Process Engineering - Science topic

Another suggestion, and highly needed: Food Forensics. I spent my carrier in foods doing Food Forensics/problem solving and I always had a backlog of requests for help often by as much as 12-14 such requests. Some from the company I worked for and some from its customers. I had to advertise a little up front, but very quickly word of mouth was all I needed to stay extremely busy. Various forms of imaging (light, electron, C- X-ray), elemental analysis and chemical analysis. My book “Food Forensics” gives the how-to.

Its really serves as a good first estimate

Process Systems Engineering (PSE) cover these aspects. PSE is a new discipline at the interface of chemical/process engineering, computer sciences, and mathematics.

High pressure steam is typically desuperheated by injecting boiler feed water to meet the desired temperature target,

A lot of companies now require software skills along with chemical engineering knowledge. The most prominent one in them is Python. I have a lot of friends working on Python in process modeling & simulation etc.

Thank you Sina Safavi

V. The recursive least squares algorithm (RLS) allows for (real-time) dynamical application of least squares (LS) regression to a time series of time-stamped continuously acquired data points. As with LS, there may be several correlation equations with the corresponding set of dependent (observed) variables. RLS is the recursive application of the well-known LS regression algorithm, so that each new data point is taken in account to modify (correct) a previous estimate of the parameters from some linear (or linearized) correlation thought to model the observed system. For RLS with forgetting factor (RLS-FF), adquired data is weighted according to its age, with increased weight given to the most recent data. No prior 'learning phase' is required.

VI. Application example ― While investigating adaptive control and energetic optimization of aerobic fermenters, I have applied the RLS-FF algorithm to estimate the parameters from the K_La correlation, used to predict the O₂ gas-liquid mass-transfer, while giving increased weight to most recent data. Estimates were improved by imposing sinusoidal disturbance to air flow and agitation speed (manipulated variables). The proposed (adaptive) control algorithm compared favourably with PID. The power dissipated by agitation was accessed by a torque meter (pilot plant). Simulations assessed the effect of numerically generated white Gaussian noise (2-sigma truncated) and of first order delay. This investigation was reported at (MSc Thesis):

About predicting a suitable 'V' angle and rotating speed for a V-shaped tumble blender please check my answers given elsehwere at this forum:

https://www.researchgate.net/post/How-do-the-angles-of-V-Blender-tumbler-affect-powder-mixing-operations

Pdf is not opening

Many thanks for the useful question and replies. I am thinking from a different angle. Advanced and new control techniques are tested via simulation (e.g., Aspen Dynamics) and are reported in academic journals. One can then use industrial scale flow rates and capacities. So, what are the pros and cons of simulation versus bench scale experimentation?

I belive bench scale experimentation will require considerable effort and budget but it will have include some practical aspects (e.g., measurement errors and noise). By the way, most of our control studies are via simulation for one reason or other. However, I welcome discussion on simulation versus bench scale experimenation.

Dear Michel, you could employ HPMC as an additive in the reactions for increasing the viscosity of the system, I'm attaching a technical brochure of one of the HPMC brand names where you could find various grades of different molecular weights. In general, HPMC is nonionic and the viscosities of their solutions are stable over a wide range of pH, in my experience pH 2-12 will not affect the solution viscosity, thus there may be a gradual loss of viscosity at higher temperatures or after long periods of standing, especially with high-viscosity solutions.

On the other hand, the hydration time of HPMC will be higher under pH less than 7, so you will have to design your experimental work to obtain the desired viscosity before running the reaction you need to perform.

Dear all of you, today I listened to theories and only theories. Unfortunately I live in a world on the edge of reality. On the one hand, we are scholars by fields and on the other, we are trivial theorists. You, like me, are people who have a superior mind, but your knowledge is for spheres of excellence. As a linguist I want to aggregate myself and ask you a question. The spreadsheet can be handled only x numerical facts, as well as a writing sheet reproduces the constant headwords of thought. I ask you great minds quantum words can be related to numbers and put them on an equal footing in a spreadsheet? e.g.: AA BB = 2 times A and 2 times B. By repeating this action 6 times how can I make it explicit in mathematical language? In linguistics I say that I get an alliterative phenomenon of alliterative concateness and you? Sorry but I need an urgent answer-

Arjun Sankar S Defined Spec. for tower is incorrect so check these paramete in order to make the converging of the tower.

re-Check the parameters again and tell me what happened??

