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Process Engineering - Science topic
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Questions related to Process Engineering
I have completed my bachelor in Food and Process Engineering. I am enrolled in a Masters of Engineering in Food Science and Technology course in South Korea. Recently I am exploring labs for my upcoming PhD career. I want to know in which departments other than food science/engineering/technology, we food science graduates can enrol for PhD. My specialisation is food chemistry.
To estimate the production costs of the chemical process plant, these are the preliminary estimated data. This helps the process engineer to make a decision among the alternatives.
What do you think?
Nowadays, chemical process simulation is applied in almost all sectors of Chemical Process Engineering. In general, it is used in almost all engineering fields. It is the inevitable part of disciplines from process design, research & development, production planning, optimization, training & education to decision-making which makes it one of the most important disciplines of engineering. A wide palette of simulation solutions is mentioned below.
If it would be okay, I would also like to who its manufacturer is and/or a specification sheet of that cooler. Thank you so much!
Hi, I am a chemical engineer graduate working as process engineer. Now a days, there is increased buzz about process plant automation, industry 4.0 and a greater push towards IoT, Cloud DBMS. As a process engineer how should we equip ourselves for this? What are the skills to develop in software aspect in this regard?
Could TOF be affected by any catalyst properties or reactor conditions? Please share more light on the choice of your answer (other than Yes/No) and if possible provide supporting materials. Thank you all.
We measure VLE in a kit with automated pressure control which make it very easy to do isobaric measurements. However in many cases isothermal measurements are preferred but these take a long time. You have to set a pressure which you think will give the correct boiling point, allow the system to equilibrate then adjust the pressure and repeat until the desired boiling temperature is achieved.
I want to install an automated control system which uses the temperature as a set point and continually adjusts the pressure of the system to achieve it. This would save a lot of manual intervention and improve the rate at which we can produce data.
Does anyone have any experience of doing this? What equipment/supplier would people suggest?
Vapour Liquid Equilibria
Most of available scale-up rules for dry powder mixing/ blending operation are applicable for geometrically similar equipments. Considering, equipments unavailability, sometime a blender with geometrically not similar is proposed for scale up batches. In such situation, how to determine different process parameters associated with blending unit operation?
I'm looking for correlation for density and viscosity of sodium hydroxide in function of concentration and temperature in range of 0-140 degrees Celsius?
If we fabricated a bench scale chemical process, will it give the same characteristics as of the production scale one?
We are plannig to make a graduation project that is based on the application of advanced control (fuzzy,neural) in the process engineering (specially, Ethanol fermentation from molasses). We thought that fabricating a bench scale process will give similar data, charactristics and measurement as the production scale, correct us please?
I plan to used a Bourne reaction system or similar to study reactive mixing. I wish to vary the viscosity of the system between experiments to understand how the viscosity influences the reactive mixing. This could normally be done using different concentrations of CMC or other additive. However during the Bourne reaction systems a neutralization reaction occurs resulting in change in pH which affects many additives and alters the viscosity.
Does anyone know a compound which can be used to increase the viscosity of an aqueous solution such that the viscosity is stable over a range of pHs?
Spreadsheet has been found in solving process engineering problems and its built in function capabilities, make data manipulation much simpler and faster.
I have used appropriate references for all the values and inputs that I have used for simulation. Please kindly help me out. I have been working through this for quite sometime.
I used unisim for carrying out this. File is attatched below if anyone is free to debug.
I am trying to design a counter-current heat exchanger that uses saturated steam at 100C to heat a process fluid from 18C to 40C of known mass flow. I need to determine the mass flowrate of steam required but this is also dependent on the condensate outlet temperature.
What is the best approach?
A. Fix the outlet temperature at 18C (Assuming the steam condensates and reaches the process fluid inlet temperature.
B. Fix the outlet temperature at 100C (Assuming only condensation occurs)
C. Fix the mass flow and determine an outlet temperature?
Or is there a way to simultaneously determine both?
