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Deoiling Hydrocyclones And Their Performance Prediction

in Ankur's_Chemical_Engg_Blog
Hi Ankur,
I need to design an hydrocyclone for degassing a low-pressure water/oxygen stream, leaving an electrolytic cell. I have found several calculation methods for different applications, but these, as you say, are empirical, and I don't dare to change a single parameter in them. I know the Muschelknautz method could be applied (with some additional considerations) for ''demisting'' hydrocyclones, but in my case, it's an entirely different application. Nevertheless, I have seen some good articles (and patents) and have a good idea of some design features the hydrocylone may have. Still, I lack information concerning the hydrocyclone design/sizing. I intend to take a ''standard geometry'' (perhaps Rietema or Bradley) and work around it, but do you know of a modelling method or any source of information it could serve my endeavour? Thanks.
  • Soothsayer
  • 11 February 2023 - 05:00 AM

Comparing Iso13709 / Api 610 With Ansi / Asme B73.1 Centrifugal Pumps

in Ankur's_Chemical_Engg_Blog

For anyone interested, I have a copy of a technical summary comparing API610, ANSI B73.1M and ISO 5199 pumps. Also, API 610 8th Edition gave guidelines for the selection of non API 610 compliant pumps (Section 1 - General, paragraph 1.1.4). No doubt the selection of API 610 pumps for all duties in refinery service would likely give an extremely robust pump, but in circumstances where a more lightly constructed pump, in relatively non-hazardous service would suffice, there are massive savings in cost and much reduced lead times for appropriate ANSI/ISO standard pumps

If still online after +10 years you posted your offering, please share a copy once more. Thanks a lot in advance. jlopezcavada@hotmail.com

  • Julianlc
  • 26 January 2023 - 06:28 AM

Design Equations For Venturi Scrubbers

in Ankur's_Chemical_Engg_Blog

Hello Dear Sir,

Thanks for your great information,according to lt = 369.561*R^0.293 / vt^1.127 , I calculated throat length for a venturi Scrubber(Q=50000m3/hr , Q liquid=65m3/hr, vt=75m/sec), and result is about 3 meters. is it right?

and could you please inform me about the reference of this formula?


Best Regards,

  • AliMoh
  • 08 October 2022 - 07:59 AM

Dissolved Oxygen Scavenger Dosing Calculations For Water Treatment

in Ankur's_Chemical_Engg_Blog


I was looking into the oxygen scavenger dosing system in water treatment plants. Would anyone know what may be the negative effects of using these chemicals to remove the dissolved oxygen in water? What would be the waste products of this system and how to dispose of it?.

If anyone could provide me with this information kindly e-mail me at shilpa.sk0995@gmail.com


Thanks and regards,


  • Shilpa SK
  • 29 August 2022 - 03:55 AM

Perforated Pipe Distributor Sizing Calculations

in Ankur's_Chemical_Engg_Blog

Dear @Ankur2061

First of all, thanks for the data that you shared.

I want to calculate the pressure drop of a perforated pipe with gas inside, using the mentioned calculation steps but I don't know how.

Ao computed from step 7 formula and number of holes calculates by dividing Ao per one hole area. I want to calculate vise versa. I mean, calculate the pressure drop of distributor pipe with specified hole diameter and number.

I will be grateful if you  help me.

  • hbiglari
  • 02 August 2022 - 01:53 PM

Multiple Centrifugal Pumps In Series And Parallel

in Ankur's_Chemical_Engg_Blog

This is excellent write up.

If there are two pumps in series, both pump having design head 50 kg/cm2, and first pump is 4 km away from second pump. there is huge pressure loss approx.15 kg/cm2, between first pump discharge and second pump suction, then total head at second pump discharge is cumulative design head of both pump or need to consider pressure drop at suction of second pump for total discharge head.

  • HRT15
  • 26 July 2022 - 04:05 AM