Before giving any response, can you advise/ provide information for the following? (The above responses cover most of your thermal design requirements.)

(i) What is the required duty?

(ii) What is the fluid to be heated? Can you confirm its temperature range and fluid properties? Is it toxic? Does its properties change significantly with temperature?

(iii) Do you have a rough size for the exchanger/condenser?

(iv) Do you have access to software such as the suites provided by HTRI and HTFS?

(v) What is the source of heat? How is this provided?

(vi) What happens to fluid to be heated if you get an upset condition resulting in too much steam being introduced?

(vii) Would any leak and cross contamination of the fluids lead to a dangerous situation?

If you are using steam at 100C and it is a condensing application, you will have a pressure of roughly atmospheric pressure and I am wondering what drives the steam flow? Condensing steam has a good heat transfer coefficient in most applications so is usually a good choice - but it is still hot and you must take suitable precautions.

In many industrial applications one measures the outlet temperature of the fluid to be heated and use this to control the inlet steam flow - but then they usually provide the steam at roughly five (5) bar g. If there is any boiling / condensation of the process fluid its temperature profile becomes flat and temperature control becomes very difficult. If you know the fluid's properties you can use velocity in the external pipework to give good control, but this does demand consistent fluid properties.

Lower pressures can be used but then all pipework, etc. becomes very large.

There is a company in the UK called Spirax-Sarco and they provide useful information for the design of steam equipment. They give a remote design course as well as providing design manuals. It use to be a very low cost course but you must verify this.

If you are doing mechanical design, please ensure that in any condensing application you design for full vacuum as if you shut in the exchanger full of steam, as it condenses due to heat loss, its pressure will drop. Under similar temperature, etc. conditions the density of steam is significantly less than the density of water.

There is a lot of legislation in the UK around the use of steam.

Don't forget that you will need safety valves and their discharge needs to be taken to a safe location.

Hope that this helps. Regards, Stephen.

Thank you Wilson, good addition.

Solvent Density and Solubility of Your Compound

Wave impedance: At a point in an electromagnetic wave, the ratio of the electric field strength to the magnetic field strength. (188) Note 1: If the electric field strength is expressed in volts per meter and the magnetic field strength is expressed in ampere-turns per meter, the wave impedance will have the units of ohms. The wave impedance, Z , of an electromagnetic wave is given by

📷

where is the magnetic permeability and is the electric permitivity. For free space, these values are 4 × 10-7 H/m (henries per meter) and (1/36) F/m (farads per meter), from which 120, i.e., 377, ohms is obtained. In dielectric materials, the wave impedance is 377/n, where n is the refractive index. Note 2: Although the ratio is called the wave impedance, it is also the impedance of the free space or the material medium.

In the following website you find and example and solution to calculate wave impedance.

Bachir Achour Thanks a lot for response. Yes, you are right regarding downstream equipment design pressure, while my question is about difference between gas and liquid overpressuring.

In the most cases of thermally driven flows the inner vortex moves because of the buoyancy force, one of the effects of this motion is the characteristic folding behind the raising air mass. We can often observe also the Kelvin-Helmholtz instability on the edge of a rising thermal. I have attached a simple computer simulation depicting solution of the inviscid Euler equations for such a case; the initial condition assumed fluid at the state of rest in the external gravity field and a small initial perturbation of the temperature.

Creation of the outer downward vortex is often due to shedding of vortices in the wake of a thermal or in result of additional thermal forcing.

This is one of these questions to which the answer is "You shouldn't start from here." In chemical engineering the design of reactor is often trivial compared with the design of the separation process, and the correct method is to design the reactor to facilitate separation, not to look for "end of pipe" solutions afterwards.