What are the trends of research in chemical engineering in general and process engineering in particular? And what are the skills needed to master (modeling , data analytics , softwares ... ) in order to not be left behind in the future.
Thanks in advance
if I want to set up a process which wants to manufacture molecular Antibodies and I want to separte them from cell debris, DNA etc. as a first separation step, are there any general criterions with respect to the following downstream processes in order to decide whether the product should be in the upper or lower phase? For instance if I want to do Hydrohobic Interaction Chromatography as a next stept, I guess it would be wise to let them go to the lower kosmotropic salt phase, since HIC starts with a kosmotropic buffer. Do you know any other other similar general rules?
I added the equation about it here.
I'm stopped since I failed to calculate wave impedence.
Especially, relative permittivity and relative permeability are big obstacles for me to solve.
What I'd like you to do for me is not let me know how to calculate easily(of course, I'd thank you for it),
it would be even very thankful to you if you share me with books addressing this, with book names together.
Thank you for reading my question. I hope you help me.
How does inner vortex creates upward flow while outer vortex doing downward? what is diference between them? why flow is upward in inner vortex?
I have a reactor (reactor 1) that contains a slurry, and I need to pump the liquid from reactor 1 to another reactor (reactor 2) while keeping the solids in reactor 1.
We have tried attaching a filter bag to the end of a pump to try pumping it through, but the filter has generally been ineffective. Usually, it gets clogged up by the solid material and stops the flow. Another challenge is that the liquid is carbonated/bubbly, which also to some extent seems to impede the flow.
What are some good solutions to this? If we were to scale this process up I would imagine using some type of belt filter, but that doesn't seem feasible at this scale as the reactors are only about 15 gallons.
Dear all, I am looking for a safe screw lubricant that could apply on the medical implant and device production unit that work around 160oC to 500oC. I have found some PFPE, synthetic hydrocarbon and Silicone base lubricant for only medical device but not the production unit.
I wonder is there any specific lubricant for the medical implant and device production machine that could use under high temperature. Have anyone study about it?
BSc. in Mechanical Engineering from Bangladesh ( 63.4 %)
MSc. in Process Engineering and Energy Technology from Germany (ECTS Grade : 2.0 - Good )
Working Experience: 3 years in Manufacturing Industries
Research Experience: 1.5 years in Diesel oil desulphurization.
Experience: ANSYS Workbench ( FEM AND CFD) , ASPEN plus, SOLID WORKS, and DOE
Research Interest: Fuel and Energy, CFD, Thermal Separation and Chemical Thermodynamics.
Hello, as part of my research I will be looking at stresses in wastewater treatment processes. I would welcome any contributions to the survey I have produced (Below). This will give me a valuable insight into the perception of process stress for wastewater treatment processes. https://www.surveymonkey.co.uk/r/NRPTB8G.
From the results of ASPEN Plus simulation I came to know the Top four gases from the last RGIBBS reactor. Can I remove one gas separately from the reactor before the last one. How to deal with this ? As I just draw stream from the second last reactor its value become zero. But I know from the simulation result that gas value is not zero.
I'd like to share a question that has been puzzling me for a long time now:
It is common to use the assumption that a partially filled cryogenic tank is a volume in vapor-liquid equilibrium (VLE).
How does this assumption hold ?
Is there a kind of Biot number one could use to justify this key hypothesis ?
Based on observations, some zonal models consider the temperature isn't homogeneous between the vapor and liquid phase.
I guess the size of the tank matters.
I am looking for a formal way to justify the VLE assumption (more or less like when using the biot number to set a thermally simple model, due to uniform temperature fields inside the body).
Any clue on this would be of immense help to me.
Key words: LNG, cryogenics, tank, thermal model, lumped thermal model, process engineering.
I am process engineer at wastewater treatment plant that mainly treat organic matter, Nitrogen, and phosphorus biologically, (Bardenpho process (Five- Stage).
