK static MIXER required the minimum P.