Feasible solutions will depend on the nature of the slurry and the liquid. If the slurry is crushed material having a wide particle distribution and many fines, then it will be if not impossible then close to it. If it is mainly (roughly) monosized beads, then you have a good chance for filters or dynamic separators such as cyclones. Note that even with pressure filtration the resulting cake is likely to contain more than 60% by volume of liquid. You will need to displace the liquid between the particles by blowing through or vacuum. How much is retained on the surface of the particles depends on the viscosity and surface tension.

For many downstream particle problems, the best solution is to change the particles, for example do not grind them so small, and sieve out the fines before putting them in the reactor. If this is possible you should seriously consider it rather than just fighting a losing battle with what you have already.

For this scale, batch treatment would be more appropriate than continuous. The most obvious is a centrifuge to separate the particles from the liquid. A small one could be used several times, e.g. a half gallon one used 30 times.

It is a very interested question ,see

I suggest you go for a PhD rather than an MSc because you already have one and have published a couple of papers . At the very least aim for an MPhil with the plan to work towards a PhD.

Interesting

Sir @Syed A.Taqvi and @Jerry Decker is there any specific separator in Which I can define that this gas I need to remove separately from the top and the other gases from the bottom. As I tried FLASH separator I found that all gases went to the top and gases from the bottom shows all values zero. I also tried just Sep to separate the gases, One specific gas from the top and other three gases from the bottom but this need Design Specification I specified the flow and split friction but this still gives this error "Number of specifications must be equal to number of components for each substream " . Do you have ever dealt with this kind of issue?

interested

This discussion on dependency of Oxygen is rubbish. If Algae is present in the secondary settler it is as Evangelos rightly wrote due to the presence of Nutrient, but the second very important factor is sunlight. If there is sunlight the O2 that might be present will be coming from the Algae them selves. This mean also that you must have a very good settling sludge since you get a good penetration of the light into the tank.

Two solutions: Go for getting a limiting concentration of Phosphorous ( <0.1 mg P/l ) by dosing coagulant direct in front of the clarifier. This will also help if you should have a small release of P in the Secondary settler. This will not totally eliminate the problem since a real limiting concentration is lower, but in general the lower the P level the less Algae you should have. Nitrogen limitation is not very realistic and hence the most efficient way to avoid the problem is covering the tanks.

Here is a link that might help:

There are also practical considerations like : local Demand, expected max time interval between shipments, availability of supply from other sources and ability to substitute other products (LPG, pipeline natural gas etc) for LNG etc

Dear Fuad,

Please have a look at these useful ResearchGate links.

Good luck!

The rates of individual reactions (forward and backward) are of course different (omitting state of equlibrium). It should remain unchanged the form of a kinetic equation, but one must remember to change the values of reaction rate constants (one on the other) or about changing the rate constant and equilibrium constant values. The problem may also occur if in the kinetic equation there will be pressure activities instead of partial pressures.

Yes, the above kinetic equation does not make sense unless we know the value of equlibrium partial pressure of benzene and the value of the constant K_B has been adapted to this situation. Regards,

Suggest to read the following paper besides a good text-book on separation processes.

The above paper has results for 13 examples (Table 4), wherein optimum reflux ratio varied between 0.08 and 18.6. Besides reflux ratio, suggest to check reboiler duty and its cost.

Teperatue rise depends on feed quality but typical conditions are 360 C inlet and 380 C outlet

Mix well, settle, and decant. Both fractions are emulsions. You may also add detergents or other surface active agents to help with final compositions.

Dear Jacob,

I don't know details about your running experiment but perhaps the following article might help you to get some ideas concerning upscaling of electrochmical reactors.

thanks a lot Mr Manner and Mr Jayant 

Hi Miroslaw,

Thanks for all your answers.

Regads

Shayan

The settler and aeration tank may need different property sets. Example is a settler using NTRL as the property set for a thermodynamic equilibrium of phases. A famous case, the settler operates at a discontinuous point, while the property set uses a continuous equation to approximate it, resulting in large percentage errors.