I have notice the presence of Algae at the effluent of secondary sedimentation tank.
What is the causes of presence Algae at the effluent of Advanced WWTP ( combined removal of nitrogen and phosphorus biologically ?
Any one can help me in the process of such type of treatment process?
Any reference that can help me in operation and processing of (Bardenpho treatment process (Five- Stage).
#wastewater #treatment #wwtps #advanced_treatment #nitrogen_removal #phosphorus_removal #five_stage #bardenpho_process
Just by knowing the total amount of gas supplied, what the main assumptions that should be considered in such this case to complete the sizing design.
If I considered typical values, can my calculations will be done in a logical manner?
Dear researchers and professors
I have difficulty to determine the exact amount (kg/hr) of PZ, H2O, CO2 in LeanIN into absorber column. If the given values are following
PZ 5 m (molality (mol/kg H2O))
mol CO2/ mol alkalinity = 0.236
LeanIN flow rate is 3180 kg/hr?
My concern is mainly the right calculation method for the certain problem if anybody can be helpful?
I have found the following rate kinetics for the following reaction. As you see, the reaction is reversible one in which Xylene disproportionates and toluene and trimethylbenzene form ( r is reaction rate for xylene ).
If in the reactor, the reaction occurs in reverse direction such as toluene and TMB react and form Xylene, is it possible to use the same rate kinetics? Should I change some parameters? or this rate is OK for both reaction's direction?
( work done by André Luís Alberton )
Thanks in advance.
I am trying to design a distillation column, and I am not sure if the value I obtain for reflux ratio is normal or not.
I need the dimensions of tatoray reactor such as diameter, height and so on. Could you please provide me with related information. Thank you in advance.
How is possible to make a stable emulsion(that don't separate as usual by gravity force) of water in oil with a wide range of API gravity?
which component except (Aniline or gasoline) we can use to get close to spec of crude oils in upstream operations?
Does this process(make w/o emulsion) have special mixer(like static mixer)?
I am currently running a constant potential chemical synthesis experiment using a three-electrode cell and a potentiostat. I’m currently making a few hundred of mg of material a time. I’d like to scale up the process to produce grams or even kgs to hopefully make it industrially viable. However, I think my potentiostat current limit is 1 A, too low for multiple gram scale synthesis. I have a DC power supply with a 10 A limit, but understand that it’s hard to control the potential using the DC power supply.
So I wonder if it’s possible to do a controlled potential on a very large scale? I read a textbook that says that industrial potentiostats are cost prohibitive and unavailable (Goodridge and Scott 1995, Electrochemical Process Engineering). But maybe times have changed since then.
If I need to use a DC power supply, should I try to switch the experiment to constant current/galvanostatic mode? Or is there a way to still do a similar, constant potential experiment with the power supply. Even if I can't control the potential, I wonder if there is some way to approximate constant potential conditions.
designing an apparatus we need :ASME codes and also a manual article or book to realize more about this device.
Is it possible to get data sheet about Dehydration from upstream oil refining?
In an adsorption process, for linear driving force (LDF) model dq/dt=K(q*-q) and K=15De/d2 .
De=1/(1/Dk+1/Dm) (as a simple basic form).
According to this calculation I found De~9 (I also considered porosity and tourtosity) but according to experimanetal data, De`0.06.
Is there anything wrong in equation I use?
Please send me any refernece or book you think is useful.
I am working on the modeling of an extension of the BSM1 considering an addition of components and some changes in the processes considered too, the problem is that although the kinetic equations seem to be right, the model is not presenting logic results for effluent and reactors, I don't know where or how else to check. Please, someone who have worked on this before could help me on how a proper extension of BSM1 should be made?
In a rotary kiln, changes in flame temperature profile has a huge effect on melting rate and kiln efficiency. I would like to know about flame temperature changes with time along the kiln.
