Lab Report

Fe 3+ (aq) + 2 NO3- (aq) + 3 Na+ (aq) + PO4 3- (aq)  FePO4 (s) + 3 Na+ (aq) + 2 NO3- (aq)

σ_(R_X )=√(((∂R_X)/(∂V_1 ))^2 〖σ_(V_1 )〗^2+((∂R_X)/(∂V_2 ))^2 〖σ_(V_2 )〗^2+((∂R_X)/(∂I_D ))^2 〖σ_(I_D )〗^2+ ((∂R_X)/(∂R_S ))^2 〖σ_(R_S )〗^2 )

Another assumption we used was amid the calculation of the current pipeline amongst D and E. It was demonstrated that there was a prerequisite to convey an extra stream, and accordingly a new pipeline (looped) was required. A diameter was to be assumed for the new parallel pipeline. After two unsuccessful attempts with diameters of 0.3 m and 0.35 m, our third diameter of 0.38 m, successfully carried the additional flow rate of

where A2 is the cross-sectional area of the throat, C is the coefficient of discharge (dimensionless), gc is the dimensional constant, Q is the volumetric rate of discharge measured at upstream pressure and temperature, w is the weight rate of discharge, p1 and p2 are the pressures at upstream and downstream static pressure taps, respectively, Y is a dimensionless expansion factor, β is the ratio of the throat diameter to pipe

This lab demonstrated the head loss in pipe systems due to friction. It was performed by pumping water into the pipe systems, measuring flow rate and taking pressure differences. Last, a final calculation of the results of the head loss and all friction coefficients from the three different equations. Given that our friction coefficients matched closely with the values from the reference table means that our data was fairly accurate. The relative errors for the minor loss are a bit high, but this could be due to mathematical errors.

Literature values for the overall heat transfer coefficients are provided in the Appendix, for both oil-water and steam-oil heat exchangers. The overall heat transfer coefficients calculated for the shell-and-tube heat exchanger will be compared to the literature value to determine the accuracy experimentally calculated coefficients. Additionally, the overall heat transfer coefficient for the double pipe exchangers will be provided by the literature data, and this will allow for equation 8 to be solved for the area of the double pipe heat exchanger. The area of heat transfer in Equation 8 varies depending upon the type of heat exchanger being used.

So the formula showed before also could present in another formula, the relationship showed below:

ln wit = α0 + α1πit + α2 ln nit + α3ait + λ t w + µ i w+ u it w (Equation 1)

b1 = h2 (1 R)/( 1 t ) and b2 = h2 (1 +(n 1)R)/(1+(n 1)t)

Pipe bends are used in power plants, oil refineries, petroleum pipelines, chemical industries, pharmaceuticals and food industry. The main purpose of bend pipe is to change the direction of substance in the piping system and it is considered as one of the critical components in the piping systems due to its flexibility. The piping system carry substances from one point to another point. The carrying of substance in pipe system will be done by applying pressure, temperature etc. If the piping system in an industry fails, company have to stop the running process and it’s directly loss to company. The company have to do maintenance of piping system and cost is increased. Therefore, the piping system have the importance in the industry. The safety of the

2 g l2 − l2 = 21 2 . 2 4π T1 l1 − T2 l2

Table will made to compare the temperature differences of each pipe and discuss which design modification produces the

The boundary conditions that are imposed to the computational domain are: for the top, front wall and back wall, a “symmetry” boundary condition; for the bottom (ground) a “no-slip wall” was selected; for the outlet, a “pressure outlet”, and for the inlet a “velocity inlet” were assigned. For the inlet boundary, the mean wind velocity profile is introduced to the software by developing a User Defined Function (UDF) according to the log-law wind profile (Holmes 2015). The parameters used for inlet wind flow is represented in Table 3. The fluctuation of wind velocity at each time step is then generated by utilizing the vortex method by adding a fluctuating vorticity field to the specified mean velocity

ln(Yit) = α + β1 ln(UEit)+ β2 ln(RDit) + β3 ln(TMit) + 훌1 ln(PTit) + 훌2 ln(SPit) + 훌3 ln(SJPit) + ɳi +ԑit (1)

Head loss in a pipe flow is mainly due to friction in pipes and again friction is due to the roughness of pipes. It has been proved that friction is dependent not only upon the size and shape of the projection of roughness, but also upon their distribution of spacing.