As an engineer in a chemical factory you are required to choose theFIGURE $2$

a$)$ Select, giving your reasons, the type of valve you would

recommend from:

Ball Butterfly Plug Globe

b$)$ Suppose the valve you have chosen has the size$-K_V$ values shown in

the table below.

i$)$ Use the table to determine the required valve size for a

nominal flow of $16$ litres per second.

$[$you will need to apply Equation $5$ from lesson $4-4$: $q_v=K_v\sqrt[\phantom{2}]{\frac{p}{d}}]$

ii$)$ Check to see if this valve size is suitable over the range of the

full flow$-$rate to $25$ litres per second

type and size of control valve to be used in the system shown below,

FIGURE $2.$ A pump is used to pass a chemical through a heat exchanger

and then on to a reactor. The valve is used to throttle the pipe line

connecting the heat exchanger to the reactor.

The sizing of the valve is important as the chemical is part of a sensitive

reaction and inaccurate additions will ruin the entire batch.

The liquid chemical, which has a density of $600$ kg$/$m$3,$ is pumped at $5\mathrm{.}5$

bar gauge at a nominal rate of $16$ litres per second. However the design

must permit the flow rate to vary over the range of $8$ to $25$ litres per

second. The design must also allow for a pressure loss of $0\mathrm{.}7$ bar across the

heat exchanger and the pressure in the reactor must be kept at $2\mathrm{.}1$ bar. It

can be assumed that the flow is turbulent and non$-$choked.Q$2.$ As an engineer in a chemical factory you are required to choose the

type and size of control valve to be used in the system shown below,

FIGURE $2.$ A pump is used to pass a chemical through a heat exchanger

and then on to a reactor. The valve is used to throttle the pipe line

connecting the heat exchanger to the reactor.

The sizing of the valve is important as the chemical is part of a sensitive

reaction and inaccurate additions will ruin the entire batch.

The liquid chemical, which has a density of $600k\frac{g}{m^3},$ is pumped at $5\mathrm{.}5$

bar gauge at a nominal rate of $16$ litres per second. However the design

must permit the flow rate to vary over the range of $8$ to $25$ litres per

second. The design must also allow for a pressure loss of $0\mathrm{.}7$ bar across the

heat exchanger and the pressure in the reactor must be kept at $2\mathrm{.}1$ bar. It

can be assumed that the flow is turbulent and non$-$choked.