Thanks in advance
Hello all, could you tell me any chemicals that has similar reaction properties to Zero Valent Iron (ZVI) Fe0. it is transition element. and very reactive chemical ( catalyst. Thanks
i am think if i shall do comparative studies for environmental remediation and addictive in process engineering.
Have you ever used Wilcoxon signed-rank test, and if so, in what cases?
Currently, I analyze the results of copyright scheduling methodology, which aims to minimize makespan (for job-shop), and I intend to compare the data obtained using the methodology of the results achieved using the selected rule priority.
What are you experience with Wilcoxon signed-rank test?
I need to determine if the system Fe2O3-ZnO make a solid solution or there are only the phases Fe2O3 an ZnFe2O4
I have a complex TRNSYS model of a solar plant with a multi-zone building
(Type 56) which was designed in TRNSYS 16. Since we have switched to TRNSYS
17, I would like to be able to continue using this model.
I've tried to open the model directly in the new version, but it crashes
after my attempts to update the project. I guess the major problem is
originated by the Type 56, as far as I understand, it suffered some changes
from the last version.
Did somebody experience this situation and how did you solve it? I would
appreciate any ideas.
I am using polyacrylamide gel electrophoresis. I want to analyse 700 kDa aggregates. I don't have gradient maker. I have tried different concentration of (stacking gel and resolving gel) as (3%,5%) and (3%,6%) but I have not observed any band. Can you help me with gel and concentration I can use ?
I have Diesel Oil with 1.3% percent sulfur content. But I need to find out the anline point of diesel for evaluating ignition quality properties.
Chemical Engineering, Pharmaceutical Engineering, Downstream Processing, Purification, E.Coli, Pharmeceutical, Process engineering, Biochemical Engineering, Microbiology
I am interested to know what will happen if two reactors are operated in parallel (the idea is separate HDO and HC). Also I was wondering if the operation condition (i.e. pressure and temperature ) in reactor A and B will differ each other. Can anyone would like to share the challenge of the reactor design? And it possible to separated water coming from reactor A (HDO) prior to second reactor B (HC)? I would appreciate for your kindness and helpful. Thank you
I want to see the effect of temperature on intra and inter layer bonding. Please suggest
One of the vent gas stream contains hydrochloric acid and we are planning to dispose of it by burning it in a flare. Could anyone help me understand whether it will burn and what is the reaction and what will be the components of product of combustion?
I am having a hard time researching replacement devices for our current uncurlers because "uncurler" is not the industry name for the equipment. I have attched a photo of the uncurlers we use.
I will simulated the polymerization of lactic acid via lactide to poly lactic acid with Aspen Plus. In the aspen component databanks I do not find anything like this. What is the best was to handle this problem?
I am currently working on 1,5 hour lecture about aforementioned topic for my seminars.
I have found some general Polish literature about adsorption and several other publications, both in Polish and English, but I yet failed to find anything specific which would be accessible to students and for educational purposes.
I am interested in both process engineering and apparatus design, so if anybody knows some books/publications/other stuff, I would be very grateful.
i* is a diagram language that is originated in order to process engineering and analysis. In order to visually model the whole system, there is a need to understand (Baier et al., 2015):
• WHAT is done
• also WHY it is done
• as well as WHO is involved as stakeholders
• and HOW everybody's goal and intentions interact.
For modeling stakeholders relationships, i* was created to be an easily accessible modeling tool.
The software for drawing diagrams, which I downloaded form i* website, is not neat enough and the final graphic view is too messy.
Does anyone know another software or maybe online interface, that can help me draw i* diagrams??
I had discovered in 2005 that most used process management model was actually developed in 1920's as a product control model, as the concept of process was not present then. It was more like having trade-smiths, who would build things. To my knowledge, this product control model is called PDCA, which led to creation of cost of poor quality. While using the PDCA model, experts like Juran, Taguchi, Ishikawa and Deming tried to fix its weaknesses, which were not adopted for convenience. This whole concept of PDCA eventually resulted in a field of quality. It is due to poor design. With this mindset, I am interested in knowing if anyone is aware of the process models used currently.
