LIST OF FIGURES

Most industrial applications involve flow through pipes in the world today, in addition to water pipelines, many other fluids are being transported through pipelines such as oil, mud, drilling mud, chemicals which have different viscosities and shear stress profiles that affect flow performance. Therefore, in this study, research on non-Newtonian polymer fluids with viscosity effects flowing through a flow circuit pipeline has been carried out; Flow characteristics data are obtained to determine the inlet length for the flow and compared to the water.

FIGURE 4.12 Graph for Water and Xanthan Gum 0.025 % at 200 kg/min 40 FIGURE 4.13 Graph for Water and Xanthan Gum 0.05 % at 200 kg/min 41 FIGURE 4.14 Graph for Water and Xanthan Gum 0.075 % at 200 kg/min 41 FIGURE 4.15 Graph for Water an

INTRODUCTION

Project Background
Problem Statement
Objective of Study
Scope of Study
Project Feasibility

The developing region of the Flow is characterized as unstable and therefore not valid as a data source for flow characteristics. As a result, to perform valid and valuable experiments in the flow loop, the data must be taken from the fully developed region of the flow.

LITERATURE REVIEW

Newtonian and Non-Newtonian Fluid

Newtonian Fluid
Non-Newtonian Fluid
Comparison between Shear Stress and Shear Rate

A non-Newtonian fluid is a fluid in which the viscosity depends on the shear rate, but some have shear-independent viscosity. This is because the viscosity of a non-Newtonian fluid changes as the shear rate changes.

FIGURE 2.1: The variation of wall shear stress in the flow direction

Entrance Length Newtonian vs Non-Newtonian

Based on current textbooks [23], the inlet length is the length from the inlet area of the pipe to the section where the liquid has fully developed. As the fluid moves, viscous effects can cause it to adhere to the pipe wall.

Table 2.1: Summary of previous investigations of development-length requirements for non-Newtonian power-law pipe flow [22]

Laminar, Transition and Turbulence Region for Newtonian

General Background of Laminar, Transition and
Newtonian and Non-Newtonian Laminar and

The shape of the velocity curve represented in the velocity profile across any pipe section depends on whether the flow is laminar or turbulent. In addition to the viscous sublayer, there is a buffer layer in which the turbulent effect is important, but the flow is still dominated by the viscous effect.

FIGURE 2.9: Velocity Components in a Pipe Flow [24]

Polymer Fluid Used for Test

Polyacrylamide
Xanthan Gum
Calculation of Percentage and PPM (parts per million) 23

27] It can cause a large increase in the viscosity of a liquid by adding just a small amount of almost one percent. One of its uses is in the oil industry where it thickens the drilling fluid to bring it back to the surface and when stopped it remains suspended in the drilling fluid. One of the requirements for this research is mixing polymers and water in order to conduct the experiment with different polymer concentrations.

Therefore, knowledge about the mixing calculation method is an important factor, which could play a major role in the results obtained for this study. Some values in this experiment can be explained in ppm or percent. In addition to the project activities and the Gantt chart, the project milestone and equipment used are also discussed in detail in this chapter.

FIGURE 2.14: Chemical structure of Xanthan Gum [28]

Procedure Identification

The project began by first identifying and defining the project's problem statement. Once the objectives were known, the author did an extensive study on the project by collecting information and data from available journals, articles, books and references. This allows the author to understand more about the project they will be conducting and allows the author to link the project to other previous research by the researchers.

Then data was collected on the parameters involved to set a limit on the knowledge to be used, e.g. in terms of calculations, what types of polymers to use as well as what type of flow loop is used. Once the results are documented, the entry length of the polymers is characterized and delineated. Now the final step is to complete a detailed report with the graphical figures and explanation of the theory and experiments performed according to the procedures and requirements.

Tool Requirement

Polymer Flow Loop Test Rig
Micro Motion Coriolis Mass Flowmeter
Differential Pressure Trasnducer
Flow Loop Software

Design and Setup

Therefore, visually, the results support the theory, as the formation of the input length slightly decreases with increasing polymer concentration. From the xanthan gum addition results, we can see a common pattern in the change in input length. The change in entry length may not be significant, but the results show a significant trend.

From the entrance length results for xanthan gum at a mass flow rate of 100 kg/min we can see the difference where from the 0.01% concentration we get an entrance length that is close to the results for water. Our experiment results indicated a difference in the entry length with the addition of xanthan gum and polyacrylamide polymers. The entry length was taken as the point where the pressure difference becomes constant or a very small difference.

Table 3.1: Concentration of Polymer used Polymer Used % concentration Weight (grams)

Experiment Procedure s

Key Milestone

Ghant Chart

RESULTS AND DISCUSSION

Introduction

The shear stress will be calculated using Equation 5 and was used in conjunction with a Rheometer (TI instruments AR-G2) to measure the viscosity of the non-Newtonian fluid within the flow loop. The dimensionless inlet length is determined from the graphs of dimensionless inlet length versus the pressure drop per length. The criteria used to verify the inlet length is by calculating the percentage difference of pressure drop per length from the first point to the last point.

