SO BASICLY WE WANT TO SIZE A PRESURE EQUALIZATION LINE FOR A 10" PIPELINE VALVE (KIND OF BY-PASS) TO EQUALIZE THE DOWNSTREAM OF THE 10" VALVE DE TO A VERY HIGH DP BETWEEN UPSTREAM AND DOWNSREAM OF THE VALVE.

THE PIPELINE CARRY A 85 BAR LPG.

The Process parameters are as follows

Flow: 10700 usgpm (Fluid: Water)

Temp in / out : 3.3 / 13.3 C

Internal tank dimensions : 14 m x 14 m x 42.5 H

There could be an H shaped or a octagonal shape diffuser with slots. The length of the diffusers (top and bottom) can be adjusted.

I need advise from fellow engineers, if any one has any calculation/references to calculate the dimensions of the slots (WxLxDepth), in-order to maintain very laminar flow/low velocity so that the thermocline thickness is not disturbed through out vertical length while charging and discharging. Or there is a dimensionless number such as Froude no or so which can relate to the slot design.

Thanks

Instrument air dryer uses adsorbent  Alumina for removal of moisture designed for 100 % humidity & 45 Deg C  With lower humidity and feed temperature at 35 Deg C whats is impact on performance respect to dew point and capacity of the dryer. 

With regards

In our product transfer unit TSV are provided on transfer lines from Tank to loading bay. TSV set pressures 12 bar are observed to match the pumps shut off pressure when operated at minimum flows.Now we need to reset the TSV set pressures,as observed frequent activation leading to maintenance.Whats should be the revised TSV pressure .considering no change in pump operation. 

Thanks 

Do you have experience with vibrational viscometers like the ones here from Rheonics: https://rheonics.com/solutions-item/meeting-rigorous-quality-control-of-asphalt-for-every-load-at-the-terminal-with-real-time-viscosity-measurements/

What else have you used? 

For the nitrogen flow measure ment we have DP type transmitter having range 0-2500 MMWC ,variance ,diff between custody meter which is ultrasonic  is observed at a lower flows < 1000 Nm3/hr . With current DP what are the options for reducing the difference  

 Do you any AI which can be used to prepare all  process engineering documents . If yes which AI is to be used any specific refence if any body have used . 

I does not mean that it is " Yeast " , it was typo error sorry for inconvenience ; instead of Yes I wrongly type yeast . My querys is that if our reaction requires some temp ;  so can we consider the heat generated during mixing of liquid by agitator -which upcourse requires power while considering heating requirment .  Power required by agitator  can be considered (as temp will  rise in slurry/liquid due to agitation ) while considering heating requirement of that reactor . Suppose tank is having heating coil; so temp rise due  to agitation in slurry can be considered while calculating heating requiremen. 

Suppose heating requirement is X and heat genereated due to agitation is Y so while designing heating requirement i.e.

Net heating requirment  for designing coil = X-Y .

SO3 is produced by conversion of the So2 to So3 in a convertor. DP for the 1 st and 4th beds has observed to have increased from the normal values to max limits .Is their a tool to predict the balance service period of operation based on DP. flow has been reduced by 20 % of cap.

Nitrogen is generated by passing compressed air in a pressure swing adsorption cycle. The adsorbent used is Carbon Mol. seive. Mechanical tests, namely Crush strength and Hardness, are required to check its performance.

Requested members to share the standard test methods document.

Hello everyone,

I would like to understand how to convert packing height into an equivalent number of theoretical trays, and vice versa (i.e., number of trays to packing height).

This is for an amine plant I am currently working on, and I am trying to evaluate which option would result in a more optimized design—trays or packing.

I would appreciate any guidance or references on this topic.

I am currently designing a cold vent (atmospheric flare/vent stack) for a high-pressure gas pipeline system operating at 70 bar.

One of the key design parameters I need to determine is the minimum required distance between the blowdown valve and the vent outlet.

Are there any specific standards in teh API 521 ( which i didn't find so far ) 

So are they any good practice to properly size this distance,

Thanks in advance.

I’m operating a chemical plant and we recently started producing about 3 tons per batch of potassium silicate solution. (90% KOH + H2O +  precipitated silica99% )

After production, we immediately rinse the tank thoroughly with water (right after discharge, before any visible drying). When the tank surface is still wet, it looks completely clean.

However, once the tank dries, we consistently find a significant amount of white powder residue on the inner walls. This residue is quite difficult to remove and requires additional cleaning effort.

We are planning to use this tank interchangeably for both potassium silicate production and cleaning agent manufacturing, so this issue is becoming a serious operational concern.

My questions:

1. Is this a common issue in potassium silicate production?
2. Is this likely due to silicate film formation or silica precipitation during drying?
3. Do most plants use acid rinse or other methods to prevent this?
4. Is it realistic to use the same tank for silicate and detergent production?

Any advice or shared experience would be greatly appreciated.

Thanks in advance!