Dear Sir/Madam
I wonder that the area of total condenser(TC) should be greater than partial condenser(PC) or not.
I got a weird htri result: the area of TC I got is less than the area of PC.
(Pls see the process drawing is attached in the post)
The air/solvent is purged and dosed in the...
Dear eng-tips members:
The toluene 1000kg/hr + Air (O2~10%,N2~90%) 909kg/hr dosing and purge to the reactor to make an exothermic reaction. (Process drawing is attached in)The toluene will be flush up to the top 2 inclined condenser to recover the Toluene back to the reactor(vol=2kL).
I have...
Dear Sir/Madam
Could anyone kindly help me which vertical leaf filter vendor provide GA drawing and pressure drop calculation formula in their Company website ? This vertical leaf filter will be used in the pump suction side for the oligomer production plant.
Usually this type filter pressure...
Dear Sir/Madam
Could any pro kindly explain to me the rigorous Hysys method to calculate the latent heat of vaporization of mixture posted on the following webiste.
http://webwormcpt.blogspot.com/2008/06/determine-latent-heat-and-maximum.html
The confusing step is following adapted from that...
Dear Sir/Madam
I have a project given poor S&T thermosiphon & VLE data and to be required to find optimum size exchanger through HTRI.
The TEMA type : NEM ( vertical), shell per unit : 1, in series : 1
Tube dimension: OD 19.05 mm, length:3048 mm, pitch: 23.81, flow angle:30 degree
The Shell...
Dear Sir
It is desired to cool down 1260kg/hr of Mixed Gas having properties in below table from 70 C to 15C. This operation is performed with cooling water (56000kg/hr) from 10C to 20C. (Note tube side inlet p=3.075barg, delta P =0.075bar Shell side inlet p=3.7barg, delta P=0.7bar). The...
Dear Sir/Madam
I got the temperature profile result (please see the attached file)from my designed 2(shell)-2(tube heat exchanger), but this result seems not reasonable.
I can only see one reason behind this in the following :
1. The hold side outlet temperature of heat exchanger(44 C) is...
Dear Sir/Madam
I would like to convert the 47.2 lb/ft^3 to API liquid density for inputting the standard liquid density (API unit) into the component properties-fixed properties function in PROII.
But, I have trouble to used the formula I found in the following :
API =141.5/(SG 60/60)) -131.5...
Dear Sir/Madam
Could you please kindly suggest any Pro \II simulation book or paper for beginner to do the process design?
For example, process engineers have to do property calculation, such latent heat calculation for the mixture, the distillation column relief valve outlet composition...
Dear Sir/Madam :
I have difficult in understanding test pressure in tightness test. Tightness test is applied to the piping system which handling harzdous, chemical, and hydrocarbon process fluid. (Note. vent, drain or piping open to atm, pressure vessel,heat exchanger, pump, turbines...
Dear Sir/Madam
The process is describe below:
Slurry from PTA rotary vacuum filter feed drum is fed on a flow rate control via RVF pump to rotating pressure
filter.Separation of solid purified terephthalic acid from water-soluble impurities is performed in two rotary filter
stages in the...
Dear Pro
I wonder why the single minimum-flow bypass (protect tow or more pumps in the same service) has to be installed at branched off upstream of the check valves instead of downstream of the check valves.
Some senior engineer told me the reason is if run both pumps at once, the speeds may...
Dear Sir
Could you kindly instruct how to construct a cooling water
hydraulic network calculation excel spreadsheet with pump and
control valve ? Or you could suggest any book or paper related
to this topic. I will be very appreciated. Thanks a lot.
Dear Sir
I have a vacuum drip leg calculation and cooling water consumption
attached in this post. Could you please kindly to comment this spreadsheet ?
Thank you very much.
Dear Sir:
The back pressure regulator located on the
nitrogen purge line (upstream pressure=10kg/cm2g)
open to relieve the pressure when the pressure upstream
increase above the set point.Upstream pressure regulators(
back pressure regulator) close upon loss of upstream pressure.
However...
Dear Sir
The fan blower veneer to me the acceleration head V^2/2g * density is gauge pressure, so I have to add 1 atm to get the vapor density through PM/RT equation.
But, from Bernoulli equation, P1/(density*g) + H1 + V1^2/(2g) = P2/(density*g) + H2 + V2^2/(2g), the term P1 should be absolute...
Dear members:
Cause our boss suggest that extreme care should be taken when sizing lines for low pressure and vacuum service.
.It is worthwhile to calculate pressure drops for small lengths say 10 ft. Using line segment equivalent lengths of 100 ft. or more can lead to errors when computer...
Dear Sir
I got some trivial question about siphon break.
(Attached drawing).
Case 1. The line 1 ( no siphon break),
As delta P(B-A) < s.g.*h1, the liquid could flow down.
but as delta P(B-A) > s.g.*h1, the liquid will hold up and
not flow down, and gas in drum B may flush back to drum A...
Dear Sir/Madam
1. Can we put the API Plan 53 and ANSI plan 7353 on the same drawing (please see the attached file)?
2. All instrument tag (TG, PG, LG) required for API plan 53 also fit in the ANSI plan 7353 ?
3. Canned motor pump seal plan drawing also required to show up in the P&ID legend...
Dear Sir/Madam
Sorry to bother you this trivial. The condensate form in these three horizontal condensers and drained directly to the storage tank.
The seal leg has to be set up to prevent the siphoning of liquid from the seal loop.
How can I determine the minimum height of the seal leg for...