The dimensionless inlet length is determined to be the point where the pressure drop per length percent variance does not leave the limit determined from the data, whereby it does not leave the determined limit for three consecutive points. Therefore, we can assume that the entry length begins at the first of the three consecutive points, where by using equation 4 to obtain the approximate entry length. The results for the dimensionless inlet length against the pressure drop per length for the experiment with water and polymer concentrations will be discussed in the following subsection.

FIGURE 4.2: Example criteria used to determine the entrance length

Results for Water

As we can see from the graph above, water flowing at 200 kg/min through the test tube at a Reynolds number of 42714.63 has an entry length of 2.08 meters. This shows the entrance length of water at this a speed of 0.6194 m/s requires 2.08 meters to develop from laminar to transition then turbulent where it is then stable where the pressure does not go out of a limit of 10% from point four to six. The entry length is determined when the pressure difference becomes even or there is only a very small difference.

As we can see from the graph above, water flowing at 300 kg/min through the test tube at a Reynolds number of 64071.94 has an entrance length of 2.7 meters. It shows the entrance length of water at this a velocity of 0.9291 m/s requires 2.7 meters of the dimensionless length, XD/D to evolve from laminar to transition then turbulent where it is then stable. Entrance length is determined when the pressure difference equalizes or there is only a very slight difference of 15.

Figure 4.4: Graph for water at 200 kg/min (Re = 42714.63)

Results for Xanthan Gum

Xanthan Gum at 100 kg/min

However, based on the criteria used, the length of entry for the following concentrations indicates the section where the length of entry has developed. The exact value of the input length can be seen visually from the graph results and according to the slope where the polynomial lines become straight is the input length. However, for the xanthan gum thickness of 0.075, there may have been some errors during data collection or equipment, as the results differ from the normal sample.

However, based on the criteria only the highest concentration shows a reduction in length. The reduction for other concentrations is very small, so it can only be determined visually on the graph where the polynomial graph forms a linear line.

Figure 4.7: Graph for Water and Xanthan Gum 0.025 % at 100 kg/min

Results for Polyacrylamide

Polyacrylamide at 100 kg/min

The same criterion is applied to the results, therefore the variance of the input length can only be seen visually and there is a very small difference. The inlet length decreases after a 15% pressure change of 3 consecutive drops with increasing percentage of polyacrylamide polymer. Therefore, using the data from this experiment we have also proven that viscosity has an impact on the inlet length of the pipe flow.

From the results of conducting the experiment with tap water, we noticed the difference in the results in terms of flow rate, pressure drop, speed and inlet length. We note that for water flowing at 100 kg/min at a speed of 0.3095 m/s the pressure drop as well as the Reynolds number and inlet length are smaller. This indicates a slight increase in its viscosity that has given effect to the length of the inlet.

Figure 4.22: Graph for Water and Polyacrylamide 0.025 % at 100 kg/min

Performance Comparison of Xanthan Gum and Polyacrylamide 56

CONCLUSION AND FUTURE WORK

Conclusion

However, there was not much published work on the study of turbulent inlet length in pipe flow. Some researchers have developed empirical equations to characterize the inlet length of Newtonian turbulent flow, however, little has been done to characterize the inlet length of non-Newtonian turbulent flow, and therefore the conclusion of this study is expected to provide researchers with next an experimental solution. for characterizing the inlet length of non-Newtonian turbulent flow. Therefore, our experiments can be carried out with full understanding of the phenomena occurring in the flow, as well as the ability to analyze the result.

This is the point where the fluid has developed where from laminar to turbulent and is proven by textbook theory and reference. 23] In addition, from the study we can also conclude that the addition of polymer provides a significant difference in the entry length, where as the concentration of the polymer increases, the entry length decreases. In conclusion, this experimental study was a success as the results proved above that the polymer affects the liquid entry length, therefore in other words, higher viscosity reduces the liquid entry length.

Future Work

Fluid mechanics at the micro- and nanoscale: transport in microfluidic devices. https://en.wikipedia.org/wiki/Newtonian_fluid. 4] Jaafar-Japper, A., 2009, “Duct Flow of Polymer Solution: Experiments, Simulations and Mechanisms”, PhD thesis, University of Liverpool, England. http://en.wikipedia.org/wiki/Non-Newtonian_fluid. 7] Apel, S.M., 1997, “Viscoelastic behavior of aqueous solutions of polyethylene oxide and xanthan gum”, MSc Thesis, California State University, USA. Time-independent rheology of fluids represented as shear rate as a function of shear stress [Online].

G., 1965, “Laminar pressure drop associated with the continuum entry region and for slip flow in a circular pipe”, ASME J.A., 2005, “The development lengths of laminar pipe and channel flows”, J.S., 1990, “Unified Entry Length for Newtonian and Power Law -fluids in laminar pipe flow”, Can. 21] Ookawara, S., Ogawa, K., Dombrowski, N., Amooie-Foumeny, E., and Riza, A., 2000, “Unified Entry Length Correlation for Newtonian, Power Law and Bingham Fluids in Laminar Pipe Flow at Low Reynolds Number”, JW, “Entrance Length and Fully Developed Flow”, Fundamentals of Fluid Mechanics, Wiley, New York, pp. Drag Reduction In The Turbulent Pipe Flow Of Polymer 197-213. http://www.zlpam.com/wp-content/uploads/2011/11/About-Polyacrylamide-Fact-Sheet.pdf.