Thank you sir.  is ZVI available on market? laboratory synthesis to it have only minimal yield.

thanks you so much Sir Kanhaiya  

Dear Bruce

Thank you for your answer. It is very interesting. I have just preparing my first publication using Wilcoxon test so we'll see how I go to explain the text in the publication :) In my case it occurs large sample (n=120), so the statistical distribution tends to a normal distribution.

Best regards, Justyna

Are there available data (diagram) for lower temperatures (500, 700 C)?

I think I have finally identified the problem and it has nothing to do with the different versions of TRNSYS.

The thing is that I have my project uploaded to the cloud and every operation with the project files is causing an instant synchronization with the cloud.  

Every time I was trying to update or run the simulation, the files created before were replaced and synchronized with the cloud. This process generates some lag and is the reason for the crash of the Simulation Studio.

The solution would be not to work with the cloud while simulating or to put the synchronization on pause while TRNSYS is working.

I have previously worked on the cloud with other TRNSYS projects (not so complex) and have never met this problem before. So, the complexity of the model is important as well.

You may want to try an agarose or agarose-acrylamide composite gel for such large protein complexes. Here are some references:

The value gives an approximation for the content of aromatic compounds in the oil, since the miscibility of aniline, which is also an aromatic compound suggests the presence of similar (i.e. aromatic) compounds in the oil. The lower the aniline point, the greater is the content of aromatic compounds in the oil.

The aniline point serves as a reasonable proxy for aromaticity of oils consisting mostly of saturated hydrocarbons (i.e. alkanes, paraffins) or unsaturated compounds (mostly aromatics). Significant chemical functionalization of the oil (chlorination, sulfonation, etc.) can interfere with the measurement, due to changes to the solvency of the functionalized oil.

Aniline point (AP) is another characteristic of petroleum fractions that indicates the degree of aromaticity of hydrocarbon

mixtures. Aniline point is defined as the lowest temperature at which equal volumes of aniline and the sample become completely soluble. As amount of aromatics in a petroleum fraction increase the aniline point decreases. Therefore, the aniline point is a parameter that is highly related to the hydrocarbon types in petroleum fractions.Aniline point is a useful parameter in calculation of heat of combustion, diesel index and hydrogen content of petroleum fuels.For non fuel products such as solvents aniline point is usually specified to quantify their effectiveness. Linden used the method of characterization of Watson and Nelson to develop a simple correlation for prediction of aniline point in terms of boiling point and API gravity [4]. However, the correlation was originally

developed based on only 37 samples.

Determination of aniline point is a test to evaluate base oils that are used in oil mud. The testindicates if oil is likely to damage elastomers (rubber compounds) that come in contact with the oil. Theaniline point is called the "aniline point temperature," which is the lowest temperature (°F or °C) atwhich equal volumes of aniline (C6H5NH2) and the oil form a single phase. Aniline point of oil gives anindication of the possible tendency of deterioration of oil when it comes into contact with packing,rubber sealing etc. in general oils with a high aromatic content are more detrimental to rubber productsthan those with a low aromatic content. The relative aromatic content of an oil is indicated by its anilinepoint and oils with a high aromatic content have a low aniline point and vice versa. The higher theaniline point of the oil ,the more desirable it is for drilling fluid usage. In our experiment, 5 ml aniline and5ml diesel were taken in a test tube provided with thermometer and heat was given until both anilineand diesel become completely miscible. The aniline point of diesel was found at the temperature of 94°C.

1.Aniline 5ml

2.Diesel 5ml

3.Test tube

4.Burner

5.Thermometer

6.Paraffin oil

7.Beaker

1. Apparatus was cleaned and dried. Then 5 ml of aniline and 5ml of the oil was measured to betested into the test tube.2. Stopper was placed into the test tube and a thermometer was inserted, making sure the bulbdid not touch the sides or bottom of the tube.3. The tube was slowly heated while stirring the mixture (stirred by moving the thermometer upand down) until complete miscibility (the mixture becomes clear) occured.4. Removed from heat source and continued stirring until aniline-oil mixture became cloudy.Thermometer temperature was observed at cloud point and reported aniline point in °C.

Result:

Observing and conducting the above experiment precisely, we concluded the aniline point of diesel is 94°C.

