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I've noticed that many of you are wanting to share Microsoft Excel files. You can upload them into your messages just like other files. This should simplify the process of sharing the spreadsheets rather than having to email them to one another.

Señor TALVI y demás miembros del Blog adjunto memorias de cálculos en Excel para su revisión técnica, ingeniería y conceptos que ustedes consideren que se deben tener en cuenta en este diseño.

 

La idea es que revisen estas memorias y la complementen con sus conocimientos y experiencia.

 

En este proyecto que estoy desarrollando se van a construir doce tanques así: Cuatro (4) de acero al carbono en SA-36, uno (1) en Acero inoxidable  tipo 316 y seis (6) en PRFV o fibra de vidrio, con capacidad cada uno de 42.5 ton. para almacenar productos para químicos para tratamientos de aguas.

 

En las memorias están los datos del este producto del tanque N° 1 de acero al carbono. Mi objetivo es que este software en Excel le sirva a todos los miembros de la comunidad.

 

a la espera de su valioso aporte.

 

Saludos

 

 

Sharing your work (calculations / excel workbooks) can be done only with an open heart and a mind free of suspicion.

 

It is outright hilarious when people claim that the calculation they have created in the form of an excel workbook is their original work. Most of the engineering calculations that we do today have their roots in the physical laws, principles, formuals, and equations developed by pioneers and researchers in the field of engineering and science long before many of us had even understood what engineering calculations are.

 

People who are developing calculations / excel workbooks are only organizing and representing the work in a proper sequence and in a manner which is easy to understand and present. Yes, it takes time and effort to do this, and those who have undertaken this task need to be appreciated.

 

I have never endorsed spoon feeding to young engineers because it allows them to think that there is an easy way out for everything. Many of the blog entries in my blog are related to engineering calculations where I have exhorted the engineers to prepare excel workbooks based on the calculation steps mentioned. For each and everyone of these blog entries related to chemical engineering calculations, I have developed an excel calculation workbook, which I have not shared for the very same aforementioned reason.

 

However, I do want to make a public pledge today. When my eyesight starts betraying me and my hands are no longer able to type on the keyboard of a computer, I would like to donate my entire set of chemical engineering calculation workbooks to "Cheresources" for Chris Haslego to use in a manner he deems fit for the good of the chemical engineering community.

 

Regards,

Ankur

I’ve lost count of how many equalization line “problems” I’ve resolved in the field in the past 55 years.  It must be around 10 to 20.  In almost every one of these so-called “problems” the cause has always turned out to be a cheap, quick, and last-minute process engineering or piping designer “solution” to a basic process design screw-up.  I’ve resolved the problem as shown in the attached revised sketch.

 

The typical situation is where a process engineer turns over the process design to a mechanical engineering team composed of usually mechanical engineers and piping designers (who are not engineers).  The basic process design package should contain all the process information critical to mechanically designing and fabricating a reliable and controllable piece of equipment.  This involves the correct sizing of attached piping, nozzles, vents, safety valves, drains, and EQUALIZATION lines.  Their locations are also required to be specified.  All this information and its communication should be carefully organized and scheduled according to project needs.  What usually happens in the case where a heat exchanger - especially a steam-heated one - is concerned is that the process engineer turns over his deliverables to a heat transfer engineer who produces the heat exchanger design for fabrication.  The need for an equalization line is left to a piping designer’s decision or criteria.  In this process, there is inevitably an oversight in failing to point out the need to control the production, flow and control of steam condensate produced in the exchanger.  The fabrication drawings for the exchanger go out approved without any thought as to how the condensate flow will be gravity drain-controlled and this become apparent when the exchanger is delivered.  The solution to ensuring that the condensate flow is allowed to drain under gravity to the respective condensate drum: quickly connect the condensate drum to the steam supply line.  This is quick, cheap, and presumably vents the condensate to a pressure “equal” to that where it originates, and it eliminates the need to do a re-work on the exchanger bonnet (possibly requiring an ASME stamp, expensive and time consuming).  WRONG!  The steam supply pressure is NOT equal to the condensate origin pressure - it is higher by the exchanger’s pressure drop.  The term “equalization” means exactly that: the pressure in the drum should equal the pressure at the condensate’s origin.  This allows for free, un-interrupted gravity flow.  The true and correct origin pressure unfortunately exists in the exchanger’s bonnet last tube pass.  This fact should have been specified by the process and exchanger engineers prior to exchanger fabrication.  An inexperienced or flawed engineering design has caused a more expensive, correct modification.  In today’s engineering world, this type of flawed, embarrassing design is becoming more repetitive than engineering houses would like to admit.