Looking at impact on conductivity of epoxy prepolymer mixed with various types of nanoparticles before curing with an amine
In decentralized control of multi-variable processes techniques such as RGA, SVD, HIIA etc. are recommended for analyzing input-output variable pairing. Is any of these tools are industrially applied ? or Industrially, is it still the experience and intuition dominates ?
I am looking into ways to modify a current design of steam spargers. Currently, we generate "lazy" steam for our process and want to improve application of the steam. The steam is applied pretty directly and I want to diffuse it and apply it over a wider area of our fabric.
Application is in the textile industry (dyes) with further reuse of H-acid. Generally, a hybrid membrane system(MF-UF-NF/BMED) will work to reach a clear H-acid brine, but I'm curious about the last step - the H-acid purification. Does NF can work well, or it is better to use a bipolar membrane? Maybe a kind of hybrid ion exchange-nanofiltration system?
Do you have any different opinions or some practical experience to share?
I'm trying to construct a high pressure containment vessel (pressure reactor) (Up to 2000psi) and probably small enough to be fitted in a tube furnace.
Currently I'm using Swagelok SS 316 union and caps, but it is quite expensive and the screw mechanism for fitting is not an effective way because we are not able to re-use the reactor cells. (Forcefully opening them breaks the caps)
Looking for lower cost alternatives! Our aim in here is to design/make a pressure containment vessel which can able to withstand the internal pressure(up to 2000 psi) from our autogenic system.
I've attached an image for our current reactor cell. Thank you.
My query is how to design a packer type gas anchor for SRP wells taking into consideration heavy oil (api=16 deg and vis.=600 cp)
1. what should be the length of chimney/small dia pipe?
2.what should be the spm ?
So I am trying to ramp up production of some oxide powders. I have used a centrifuge in the past, with the capability of using 15ml tubes in the centrifuge. These 15ml tubes are way too small, and would increase the washing step by many hours. I have thought about synthesizing in a large beaker, allowing the precipitate to sink to the bottom, and then sucking out the supernatant. And then washing 2-3 times in this manner. Then spreading the precipitate on a drying dish, and allow to dry. Seeing as I am using a cerium nitrate in my synthesis, i must get all of it out so as to not risk release into the environment. So this manner may not be worth the risk.
I would like to upgrade the centrifuge to be able to hold larger tubes, but the centrifuge we have at our company has been withdrawn. Seeing as I would like to avoid purchasing another centrifuge just for this; is there another route that I may be over looking? I would also like to avoid gravity filtration, since we do not have the large enough glassware to make this process much faster than using the 15ml centrifuge tubes.
Any help will be great. Thank you!
Currently, I work on hydrocracking of Methyl ester with addition of hydrogen gas into the reactor (mainly Trickle bed or fixed bed reactor). The flow rate of liquid is 128.1mL/min at 1 bar and temperature 85C flowing into the reactor, and hydrogen gas is unknown flow rate. Can somebody help me to calculate hydrogen gas flow rate at 40 bar and temperature at 25C and H2/Oil ratio is 500Nm3/m3 or 500NI/I?
Similar work has been done by: Pasiuk-Bronikowska, W., & Rudzinski, K. J. (1991). Absorption of SO2 into aqueous systems. Chemical Engineering Science, 46(9): 2281–2291.
If I do the ball milling of Ni50Mn45Sn5 (atomic %) for 20 hours in presence of Toluene as process controlling agent. Argon flow and vacuum were not maintained during milling.
(i) Will the outcome alloy be a single phase or not?
(ii) What phase (Austenite or Martensite) will form just after the ball milling?
(iii) If I want to go for magnetic measurements, Do I need to anneal it first? else I can go for magnetic measurements without annealing?