Precaution:

1. As aniline is poisonous, the vapor of the mixture could cause severe health damage. Thats why mask was worn during the experiment.

2. Well ventilation at the lab was secured to pass the vapor without causing any damage.

3. Apron and gloves were used to restrain from direct contact.

4. Our hand was thoroughly washed after the experiment.

5. Temperature was measured cautiously to avoid humane error.

6. Water was kept away from paraffin.

While I have no first hand experience developing an insulin purification process, I've spoken with others who have.  I'm told that there are many different insulins and that the process required to achieve an injectable quality drug is extremely complex.  Early processes used by the leading suppliers had as many as 27 steps in downstream. Chromatography suppliers such as GE Healthcare have related experience and appropriate products to begin to develop such as process.  Good luck,  Craig

Hi

Why not use pressure swing system while operating in parallel. This will ensure optimal usage and conversion in each stage.

As far as removal of water is concerned; you can go for reactive separation if water is not needed in the downstream section. If not physical methods need to be implemented.

You can use either ANSYS Workbench /ANSYS Mechanical for your desired purpose by using "DEATH and BIRTH codes" . For that firstly, you have to create elements in your geometry depicting the deposited material. Initially, these elements were killed by writing codes in " command snippet" using 'EKILL command' in ANSYS Workbench (I followed the same procedure for welding moving heat source). Subsequently, these elements were made alive step by step by using 'EALIVE' command. 

POX is a  good way to produce syngas/H2 from any hydrocarbon.  Usually low value  hydrocarbon  like vacuum resdue or natural gas are used as feed but any hydrocarbon will work.  

If you want to produce H2 from C6+ Hydrocarbon naphtha reforming is a good option that will increase the octane of the naphtha and make H2 as a byproduct 

Never heard of it, that HCl can be burned in a flare stack. It is not a hydrocarbon and as such you cannot burn it. The best option is to pass through a Packed bed Scrubber before venting it to atmosphere.

selvage uncurler??

Dear Roy Nitzsche,

Aspen Polymers® is the market-leading, first-principles polymer modeling technology for accurate and reliable simulation and optimization of polymer processes.The Process of poly lectic Acid can be simulation by Aspen plus. A process flow diagram for the production of polymer grade lactic acid has been developed using Aspen Plus. The process has successfully simulated and converged results has obtained. An extensive sensitivity analysis is conducted on each of the key pieces of equipment to obtain high purity methyl lactate and subsequently pure lactic acid. The process conditions are subsequently optimized based on these attached results. The desired purity of polymer grade lactic acid (99 wt. %, dry basis) was obtained. Also, the purity of methyl lactate was above the desired percentage of 98.5 wt. %.Many options are open to reach this goal including the bioconversion of biomass into either energy carriers or bulk chemicals. In this respect, bioethanol and lactic acid are excellent candidates as liquid fuel and bulk chemical, respectively. As for the biomass to be used as feedstock, potential interference with human consumption should be avoided. Hence, lignocellulosic biomass is the preferred option for future large scale processes. Bioethanol can be applied directly or in the form of ETBE in blends with petrol; lactic acid is a renewable alternative for petrochemical solvents and for production of polylactic acid (PLA) to replace petrochemical packaging materials and other synthetic materials. The preparation of fermentable sugars from lignocellulose is a major challenge for both bioethanol and lactic acid production and requires integral optimization of the trajectory from feedstock through fermentation to product recovery.

You can browse Prof. Nishith Verma google scholar page for more papers on VOC removal. The group has worked a lot in this field. Hope it helps!

Link: https://scholar.google.co.in/citations?user=pwNT4HkAAAAJ&hl=en

Dear Elahe,

Many different types of models are used in various scientific and engineering fields, reflecting the subject matter and the kinds of understanding that is sought in each field. Conceptual modelling techniques in software and information systems engineering have in the past focused mainly on describing and analysing behaviours and structures that are implementable in software. As software systems become ever more complex and densely intertwined with the human social environment, we need models that reflect the social characteristics of complex systems. This chapter reviews the approach taken by the i* framework, highlights its application in several areas, and outlines some open research issues.