 

I have preached this reality countless times on our forums and have probably become an un-welcomed bore.  I promise this will be the last time.  Samroo’s recommendation is the correct answer.

 

Hi,

The last one on hands is from august 2020 .

Sorry I don't have anymore a subscription to CHE .

Good luck

Breizh 

Hi,

Consider this resource from Bobby. He was a member of this community.

 http://www.bobby-str...I_Decanter.aspx

 

Do you have access to real solutions? if yes perform test to get data about the decantation time. Several parameters to consider, temperature (viscosity), ratio aqueous phase / organic phase (could be modified by recirculation of one phase), coalescers to reduce the size of the decanter. Based on 8 years' experience designing and operating Mixer settlers for rare earths purification.

Check your document ( flow rate should be expressed in Kg/h )

 

Another resource could be Perry's chemical engineering handbook.

 

 

Breizh

Bitan729:

 

I presume you are dealing with an adsorption unit operation that is dependent on temperature bed regeneration – commonly called a “TSA”.  I’ve designed and built this type of adsorption unit and have dealt with the subject at length.  I don’t understand why you’ve posted this thread in the Process Simulation section.  What you ask has little or nothing to do with simulating adsorption.

 

First and foremost, your needs to define the sorption and desorption abilities of your adsorbents should be addressed to your adsorbent supplier.  Today, there are many – in different countries, and with different degrees of performance and credibility.

 

I don’t know whose process and cold box you are using to produce both gaseous and liquid Nitrogen, but I note that your feed air supply is at a rather low 110 psig.  What this indicates is that your water load is much larger than what I’m used to in the past: 1,000 to 2,000 psig.  Your adsorbers are going to be larger beds.

 

I’ve designed and operated my adsorbers for superficial velocities of 20-50 ft/min and I’ve heated my regenerated beds to 400 – 500 ºF, far in excess of your 375 ºF gas flow.  I started with 350 ºF gas flow temperatures as regen gas and as I got more experienced and obtained more professional advice and knowledge, I wound up with getting the beds to reach the higher 400-500 ºF.  This not only produced better operating results, it also increased the adsorbent operating life.  At the end of my career in compressed gases, I fully expected and got 3-5 years of operating life from my adsorbents which included ALCOA’s Activated Alumina and Linde’s Molecular Sieves.

 

Not knowing what you are operating – or how – I can’t offer any more comments.  I offer you the attached interesting article on the adsorption operation in compressed gases.

 

Some recommended adsorbent bed regeneration temperatures for common adsorbents are as follows:

 

Adsorbent

Regeneration Temperature

Molecular Sieve

450 °F to 600 °F

Activated Alumina

400 °F to 500 °F

Silica Gel

400 °F to 500 °F

 

The required regeneration gas temperature exiting the heater is a function of the regeneration gas water content, the regeneration pressure and the desired level of dehydration or final product gas water content.  An adsorbent supplier should be consulted for specific cases.  Note: the regeneration bed temperature is different from the regeneration gas temperature.

 

 Mol Sieve Dehydration Design and Operation.docx   329.61KB   79 downloads

 

 

 

Main Site

https://oilprocessing.net/

@Asgar,

 

I think you are talking about centrifugal compressor. Blocked outlet scenario for centrifugal compressor must be evaluated very carefully as there are certain consideration behind the deriving the worst case blocked outlet relief case. 

 

Usually, you have compressor discharge pressure VS flow curve at normal operating conditions. Blocked outlet can occure when you are off your normal operating coditions. Hence, blocked outlet scenario should consider below cases 

 

1) compressor being operated at maximum suction pressure (higher than normal suction pressure)

2) compressor being operated with fluid with different molecular weight. specially higher than normal case

3) compressor being operated at its maximum speed. 

