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Was thinking of a check valve to prevent backflowing from higher level tank to the lower level tank. BUT then I will not be able to drain the lower level tank and at the same time draining from the higher level tank. A separate line from each tank should do the job. But any smarter way with...

a. One tank is for normal use and the other one is for emergency - collect off spec water and then slowly mix the water with the other water into the biotreater. Problme arises when trying to run both tanks. b. Thanks for the feedback on the FM side. Proposal is to line up both tanks to the...

I have 2 waste water tanks. Feed from these tanks to the biotreater is via gravity. Problem is, we cannot control the tank levels in example given below. When tank A level is 10 m with tank B at 5 m, opening both tanks to biotreater under gravity will result in the 2 tank levels equalising...

Could there be something in the BFW / BW which is "eating" up the pH ? Organic acid ? We managed to increase the boiler water pH via increasing the morpholine injection. Increase further on your morpholine ? On PO4, sometimes we see higher pH with higher PO4 and sometimes not. So difficult to...

I work in an oil and gas company with a waste water treatment plant. Now and then, we have foaming in the storage tank. Sometimes in the biotreater as well. Like to know from your experience on possible causes of the foaming, method to determine the cause and method to reduce or eliminate this...

Hope some one can help with a drawing to show where the bridge wall is in a typical boiler / furnace.

Hope that you can help me here. In the pump data sheet ( for pumping gasoil ), stated the NPSH is 12 m. Is that 12 m of water or 12 m of gasoil ? Background to the above question is my attempt to justify lowering the low alarm subject to the NPSH. Thanks.

I changed one parameter in the process and the graph shows an improvement in the product quality. Thinking of using Excel's Ftest to quantify the confidence level that there is indeed a change. Your feedback on Ftest to quantify the confidence level ?Other tests available ? Thanks.

Sorry, more infor as below. Water is from a scrubbing unit and pressure at about 15 barg. About 10 barg after the control valve. Temp at about 110 C. Pump is upstream of the scrubbing unit. Vibrating line is after the scrubbing unit.

To prevent back flow of process (liquid, gas, flammable, non-flammable, etc )into N2 line, one can have block valve, check valve ( single or double ), double block and bleed, spade and PD TSOV. Any guidelines on which of the above isolation to use for different cases ? Thanks.

If it is really cavitation, you can resolve via : a. increase the system pressure ( e.g. RO ) b. reduce the fluid temp below the fluid boiling point at the given pressure. a and/or b above will eliminate the formation of bubbles which later lead to cavitation on the collapse of these bubbles...

Chief, Thanks. Thought of doing what you have suggested. But the flows ( process and coolant ) need not be constant. So an increase in process flow will result in a higher exit temp which suggests an increase in fouling. Same problem if the coolant is at a higher temp. One way out is to...

Like to know how to differenciate between vibrating line due to hammering and cavitation. Line is for transporting water at about 110 C through a control valve. I thought for hammering, one needs a change in the flow, e.g. closing a valve. The vibration is continuous and not intermittent. Think...

For a plate heat exchanger, can I use C in the equation below to monitor the fouling ? Q = C*A*LMDT Or is there another way of calculating the fouling coeff for a plate exchanger ? Thanks.

Like to know whether there are smart ways of recovering low quality heat energy from waste warm water ( ~40deg C ). Thanks.