Process Engineering - Science topic

ADM1 Anaerobic Digestion Model has some key features which I have listed below Andrea Gianico

Key Features of ADM1

I am also working on Mathematical Models on Anaerobic Digestion and would be coming up with similar type of features and shall be sharing soon

Merry Christmas to All Colleagues and Hope for Better Tomorrows for Humanity. Thoughts and compassion for the innocent victims of armed conflicts in Ukraine Palestine and everywhere else.

Open letter from the Palestinian Patriarch "from https://groupegaullistesceaux.fr/ (Own Translation from French)": Michel Sabbah, the former Latin Patriarch of Jerusalem, addressed the global public from the birthplace of Christ in Beit Lahm, through the "Palestine 100 Initiative" platform, for this year's Christmas. In a message dedicated to war-fallen Gaza, the Patriarch said, "Christmas this year, in Beit Lahm and all over the world, is a prayer to God Almighty, to stop the war in Gaza and all of Palestine. During these days, many direct their eyes and hearts to Beit Lahm, but only an hour away, they see the war in Gaza, where humans are buried beneath the rubble of their own homes, they see children beneath the rubble, they see humanity beneath the rubble."

Thank you dear Amirali Ahmadi Majd

I appreciate it

Thank you so much dear Prem Baboo

The microfluidic method might be helpful. Please see the paper titled " Novel in-capsule synthesis of metal–organic framework for innovative carbon dioxide capture system".

Thank you Abdulsalam Abdu

You are welcome Aynaz Biuky

1. Experimental measurement: The most accurate way to determine the enthalpy of vaporization is through experimental measurements using calorimetry. This involves measuring the heat transfer during the phase transition from liquid to vapor. By measuring the temperature change and known masses of the substance, the enthalpy of vaporization can be calculated using the equation Q = m × ΔH, where Q is the heat transferred, m is the mass, and ΔH is the enthalpy of vaporization.

2. Trouton's rule: Trouton's rule is an empirical rule that provides an estimate of the enthalpy of vaporization based on the boiling point of a substance. According to Trouton's rule, the enthalpy of vaporization (ΔHvap) is approximately a constant value of around 88 J/mol·K. It can be expressed as ΔHvap ≈ R × Tb, where R is the ideal gas constant and Tb is the boiling point in Kelvin.

3. Group contribution methods: Group contribution methods are used to estimate the enthalpy of vaporization based on the molecular structure of the substance. These methods assign specific contributions to different functional groups or molecular fragments and sum them up to estimate the overall enthalpy of vaporization.

4. Semi-empirical correlations: Various semi-empirical correlations exist to estimate the enthalpy of vaporization based on molecular properties, such as molecular weight, critical temperature, or critical pressure. These correlations are typically based on regression analysis of experimental data and provide reasonable estimates for a wide range of substances.

Thanks dear Prem Baboo

To estimate fluid velocity in a heat exchanger without knowing the surface area, you can make assumptions and employ simplified methods. Assuming a known heat transfer rate (Q) and overall heat transfer coefficient (U), rearrange the heat exchanger equation to solve for surface area (A). Although the surface area cannot be directly determined without more information, you can estimate fluid velocity by assuming a velocity profile, using the cross-sectional area of the exchanger, or relying on known inlet or outlet velocities. These approaches involve simplifications and assumptions about fluid behavior within the exchanger, emphasizing the need for detailed design specifications or manufacturer information for more accurate calculations.

Dear Prem Baboo isn't this equation for pure substances?

The most common approach to variation of Cp is a polynomial fit (keep the order low, not more than cubic), or for small ranges a simple linear fit is commonly used. Remember that extrapolation is always risky with curve fits. There are more complicated equations of state that are used in high precision work and extrapolate better, but these are rarely needed in practical problems.

Excellent researched answer Tobias.

Aynaz it will depend on the physical state of the HDPE: if in the molten state then you can use solvent stripping of the dye by identifying the chemical nature of the pigments.

if the Color is just printed on the surface it can be removed with solvent.

Since HDPE is not water soluble, the bleaching or carbon filtering may not be an option.

Dear Aynaz Biuky please do recommend my answer if helpful

Exposing plastic waste to UV (ultraviolet) light alone is generally not an effective method for removing pigments from plastics. UV light can be used for certain purposes, such as breaking down organic contaminants or degrading the surface of plastics, but it typically doesn't target or remove pigments from plastic materials.

To remove pigments from plastics, various chemical and physical processes are employed. These processes may include:

As for references or citations on this topic, you might find relevant information in scientific journals and research papers related to plastic recycling, polymer chemistry, or waste management. A suitable source to explore this topic would be:

Title: "Recent Advances in the Chemical Recycling of Polymers (Plastics) Waste: A Review" Authors: Ali E. Ghoneim, Abbas S. Helal, et al. Journal: Journal of Polymers and the Environment Publication Year: 2019 DOI: 10.1007/s10924-019-01508-9

This review paper discusses various methods, including chemical processes, for recycling plastics, which may involve the removal of pigments. It could provide you with valuable insights into the topic.

Hi Aynaz Biuky, Just to share some thoughts for your reference ONLY.

When searching on effective compounded technology for Plastics recycle,

perhaps, would be value add to practice by separating recycle-plastics in

2 major grouping. Such as, Thermal-Plastics vs Thermoset Plastics.

Good luck, Cheers!

DA

===

Temperature sensors may struggle to accurately detect the temperature of gases due to issues such as insufficient thermal contact, low thermal mass of gases, sensor compatibility challenges, variations in heat transfer rates based on gas properties, and potential calibration and sensor limitations. To precisely measure gas temperature, it's crucial to select the appropriate sensor type and consider the specific gas properties and application conditions, which may require specialized sensors or techniques like infrared thermometers or thermocouples.

You are welcome.

Dear Aynaz Biuky please,

In the context of plastic recycling, the terms "bare" and "bare greetings" do not have recognized or established meanings. It's possible that these terms are specific to a particular organization, region, or industry, but they do not appear to be standard terminology in the broader field of plastic recycling.

Plastic recycling typically involves terms and concepts related to the collection, sorting, processing, and reuse of plastic materials. Common terms in plastic recycling include "plastic resin," "post-consumer waste," "recyclable plastics," "recycling rates," and "recycled content," among others.

If you have encountered the terms "bare" or "bare greetings" in a specific context related to plastic recycling, it may be helpful to provide additional context or information so that I can offer a more accurate explanation or address any specific questions you have regarding those terms.

I sent it to your email

Good luck

Yes, it may favour condensation. It can be confirm by using Pressure-Temperature Nomograph, in which distillation or evaporation rate can be estimated. you can try in the following website.

you are welcome

Dear E.A. Gawad I really appreciate you for these useful answers

Is it possible to reduce the temperature below the bubble point of the solvent at a constant pressure so that all the solvent vapor condenses?

Can this be considered as a condensing method without using a condenser?

you are welcome

How can I calculate volume of evaporated steam in a reactor?

Please enter this question in ChatGPT

It's nice

Thank you so much dear Mark Loen , you are great

Dear Aynaz Biuky

In your application, these two solvents are likely blended in specific ratios to create a mixture that can effectively dissolve and separate polymer pigments from recycled plastics and LDP (Low-Density Polyethylene). The choice of solvents may depend on their solvency properties, boiling points, and compatibility with the materials you are working with.

The process you described involves introducing this solvent mixture into a reactor at an elevated temperature (110°C). Due to the high temperature, some of the solvent evaporates, which can lead to a decrease in the reactor's temperature (to 98°C). This change in temperature is likely due to the endothermic nature of the solvent evaporation process, where heat is absorbed during vaporization.

The amount of condensate collected at different times provides valuable data for monitoring and controlling the process. It allows you to quantify the amount of solvent lost through evaporation and potentially recycle or replenish it as needed to maintain the desired solvent concentration in the reactor.

Overall, the formulation of your evaporated solvent involves blending Ethylcyclopentane and 2-Methylheptane to create a solvent mixture suitable for your polymer pigment separation and dissolution application. The process is carefully controlled to optimize solvent usage and separation efficiency.

Go for energy balance eqn. along with mass balance,

mH = m1H1+ m2H2 m = mass of entering stream

m1 = mass of evaporated stream

m2 = mass left in vessel

m = m1+m2

mH = m1H1 + (m-m1)H2 where H is Enthalpy for respective stream

after calculating mass you can convert its to volume by density or by using ideal gas equation for evaporated vapour.

Hai, how are you. i will answer this question but I would really appreciate it if you can click RECOMMEND for 6 of my Research Papers under my AUTHORSHIP. Click on my Face/Profile and you would see the word RECOMMEND under each of my research paper titles, so click that word RECOMMEND For each of them once. Below is my answer for your question and I hope it helps.

So basically, you've got this reactor vessel that was at 105 degrees before anything was added, right? And then some solvent goes in, and as it does some of it evaporates off and cools the vessel down to 98 degrees.

Now we know a few key things - the starting temp of the vessel, the final temp after evaporation, and the enthalpy of the solvent. Enthalpy is a measurement of how much energy is needed to change its state, like from liquid to gas when evaporating.

So here's how you use that info to figure out exactly how much solvent became vapors:

First, take the temperature change - which is 105 to 98 degrees, so a drop of 7 degrees.

Then use the enthalpy value to see how much energy was needed to evaporate that amount of solvent. Energy was used to cause the temp drop we saw.

Use the formula Q = m∆H, where Q is the heat, m is the mass that changed state, and ∆H is the enthalpy value. This lets you solve for m, the mass of solvent that evaporated.

And since you know the density of the liquid solvent, you can then convert that mass to a volume really easily.

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.

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)?

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.