 

Usually, you should ask vendor about the curve with above consideration and confirm with vendor for the accurate blocked outlet relief flow. otherwise, based on the efficiency data by compressor compressor vendor, you can simulate it for governing case considering power constraints. Note that, in absence of vendor supplied curve, if you are using HYSYS to evaluate the relief flow, it must be carefully done given that the procedure is different for fixed speed compressor vs variable speed compressor. Also, it it two stage compressor, 2nd stage discharge relief flow depends on 1st stage compresor operating condition. I can give you quick method for fixed speed and single stage compressor using simulator as below

 

- take the maximum suction pressure at suction

- model compressor curve in the hysys given by the vendor

- keep discharge pressure same as relief valve set pressure or relieving pressure

- keep increasing the flowrate till the time you see power calculated by simulator is equivalant to maximum power constraints by vendor. 

- add 5% margin on calculated flowrate to abosrb any uncertainly/error. 

- repeate the above steps for lowest molecular weight and highest molecular weight and use PSV sizing for governing case

 

Above step, can give you the relieving temperature also readily from simulator. 

 

If you are at proposal stage and dont have vendor info, you can use guidline as - for variable speed compressor relief flow rate can be in the range of 1.5-1.8 times the design flow rate and for fixed speed machines, this can be in the range of 1.3 to 1.5 times design flow rate.

 

Trust this helps. 

Good luck. 

hi ,

hope this is helping you and others.

Good luck

Breizh

hi ,

October 2018 :616.3  (final)

November 2018 : 616.4  (preliminary)

 

good luck

Breizh

You don't need to do complicated VLE calculations.

 

A value for total absolute pressure P is required but normally that is known.

But even if it is not known you can simply assume a value for P to determine H.

 

For example, using the graph in GPSA EDB, the K-value for H₂S in hydrocarbons is:

K = 32  at P =   1 bar & 38 ^oC

K = 3.2 at P = 10 bar & 38 ^oC

 

So at 1 bar Henry constant H = 32 * 1 = 32 bar at 38 ^oC

and at 10 bar Henry constant H = 3.2 * 10 = 32 bar at 38 ^oC

 

It makes no difference what P is because K is inversely proportional to P as long as P is not too high (see graph).

In other words: only at very high pressures H is dependent on P.

Van8888:

 

Just as Latex and Fallah state: Although you don't tell us the TYPE of positive displacement pump you are using (a piston pump will have essentially no pump curve; it's displacement is constant if both valves work), the pump's volumetric efficiency will increase as the viscosity increases.  Rotary type pumps depend on internal clearances (pistons don't) in delivering a specified liquid volume per time.  As the viscosity increases, the pump increases its effectiveness due to the thicker fluid.  So, a rotary pump's pump curve will be different for different viscosities.

 

ON A MORE PERSONAL NOTE:

Happy New Year to all our members and a special salute and recognition to our good Breton friend, BREIZH, who has announced his retirement.  I hope he persists in joining us here on the Forums and I like his latest personal photo  ........ although, like me, he seems to be losing a few hairs.

 

My personal well wishes go out to all our members and contributors.  May this year be one of happiness and prosperity to all.

there was a Excel page showing how to calculate properties in different zones I attach a copy, you can examine the VBA code for details,

 

Prode Properties can export flows or you can calculate from (molar) phase fractions and molar weights of different fractions, see this VBA example

 

PF = StrLf(Stream)
If (PF > 0.000001) Then ' Liquid present ?
            mw = StrLMw(Stream)
            Cells(rpt + I, 6) = W * PF * mw / mwm ' Liquid Flow

 

and so on...

 

you can calculate mixture properties (density, viscosity, thermal conductivity etc.) in different ways,

Prode Properties exposes methods StrGD, StrLD etc. (there are about 300 methods...)

in this Excel VBA example the procedure calculates vapor properties as

 

            Cells(rpt + I, 14) = StrGMw(Stream)
            Cells(rpt + I, 15) = StrGCp(Stream)
            Cells(rpt + I, 16) = StrZv(Stream)
            Cells(rpt + I, 17) = StrGD(Stream)
            Cells(rpt + I, 18) = StrGV(Stream)
            Cells(rpt + I, 19) = StrGC(Stream)

 

of course different variants are possible (many methods available),

 

you can solve many different Flash Operations with Prode Properties, in this case (heat exchanger simulation) the procedure solves a operation with specified P and H but different alternatives are possible

 

 htcprops.xls   176.5KB   53 downloads

Hi,

 

In syngas plants (ammonia, hydrogen, methanol, etc.) the concepts are different. Steam to dry gas ratio (usually abbreviated as S/DG) is the ratio between molar flow rate of steam and gas, so it's steam flow rate divided dry gas flow rate. This ratio is use frequently at the inlet of shift reactors (HTS, high temperature shift, and LTS, low temperature shift), in particular to evaluate of the flow fed has enough steam as to prevent iron carbide formation in iron-based HTS catalysts.

 

Steam to carbon ratio is usually used to evaluate the amount of steam at the inlet of a steam reformer, and is the ratio between the steam and the carbon, in mole basis. Consider that C2H6 counts as 2 carbons, C3H8 as 3, etc. E.g. if you have a stream consisting of a mixture of 3000 mol/h of steam, 500 mol/h of C1, and 200 mol/h of C2, ethane counts twice as much (2 carbon moles), so in this case it would be 3000/(500+200*2) = 3.33. In this same case, the S/DG ratio would be simply (3000/700) = 4.28 (though in practice no HTS reactor operates with such a high value).

 

Theoretically speaking, in the case of a stream consisting of just steam and methane, S/DG and S/C ratio would be the same. In the case of a stream with only steam, methane, and some nitrogen, the S/DG ratio would differ from the S/C ratio. There are some other ratios used, such as the S/C ratio just for hydrocarbons (so you don't consider inorganic compounds such as CO or CO2) or the S/HCC ratio (you just consider HC C2+).

 

Hope it was clear enough

 

Best regards

Mohammed:

 

To learn how to process design a distillation column you can do a variety of things:

 

• You can take a first year chemical engineering Unit Operations course in a university that offers such a study;
• You can purchase and study a book on the subject;  some books are:
  Douglas, James M., Conceptual Design of Chemical Processes, McGraw-Hill, 1988, pp. 453-457.
  Kister, Henry Z., Distillation Design, McGraw-Hill, 1992, pp. 275-282.
  Luyben, William L., "Introduction" in Practical Distillation Control (W.L. Luyben, ed.), Van Nostrand Reinhold, 1992, pp. 10-11.
  McCabe, W.L., J.C. Smith, P. Harriott, Unit Operations of Chemical Engineering, 5th Edition, McGraw-Hill, 1993, pp. 560-568.
  Seader, J.D. and Ernest J. Henley, Separation Process Principles, John Wiley, 1998, pp. 305-312.
• You can study the material found in many web sites on the internet.  One such site is Dr. Randel Price's (http://facstaff.cbu.edu/rprice/) and a sample of his lecture notes is attached.

 

 7-Distillation - Principles.docx   41.13KB   142 downloads

 8-Distillation II - Modeling.docx   43.81KB   117 downloads

 9-Distillation III - Operating Equations.docx   51.76KB   113 downloads

 10-Distillation IV - Calculations.docx   65.62KB   145 downloads

 11-Distillation V - Ethalpy Balances.docx   39.63KB   102 downloads

 12-Distillation VI - Enthalpy Concentration Methods.docx   63.35KB   94 downloads

 13-Distillation VII - Equipment & Column Sizing.docx   56.11KB   141 downloads

 14-Batch Distillation.docx   45.86KB   104 downloads

Ghasem:

 

This is a very poorly written request for help.

• We don't know how this can be within the Relief Devices Forum.  It is not a relief device.
• Is the Closed Drain located on shore?  Off shore?
• Are you a student?   Your request is very amateurish.  You don't give specific, detailed, and illustrated information on what your query is.
• Is this an academic assignment?  Or is it real life?
• Why the need for heat or vaporization?  Be specific.
• What kind of process environment is this closed drain meant to service?
• Furnish a detailed P&ID of the process, complete with a written description.
• What do you mean by "Basis for selection"?  Be detailed and specific.
• A closed drain is there to protect personnel and the environment.  This is a very serious and important item and requires a lot of specific, accurate, and detailed information if our members are to give suggestions or recommendations.

You are requesting specific and detailed recommendations.  The same type of information is required by the Forum.   The quality and detail of the response is directly proportional to the quality of the request.

 

And don't fail to fill in the requested information in your personal information form.

 

Await your response.