(iv) If annealing is necessary then what should be the annealing temperature and time?
What is difference b/w ASTM D3172 and ASTM-D5142 methods for Proxmate analysis for coal of lignite type?
whose method is accurate and how much error between them of these two methods?
Questions in Your Topics. Available from: https://www.researchgate.net/topics?askQuestion=1&tpca=1 [accessed Mar 20, 2015].
When dealing with enzyme production, we have a certain cell mass at the end of fermentation, which is defined as yield. Now, i sonicate to get the crude enzyme supernatant and find the activity. If i divide this activity by previously defined yield, can it be called specific activity? If not what is it called? Just a heads up, I am a process engineer and not a molecular engineer. Any publication supporting your explanation could be of immense help :)
Can anyone provide a tutorial on dual fuel engine in GT-POWER software with constant RPM and constant load. fuel injection control in GT-POWER for CI engine.
I have infiltrated CuO into SiC foams (40mm dia, 10 PPI). Now I need to further need to reduce CuO to Cu. Does anyone has done this reduction. If so, then what's the decomposition temperature and the time up to which it was kept in the furnace and the setup. As of now I'm thinking of reducing it using Ar (5% H2) gas as catalyst in a furnace chamber at about 450-600 C. I'm not certain about the temperature, so kindly help me out in this.
For the following bracketed paragraph how one can formulate the experiments(i.e. how many and with which combination the dyes should be mixed) with binary dye solutions for calibration. I have seen lot of research papers, all those give only formulas and explanation of the terms in the formulas but they are not mentioning any clue about the experiment.
(In a binary system with components A and B, the measurement would be carried out at their maximum absorbance wavelength λ1,max and λ2,max, respectively, giving absorbances of A1 and A2. The dye concentration of the particular component could be determined by the following equations
CA = (kB2A1 -kB1A2)/(kA1kB2 -kA2kB1)
CB = (kA1A2 -kA2A1)/(kA1kB2 -kA2kB1)
where kA1, kB1, kA2, and kB2 are the calibration constants for components A and B at wavelength λ1max and λ2max, respectively)
Respected EEG experts,
I am trying to study the dynamic difference in topography between different states, e.g. resting vs. gaming tasks, and attached is a schematic illustration of experimental design for your understanding. (Between each state, say R1 and G2, there was a short pause in the recording for preparation so that the data I finally have is 7 ".set" data for each state)
I filtered the data to four bands (delta, theta, alpha, beta) by using EEGLAB. Then, I windowed the time-series data to see the dynamic change with length 30s and slid it by 2s (sliding window analysis).
I wonder if I can see the topography of each windowed data for each band so that I can study the developing topographical changes and investigate their spectral differences.
I know that EEGLAB provides the plot for EEG channel spectra and maps by using "spectopo" function. Still it gives the topography in separate frequencies. What I want to have is to see the averaged topography over whole bandwidth.
Is is possible? or Is this unnecessary so that I am okay to only see the topography at the middle point of the bandwidth.
One more question for the experiment itself.
During gaming state, subjects had to open their eyes and play the game. As I am not the expert in EEG but just a signal processing engineer, I am worried at the effect of lights to the data.
Would it be the problem to say that the differences in topographies of each band are due to different brain activities for each state? (Generally alpha wave comes while resting and beta is induced by alert ..)
If so, what kind of amendments or process I can do to avoid the problems? (I cannot re-collect the data, I got this time series data from the other researcher)
If you can comment me with the other problems I have not mentioned here, please let me know (in data processing, collection scheme whatever).
I want to link matlab with chemical process eng software "Aspen Hysys"
I found I should use OLE automation for this purpose
but I don't know exactly what's that?!
I have a composite of kaolinite(80%) and illite(20%), is there any method to separate or upgrade the illite from this composite? Please give me a detailed method which I can follow in labl. Thanks a lot