In the philosophy of language is any language which arises I* an unpremeditated fashion as the result of the innate facilities for language possessed by the human intellect. A natural language is typical used for communication and may be spoken, signed or written.

i* (pronounced "i star") or i* framework is a modelling language suitable for an early phase of system modelling in order to understand the problem domain. i* modelling language allows to model both as-is and to-be situations. The name i* refers to the notion of distributed intentionality which underlines the framework. It is an approach originally developed for modelling and reasoning about organizational environments and their information systems composed of heterogeneous actors with different, often competing, goals that depend on each other to undertake their tasks and achieve these goals. It covers both actor-oriented and Goal modelling. i* models answer the question WHO and WHY, not what.

i* provides the possibility to achieve information in an early phase of the software engineering process. In former days UML was used to make information visible, but as UML often focuses on organisational objects, which are not so important in the early phase, when the emphasis should be on helping stakeholders gain better understanding of the various possibilities for using information systems in their organizations.

i* provides the possibility to achieve information in an early phase of the software engineering process. In former days UML was used to make information visible, but as UML often focuses on organisational objects, which are not so important in the early phase, when the emphasis should be on helping stakeholders gain better understanding of the various possibilities for using information systems in their organizations.

i* provides an early understanding of the organizational relationships in a business domain. The Use Case development from organizational modelling using i* allows requirement engineers to establish a relationship between the functional requirements of the intended system and the organizational goals previously defined in the organization modelling.

i* is used for the early requirements and UML for late requirements. Thus you have to transform the i* model into a UML model. You can do this by using the following guidelines:

There has been a proliferation of various clones of stakeholder engagement in modelling, or, rather, of the use of modelling in support of a decision-making process that involves stakeholders. In many cases the differences are quite subtle and it may seem that various agencies or groups come up with a new term to serve as a recognised trademark for their efforts. In essence they tend to be doing more or less the same things.have recently proposed literature reviews on participatory modelling: below is a brief overview of various types of stakeholder-based modelling, as well as some stakeholder processes that do not rely on modelling.

regards,

Prem Baboo

Dear Praveen,

you make an interesting question. One has to decide where the boundaries of the process lie. In my case I come from a design background. It is well documented that 90% of product cost is committed at the design stage and many quality issues can be "designed out".

The methods that I have found most useful are:

BS7000 http://shop.bsigroup.com/ProductDetail/?pid=000000000030314817

Theory of constraints (for manufacturing) http://www.spcforexcel.com/publications/Theory_of_Constraints/13B63E123ED3A6769B6575CE93DA4F2F/Theory%20of%20Constraints.pdf

and Prince 2 for management control https://www.prince2.com/uk/what-is-prince2

However, these are heavyweight methods and I use them as guides to good practice rather than adhering to their every detail; more like a tool box where the craftsman decides which tool to use.

Hope this helps

Paul

Dear Tim Shenk,

Thermosetting epoxy polymers are widely used in aerospace and automotive applications as matrices for manufacturing fibre reinforced composites and as adhesives for joining structural components. Despite offering many desirable properties, Carbon nanofibres offer a promising solution but their effectiveness has been limited by difficulty in achieving directional alignment. Here we report the use of an alternating current (AC) electric field to align carbon nanofibres in an epoxy. During the cure process of an epoxy resin, carbon nanofibres (CNFs) are observed to rotate and align with the applied electric field, forming a chain-like structure. The fracture energies of the resultant epoxy nanocomposites containing different concentrations of CNFs (up to 1.6 wt%) are measured using double cantilever beam specimens. The results show that the addition of 1.6 wt% of aligned CNFs increases the electrical conductivity of such nanocomposites by about seven orders of magnitudes to 10−2 S/m and increases the fracture energy, GIc, by about 1600% from 134 to 2345 J/m2. A modelling technique is presented to quantify this major increase in the fracture energy with aligned CNFs. The results of this research open up new opportunities to create multi-scale composites with greatly enhanced multifunctional properties.

Electrical measurements were carried out on rectangular specimens with dimensions of 30 × 30 × 3.2 mm for carbon composites and 30 × 30 × 3.7 mm for glass composites. The surfaces of interest were painted with a suspension of silver in methyl isobutyl ketone (Acheson Electrodag 1415M). DC electrical resistivity of the carbon composite samples was measured using a DC precision current source (Keithley model 6220) and a nanovoltmeter (Keithley model 2182A) via the three-point delta current reversal technique. The electrical conductivity of the samples was measured using 100 µA current in three directions: through thickness, transverse and longitudinal. Through thickness electrical conductivity of the glass composite samples was measured via AC impedance spectroscopy using a Solartron SI 1260 frequency response analyser. Twenty nine frequencies from 1 Hz to 1MHz were swept on a logarithmic scale. The electrical resistance of the samples was determined from the peak value of the imaginary impedance spectrum

For more detail please find attached herewith file & link

Regards,

Prem Baboo

I have not worked in industry on process but from my plant-wide control class last semester, taught by a renown process control engineering ptofessor, it was said that RGA SVD are the industrially used pairing strategies.  He however mentioned that RGA is the best reliable means for pairing.

Dear Thomas

For Soarger design following steps may be used

1.       Calculate steam pressure at sparger

2.       Calculate the mass of steam (w) by combining the heat lost and heat gained equation.

W= mass of the steam

Cp=Specific Heat

Hv = Enthalpy

∆T = Saturation Temperature.

Vs = specific volume

3.       Calculate Steam Volume Flow

4.       Calculate Steam velocity.

5.       Calculate the Area

Now you can calculate size of the sparger

The time taken to heat the liquid depends on how fast the steam is introduced, how much hotter the steam is than the liquid and how well it is distributed through the liquid, i.e. holes dia of sparger ,velocity of the steam & Enthalpy of the steam.

For more detail, please find attached herewith sparger design guide,

Regards,

Prem Baboo

I would advise you to do a few lab test for further H-acid purification

I seems the temperature is high! I didn't  know that.

I think, you should seek help from any market suit software and run Nodal Analysis for various sensitivities of all possible parameters.   That would certainly facilitate u with an optimum design.   Otherworldly, contact any manufacturer for compatible assembly with in-situ fluid conditions.   Thanx

Thank you everyone.  I think vacuum filtration might work best.   Thank you for the help

At 25°C ad 40 bars hydrogen behaves almost like an ideal gas. Its compressibility factor is close to unity.Its value of Z at 25 C and 40 bars is about 1.02

So 500 Nm3 of hydrogen at 25 C and 40 bars have a volume 500x(298.15/273.15)x(1.01325/40)x1.02=14.1 m3

I also think that the concentration of H+ can be evaluated by assuming electroneutrality, i.e. [H+] +2[Ca2+] - [OH-] - [HSO3-] - 2[SO32-] - [HCO3-] - 2[CO32-] = 0. Where the concentrations of all species are written in terms of [H+] and equilibrium constants. The only challenge is to correctly evaluate [SO32-] and [CO32-] in:

1. The case where the slurry is consisteing of CaCO3 + water only.

2. The case where the slurry consist of CaCO3 + CaSO3 + water.

3. The case where the slurry consist of CaSO3 + water only.

Yeah, am an expert in that area. I did Industrial and Production Engineering (B.Sc) and Agricultural & Environmental Engineering (M.Sc). Production scheduling is my core area.

Attached articles may be useful to you

I support both opinions by Martin and Ignatius, but note that in enzymology, specific activity is total enzyme activity divided by the total protein

Hi,

Please use DIgSILENT POwer Factory and Please see this link:

When I had to reduce CuO into Cu powder, I used 550°C, and it was perfect. As your H2 is not pure but diluted in Ar, it'll take a bit longer, but it mainly depends on how much CuO you have to reduce.

Alain

This calibration requires in the simplest way a minimum of two solutions: the first containing A alone at known concentration that its absorbance will be read at the two wavelenth to determine k_A1 and k_A2 , and the second containing B alone at a known concentration to determine k_B1 and k_B2.

There are several papers for evaluating this problem. Please, have a look some manuscripts at Attachment.

The following links are useful: