Thorntons PLC Strategic Analysis Assignment Example | Topics and Well Written Essays - 4000 words

Thorntons PLC Strategic Analysis - Assignment Example Thornton's PLC has 230,000 representatives worldwide and works 520 manufacturing plants in 82 nations. Thornton's PLC major social effect is to improved ways of life among a huge number of individuals through formation of profitable, maintainable monetary turn of events. Thornton's PLC brands demonstrated the most grounded development, at present presenting deals close on 700 million liters in more than 20 nations. Thornton's PLC administration is gathered in Europe (districts where monetary hazard is restricted, salaries are high and development possibilities are vigorous) through the advancement of solid brands, the HOD business, and acquisitions that offer genuine open doors for collaboration. In 1999 Thornton's PLC worked from 509 manufacturing plants around the world, 424 are in extraordinary chocolates and toffee items. Extraordinary chocolates represented 28% of 1999 incomes; 26%; chocolate and dessert shop, 54% are in toffee. With a net benefit of 4.724 million, up 12.3 percent over a year ago, and with huge, expansive based improvement in all significant presentation pointers, Thorntons PLC thinks back on a record year 1999. The net revenue arrived at 6.3 percent (5.9 percent in 1998) on merged deals of 74 660 million (1998: 71 747 million). The exchanging benefit of 7 914 million expanded by 11.8 percent, an edge of 10.6 percent of deals (9.9 percent in 1998). EBITA (Earnings Before Interest, Taxes and Amortization) improved by 12.4 percent to 8 298 million (1998: 7 382 million). These considerable enhancements mirror a progression of measures assumed control over the previous years, contacting practically all exercises (Mitchell, 2002). Smoothing out the business portfolio, expanding operational productivity, modern rebuilding and progress in buying and gracefully chain the board empowered the Group to accomplish higher benefits, edges and profit for contributed capital. Thornton's PLC additionally made the fundamental speculations to guarantee future top-line development by putting resources into new items and fortifying its brands and pieces of the pie. During the principal half of 2000, Thorntons PLC accomplished a noteworthy increment in the two deals and overall revenues. Table shows that united deals developed by 9.9 percent to 38.8 billion, with genuine inward development quickening to 4.5 percent, contrasted with 2.1 percent in a similar time of 1999. Exchanging benefit added up to 4296 million. This speaks to 11.1 percent of deals against 9.8 percent for the first 50% of 1999. Net benefit expanded to 2798 million or CHF 72.7 per share, bringing about a net revenue of 7.2 percent (5.9 percent in the principal half of 1999). The solid deals execution mirrors the Group's accentuation on inner development. The edge upgrades result from progress accomplished in improving operational productivity, the smoothing out of the Group's item portfolio, modern rebuilding and some lower crude material costs which had the option to counterbalance higher bundling costs. Inner Growth and Currencies Push Up Sales Consolidated deals, at 38.8 bil lion, were up 9.9 percent. At tantamount structure (barring acquisitions and divestitures) and at consistent trade rates, deals rose by 4.9 percent (see table 1). Table 1. Thornton's PLC Figures for 1999-2002 Thornton's PLC Annual Report 2002 2001 2000(e) 1999(f) In a huge number of CHF (aside from per share information) United deals 89 160 84 698 81 422 74 660 71 747 EBITA 10 940 9 987 9 911 8 700 7 606 as % of

Managing Financial and Information Resources Coursework - 1

Overseeing Financial and Information Resources - Coursework Example Net overall revenue indicated an upward pattern all through the period; it expanded from 57.76% in 2011 to 63.31% in 2013. This suggests the organization procures more pennies per dollar of income, and this is good since more benefit is created to take care of non-creation costs. Working net revenue expanded in 2012 however diminished in 2013. Despite the fact that there is a decline, the organization is as yet productive in light of the fact that it is creating enough cash from its tasks to pay for both variable and fixed expenses. As a rule, the company’s gainfulness is improving as showed by the expansion in its benefit proportions (Kimmel et al 290). Proficiency proportions show how the organization is dealing with its liabilities and utilizing its advantages for create salary. Fabrique Aã ©rospatiale is generally effective in its activities. The indebted person days expanded from 59.33 days to 59.79 days in 2012, and further diminished impressively to 34.31days in 2013. This improvement in account holder days infers that the company’s productivity in gathering its receivable expanded (Kapil, 128). The organization is, along these lines, exceptionally fluid since it requires some investment to gather its receivable subsequently increment in effectiveness. Leaser days expanded from 91.56 days to 97.5 days yet diminished to 78.43 days. This demonstrates brief installment to leasers. This decrease infers that the organization is attempting to exploit the rebate that the providers is advertising. Fabrique Aã ©rospatiale is wasteful in dealing with its stock. It has higher estimations of stock days that isn't positive for the business. Stock days expanded from 134.21 days in 2011 to 142.5 days in 2012 yet diminished to 116.14 days in 2013. Despite the fact that the abatement is a decent marker, it is exceptionally negligible. The organization has higher days’ stock close by. As far as liquidity, Fabrique Aã ©rospatiale is exceptionally fluid. The two its basic analysis proportion and current proportion have values more prominent that one for all the years. The organization can meet its close term

March Questions Omnibus 1

March Questions Omnibus 1 applicant asked, when r u goin to answer the questions?? Sorry, things are, as you might imagine, quite busy around here. Ill do my best to answer them now Matts Helper asked, What did you major in, when you were at MIT? I spent some time with both Architecture (Course IV) and Math (Course XVIII), but ultimately I graduated with a degree in Management Science (Course XV). Saad Zaheer wrote, i was really wondering last night about ur watching bollywood movies; well it implies that u can understand some Hindi and Urdu (pakistani language) is quite similar to Hindi. even if u watch translated into english ones, i would recommend u try to learn some hindi and of course urdu know how follows itself. its grt to know that becuase u will have a vast eastern culture to discover, and the eastern culture is awesome to discover. Well, Im picking up a bit of Hindi here and there maybe, if I get some free time, Ill actually take a Hindi course (though Mandarin is up next for me). hedwig asked, i was just wondering, since i had my sister do me a favour by filling out the technical details in the MIT admission form (like my achievements etc.) would they think that one of the essays which i typed was written by her or somebody else (since i also included a completely optional essaywhich was naturally in my own handwriting) or would they give me the benefit of doubt and accept that it was indeed I who wrote the essay. We generally give people the benefit of the doubt, as Im sure we did in your case. hedwig also wrote, Yeah, i almost forgot; since January i have been trying to contact the admissions office via email to give them some background information about me and my school and that I was chosen to represent India at GYLC(though i wont be attending due to financial constraints) but i have received no reply; is that normal?? Also since i could not give an interview due to the ongoing school exams(though I never told this either to the EC or anyone else who is associated with the admission process) , Id like to ask: if somebody does not give an interview does it reduce his chances of getting into MIT?? and if so, then by how much? Im sure your email was filed by the email staff. As for the interview, we do not assume that international applicants can always complete it, but it can definitely help in the cases when it is available. Aarthi wrote, I think Ive made one of the biggest mistakes of my life. While looking over my MIT essays today, I realized an egregious error in one. I really do think it could have made a difference in the outcome of my decision, and so immediately sent an e-mail to the Admissions Office. At this point, will you all ever consider this revision?? It is highly unlikely that an error in your essay would make the difference in a decision. I wouldnt worry. andrew wrote, Would you say that March 15 is a reasonable estimate [for decision letters]? I cant provide estimates now, but when we mail, youll see an update on this blog. Sloanapplicant wrote, Would you say that, by the end of the selection process, you are at least minimally familiar with all of the acceptees? Well, maybe not all of the acceptees, but during Campus Preview Weekend, I do get to put a lot of faces with their familiar names. Its nice =) Carlos wrote, Matt, just a question I heard somewhere that International Students will be able to check their decision using a special web page when they are released. Is this really true and if it is, where we can find the adress to that website. We will mail all decisions on the same day, and we prefer for all applicants to receive their decisions by mail. No decisions will be available online. A Regular Decision Applicant wrote, Is there any way to find out an applicants decision before mid-March? Someone from my high school found out her decision already, and she said that someone she knows in the admissions office told her. At this point, the only people who have been admitted are the 383 EA admits from December. No regular action admission decisions are final until they go out the door of the admissions office on the day we mail. The situation you describe does not sound credible for regular action decisions. A wrote, I was wondering if international applicants are also placed in the waiting list, exactly like domestic applicants? If so, how many applicants (international if possible) do you plan to include in that list? Yes, we do maintain a waitlist of international students, usually on the order of lower double-digits. SMer wrote, Just out of curiosity, what percentage of decisions do you estimate are reversed through this last part of the admissions process? I dont know. hedwig wrote, Id also like to know how many Indian students on average get admitted into MIT and approximately how many apply each year? and another thing, i dont know whether its just my computer that is acting up or is there something wrong with the contact link on your blog? everytime it tells me that there is some problem with the mail server Something on the order of hundreds of students solely with Indian citizenship apply each year, and in the past we have admitted on the order of mid-single digits have been admitted. Also, it appears the contact link for all sites on blogs.mit.edu is broken. Sorry. paul asked, can a research paper in an international journal gaurentee admission The short answer is, no, it does not. For a longer answer, read over my previous blog entries. mit_hopefulgirl wrote, Matt exactly how many internationals applied this year, and exactly how many is MIT intending to admit? I believe we received about 2200 applications, and I believe we will admit about 100 students. Transfer Student wrote, Matt, would it be possible for you to scan and post a E3 [summary] card for an admitted student and a rejected student (without names of course)? Sorry, thats not something I can do. sreraman wrote, I have submitted my research papers along with my application..May I request that it should be kept confidential,since it is not yet published We will keep your research papers and other aspects of your application private and confidential. applicant asked, how often do u admit people from this category [students who have both a low NI and PR, but the readers feel that the applicant would thrive at MIT and contribute to the community]?? sad applicant wrote, i think that i will not get into mit this year becozz of my low SAT scores(my gpa is excellent)!if you find a sense of resonance between an applicant and MIT, but not SAT scores will you ever give a chance to an applicant to write SAT and prove him/herself in may since ur class starts only in sep. MS wrote, I know a boy who got into MIT physics dept. inspite of his low GRE scores (1130)owing to his stellar research accomplishments..can v expect things like this to happen in undergraduate selection also??? Anonymous wrote, So you say that you admit people, not numbers, that MIT is self-selecting and that youd be hard pressed to remember a single applicants numbers.. does that mean that theres a certain cut-off where youd be considered competitive and thats it? A 1600 on the SAT is considered no better than a 1500, scorewise? See my earlier post on the topic. Generally, test scores beginning with the number 7 (SAT) or 3 (ACT) will put you within the range. Students should try to score above 650 on any individual SAT, though there is no minimum score for any test except the TOEFL. applicant for 2005 asked, I read this [description of MIT admissions process] in a college discussion website..is it true??? There have been some articles published about MIT admissions in various publications over the years, one of which I believe your post was based upon. Most recently, both MITs student newspaper and its alumni magazine published articles which were, for the most part, were accurate, though they talk about the process from a journalists point of view, and not an admissions officers. Im trying to do what I can to explain the process by writing this blog. applicant in distress wrote, I have a serious problem which could be solved only by you.I decide to update my information to MIT and also dartmouth.Hemce,i had 2 seperate cover letters,one for MIT and other for DArtmouth.I gave it to the faxing centre for sending the info.The man in faxing centre sent the cover letter for MIT to dartmouth to MIT and Dartmouth to MIT.. Its not my fault. Can you please help me!!!!!!!!!!! This isnt a problem. We expect that you are applying to other schools (we hope you are!); we dont imagine that you are only applying to MIT. Dont worry about it. Shahab Umer asked, Is it really that easy to select 100 international applcants from over 2000 in just one or two days? How many people are working with you? The international process has been going on for some weeks. When we start international selection, we will choose from several hundred applications after all of them have been reviewed. The usual set of admissions officers will be participating. Jeremy wrote, A small question that Ive been trying not to ask; I live in Europe, but applied as domestic because of my US citizenship. I have tried best I can not to overstate the grading difference and I wonder if that was stupid? Were pretty experienced with non-US school systems. For example, we know that getting a 20 in the French system is very different from getting an A+ in the US system. Im sure this was fully considered. parent wrote, Could you post a sample or two of the actual deliberations of the admissions committee on applications minus the names of course? How exactly do you decide generalizations and glorified principles aside? If you can post two examples of applications that were binned in widely differing cells and explain why they were admitted, and one example of an applicant in cell1 who was not, that should greatly help in understanding the process. Im sorry, that is not something I can do. parent also wrote, Do you document your decision of why you admitted an applicant, and why you rejected another? The standard response from the admissions officers upon inquiring why someone wasnt admitted, is that they have no idea and do not know what the committe was thinking at the time! How can this be? We do not document the exact reasons for our decisions. While we cannot recreate deliberations on each case, all decisions are thoroughly reviewed many times according to our guidelines during the process. Usually, theres no one reason why someone wasnt admitted. For the most part, our applicants are very qualified, and unfortunately we can only admit a very small number of them. Applicant Dudette wrote, I couldnt find the answer this anywhere (but could someone direct me to the answer if has been answered? :) ): I know Dartmouth and Yale and some other very competitive colleges send likely letters before the official decision deadline. Does MIT do this? MIT does not do this. Check out my earlier post on the topic. geniezclone wrote, Matt, I have a few quick questions. I know youve mentioned that most accepted international applicants had distinctions either at the international, national, or regional level. Could you tell us just about how many percent did not have any distinctions, but were admitted because of other factors (dazzling standardized test scores, pure passion which shows through essays/ECs, etc.)? Or were they simply considered not stellar enough to be admitted? Also, do you try to keep the male-female ratio of the international acceptees 50:50? I dont know the answer here, but I assure you, students stand out in many ways besides awards. We do not try for a 50:50 gender ratio. Last year I believe it was closer to 70:30 among the international admits. kumar asked, Do you ever read applications on a country basis ie do you read all indian applications together.. if so can u tell me when?? We will consider all applications from the same country together during the selection committee. Ian T. asked, Uh-oh, will being younger hurt me? What if you were born in 1988 and therefore applied when you were still 16, but will be 17 by the beginning of the 2005 fall semester? No problem. This was exactly my situation when I was applying to MIT, as well as a number of my MIT friends. expatmom asked, Are each of the subcommittees composed of people who are familiar with non-US educational systems? Yes. Each subcommittee is headed by an experienced admissions officer who has at least several years experience in international admissions as well. Sreraman muralidharan had two questions: 1) I have submitted updates on my application through e-mail before a week,But I have not yet recieved a confirmation of itCan I assume that it has reached my folder.. 2) With my application, I have also sent additional letters of recomm. (one from prof.Alladi Ramakrishnan(founder-director of Matscience) and other from Mr.Balasubramnian Ramkumar(Founder-head of theo. physc.gp.)) will they be read by the admissions office.. 1) Yes, you can assume these emails have been filed. 2) Yes, we will read all recommendations in your folder. ^ wrote, The reading period for intls is on, so thjat means youre summarising the applicants files into that E3 card right?? Yes, just as for domestic applicants, we will use summary cards for international applications. NoCreativity wrote, hey matt, i was wondering.. could u tell us which essays you liked best or thought were most compelling and well written.. after admission letters have been sent out? Some admissions officers, mentally or otherwise, compile lists of essays theyve really liked, but I dont; I dont tend to think about applications like that. For me, though, the best essays are those that really give me a sense of who you are. kendall asked, in terms of mailing letters, is there any way we can have them mailed to a different address? Yes. Please email [emailprotected] immediately if this is your case. nghi asked, there is such thing as the $1000 bill? Yes. The Treasury Department wrote, There are also several denominations of currency notes that are no longer produced. These include the $500 bill with the portrait of William McKinley, the $1,000 bill with a portrait of Grover Cleveland, the $5,000 bill with a portrait of James Madison, the $10,000 bill with a portrait of Salmon P. Chase, and the $100,000 currency note bearing a portrait of Woodrow Wilson.

Simulated moving bed technology from concept to operation - Free Essay Example

Sample details Pages: 27 Words: 8169 Downloads: 9 Date added: 2017/06/26 Category Statistics Essay Did you like this example? 1. Introduction 1.1. Continuous counter current chromatography Continuous industrial-scale adsorption processes are well known for their efficiency. Don’t waste time! Our writers will create an original "Simulated moving bed technology: from concept to operation" essay for you Create order Very often, the Height Equivalent of a Theoretical Plate (HETP) in a batch operation is roughly three times higher than one find for the continuous mode (Gembicki et al., 2002). The operation of continuous chromatographic counter current apparatus (here-by referred as True Moving Bed, TMB) in particular, maximizes the mass transfer driving force providing a better utilization of the adsorbent, and thus, allowing the use of lower selectivity materials (Ruthven and Ching, 1989) as to operate with an increased productivity (i.e., higher processed throughput using less packing material). A scheme of a TMB unit is shown in Figure 1. Figure 1 A four section True Moving Bed (TMB) unit for the separation of A and B with D as eluent or desorbent (Fructose/Glucose separation). If we define section as the part of the TMB unit where the fluid flow rate is approximately constant (section limited by inlet/outlet streams), then, it is possible to find four different sections with different roles: Section I: Regeneration of the adsorbent (desorption of A from the solid); Section II: Desorption of B (so that, the extract is not contaminated by the less retained component); Section III: Adsorption of A (raffinate clean from the more adsorbed species); Section IV: Regeneration of the eluent/desorbent (adsorption of B from the fluid phase). From Figure 1, one can observed that the counter-current movement of the solid, with respect to the fluid phase, allows continuous regeneration of both the adsorbent in section I as the eluent/desorbent in section IV. Also, the moving bed arrangement allows the achievement of high purity even if the resolution of the two peaks is not excellent, since only the purity at the two tails of the concentration profiles, where the withdrawal ports are located, is of interest. This is contrary to batch chromatography where high resolution is vital in order to achieve high purity. Nevertheless, with this counter current mode of operation is necessary to circulate not only the fluid phase but also the solid. The solid motion inside of the column and the consequent recycle presents some technical problems, namely: equipment abrasion, mechanical erosion of adsorbent and difficulties in maintaining plug flow for the solid (especially in beds with large diameter). From a technical point of view, this clearly limits the implementation of such technology. 1.2. The Simulated Moving Bed (SMB) concept In order to avoid this issue, a sequence of fixed bed columns was conceived (Broughton and Gerhold, 1961) in which the solid phase is at rest in relation to a fixed referential, but where a relative movement between both phases is experienced by switching the inlet and outlet fluid streams to and from the columns from time to time (in the direction of the fluid flow). In the simplest operating mode, the period that a certain operating configuration prevails is called the switching time, . Since the solid flow is avoided, although a kind of counter-current movement is created relatively to the fluid, this technology is called Simulated Moving Bed (SMB). Consider that at certain moment in the operation of an SMB, the positions for the inlet of feed and desorbent and outlet of products is represented by Figure 2a. Assume also the simplest operating mode (synchronous advance of all streams) and one column per section. After a period of time equal to the switching time, the injection and withdrawn points all move one column in the direction of the fluid flow (Figure 2b). When the initial location of injection/collection of all the streams is reencountered, we have completed one cycle (in a four equally zoned SMB, it takes to complete one cycle, where is the number of columns in each one of the four sections). As it is possible to see in Figure 2, during one cycle the same column is in different sections, assuming therefore different roles in the separation process. Figure 2 Schematic representation of a 4 columns SMB unit operating over a complete cycle, from 0to (with representing the ports switching time); (a) period of the first switch; (b) period of the second switch and (c) a TMB unit. As mentioned before, the continuous movement of inlet and outlet lines into and from the column is almost impractical, therefore discreet jumps (with the length of one bed, during ) have to be applied. The analogy between SMB and the TMB is then possible by the introduction of the relative velocity concept, where , with the fluid interstitial velocity in each section in the TMB, the interstitial velocity in the SMB unit and the solid interstitial velocity in the TMB. The solid velocity is evaluated from the switching time interval value in the SMB as , being the column length. As consequence, The internal flow rates in both apparatus are not the same, but related by where and represent the internal liquid flow-rates in the SMB and TMB, respectively, is the bulk porosity and the column volume. 1.3. SMB Applications Industrially, SMB applications can be regarded as Old and New, associated with petrochemical and pharmaceutical/fine chemistry fields, respectively (S Gomes et al., 2006d). Among the first applications of SMB technology (back to 1960s) are the ones implemented by the UOP Inc. (Des Plaines, IL-USA) with the Sorbex processes, such as: the Parex unit for separation of p-xylene from mixtures with its C8-isomers (Broughton et al., 1970), separation also performed by the Aromax process from Toray Industries (Tokyo, Japan) (Otani et al., 1973) and the Eluxyl process by Axens/IFP (Institut Franais du Ptrole, France) (Ash et al., 1994); the Ebex for the separation of EthylBenzene (EB) from a mixed of C8-aromatic isomers (Broughton, 1981); the Molex for the separation of n-paraffins from branched and cyclic hydrocarbons; and the Olex process to separate olefins from parafins; the Cresex and Cymex for the separation of p-cresol and p-cymene from its isomers, respectively. The application of SMBs in the sugar industry is also substantial, with the Sarex process, for the separation of fructose from the corn syrup with dextrose and polysaccharides on polystyrene-divinylbenzene resins in calcium form (Broughton, 1983); or as patented by Japan Organo Co. (Japan), (Heikkil et al., 1989); by Amalgamated Sugar Company LLC, also known as the Snake River Sugar Company (Boise, ID-USA), (Kearney and Mumm, 1990, , 1991). In the last decade, particularly in the area of drug development, the advent of SMB has provided a high throughput, high yield, solvent efficient, safe and cost effective process option. Although it had long been established as a viable, practical, and cost-effective liquid-phase adsorptive separation technique, the pharmaceutical and biomolecule separations community did not show considerable interest in SMB technology until the mid-1990s. The application of the SMB concept to the fine chemical separations in the earlier 90s, led to the second boom on the number of applications of SMB technology (Negawa and Shoji, 1992; Nicoud et al., 1993; Kusters et al., 1995; Rodrigues et al., 1995; Cavoy et al., 1997; Francotte and Richert, 1997; Guest, 1997; Pais et al., 1997a; Pais et al., 1997b; Francotte et al., 1998; Grill and Miller, 1998; Lehoucq et al., 1998; Pais et al., 1998; Dapremont et al., 1999; Miller et al., 1999; Nagamatsu et al., 1999; Nicoud, 1999a, 1999b; Pedeferri et al., 19 99; Strube et al., 1999; Juza et al., 2000; Kniep et al., 2000; Wang et al., 2001), among other pioneers. Daicel Chemical Industries, Ltd (Japan) first published the resolution of optical isomers through SMB (Negawa and Shoji, 1992). Since then, several are the SMB based processes already approved by the Food and Drug Administration (FDA) and others regulatory agencies. Examples includes renowned products such as: Biltricide (Praziquantel) Cipralex/Lexapro (Escitalopram), Keppra (Levetiracetam), Modafinil/Provigil, Taxol (Paclitaxel), Xyzal (Levocetirizine), Zoloft (Sertraline), Zyrtec (Cetirizine), Celexa/Citrol/Cipram (Citalopram), Prozac (Fluoxetine hydrochloride), (Abel and Juza, 2007) o paper de real SMB e rajendran, among others biological separation, with a particular emphasis in protein separations meteer referencias a biologias e proteinas. Given the importance of such technique, this work reviews different operating SMB modes; design, modeling and optimization techniques; and addresses an example of the design, construction and operation of an SMB unit. 2. SMB modes of operation So far, only the so-called conventional SMB mode of operation has been considered, which indeed means that each section has a fixed number of columns and there is no variation on the pre-established inlet/outlet flow rates or the switching time value. However, over the last decades some non-conventional SMB operating modes were proposed, developing the range of the applications of SMB technology and extending further its potential. Some of these operating modes, worthy of note, are listened in the following Sections. 2.1. Asynchronous shifting SMB (the Varicol process) The asynchronous shifting SMB or Varicol process (Adam et al., 2000; Bailly et al., 2000; Ludemann-Hombourger et al., 2000; Ludemann-Hombourger et al., 2002) commercialized by Novasep (Pompey, France), became one of the more studied and used processes of the so-called non-conventional SMB modes of operation. Instead of a fixed unit configuration with constant section length, the Varicol operating mode is performed by the implementation of an asynchronous inlet/outlet ports shift, providing a flexible use of each section length, Figure 3. Figure 3 [11.51.51] Asynchronous SMB for a complete cycle; section II has 1 column during the first half of the switching time and 2 columns in the remaining time (within a switching time period), thus 1.5 columns; the opposite happens to section III. By means of Varicol mode of operation it is possible to increase the productivity value up to 30% more than the classical SMB apparatus, principally when operating under a reduced number of columns (Toumi et al., 2002; Zhang et al., 2002b; Pais and Rodrigues, 2003; Subramani et al., 2003b, 2003a; Toumi et al., 2003; Yu et al., 2003b; S Gomes et al., 2006d; Mota et al., 2007b; Rodrigues et al., 2007a; S Gomes et al., 2007b; Zhang et al., 2007). 2.2. Partial-Feed, Partial-Discard With the Partial-Feed mode of operation two additional degrees of freedom are introduced: the feed length and the feed time (Zang and Wankat, 2002a; Zang and Wankat, 2002b). Feed during a given feed length period will consequently influence the raffinate and extract flow rates are along the time. Also referred in the literature is the Partial-Discard (or partial withdraw) operating mode, where just a part of the outlet products is used in order to improve the overall purity (Zang and Wankat, 2002b; Bae and Lee, 2006), or with the partial recirculation of the outlet products back to the feed (Kessler and Seidel-Morgenstern, 2008a; Kessler and Seidel-Morgenstern, 2008b; Seidel-Morgenstern et al., 2008). The ISMB (Improved SMB) mode of operating, commercialized by the Nippon Rensui Co. (Tokyo, Japan) and FAST Finnsugar Applexion Separation Technology, now Novasep-France, is also well known (Tanimura et al., 1989). In this process, during a first step the unit is operated as a conventional SMB but without any flow in section IV; in the second step the inlet and outlet ports are closed and the internal flow through the four sections allowing the concentration profiles to move to adjust their relative position with respect to the outlet ports (Rajendran et al., 2009). Meter referencias do mazzotti e nova de sa gomes Another novel non-conventional mode of operation, the Outlet Swing Stream-SMB (OSS) (S Gomes and Rodrigues, 2007), was developed under the framework of this thesis and is latter detailed in Chapter 3. 2.3. PowerFeed and ModiCon The modulation of the section flow rates (PowerFeed) was originally proposed by Kearney and Hieb (1992) and later studied in detail by other authors (Kloppenburg and Gilles, 1999b; Zhang et al., 2003b; Zhang et al., 2004b; Kawajiri and Biegler, 2006b). Another SMB operating concept, based on the feed concentration variation within one switching interval, was suggested by Schramm et al., (2002; 2003b) known as the ModiCon. The use of auxiliary feed tanks, where section flow rate flows into a tank to dissolve solid raw materials and fed into section III, has also been studied (Wei and Zhao, 2008). The cross combination of PowerFeed, Modicon and Varicol modes of operation is also a recurrent research matter, principally of optimization studies (Zhang et al., 2004a; Arau?jo et al., 2006a; Rodrigues et al., 2007b), providing more degrees of freedom and allowing better performance values. 2.4. Two Feed or MultiFeed SMB and Side Stream SMB Recently, the introduction of multi feed streams in the SMB area, by analogy with distillation columns, led to the formulation of the Two Feed SMB, or MultiFeed, operating mode presented by Kim (2005) and later studied by S Gomes and Rodrigues (S Gomes et al., 2007b; S Gomes and Rodrigues, 2007). Also multi extract/raffinate are referred in the literature (Mun, 2006), known as side stream SMB (Beste and Arlt, 2002). These techniques, combined with the distillation know-how for the optimum location of multiple feeds, can allow the development of more efficient SMB processes. 2.5. Semi Continuous, Two and Three zones SMB There are several semi continuous SMB apparatus that operate with two-zone, two or one-column chromatograph, with/or recycle, analogous to a four-zone SMB(Abunasser et al., 2003; Abunasser and Wankat, 2004; Arau?jo et al., 2005a; Arau?jo et al., 2005b; Jin and Wankat, 2005b; Mota and Arau?jo, 2005; Arau?jo et al., 2006b; Arau?jo et al., 2007; Rodrigues et al., 2008b), that allow a reasonable separation, some allowing centre cut for ternary or quaternary separations (Hur and Wankat, 2005b, 2005a, , 2006a, 2006b; Hur et al., 2007), under reduced equipment usage. The discontinuous injection in a system with 2 or more columns, based on the concept of simulated adsorbent movement, as been applied by Novasep under the denomination of Cyclojet, Hipersep, Supersep (Supersep MAX with Super Critical CO2) and Hipersep, (Grill, 1998; Valery and Ludemann-Hombourger, 2007). 2.6. Gradient SMB As a further possibility for increasing the productivity, the introduction of gradients in the different separation sections of the SMB process is also described in literature. The gradient mode was suggested firstly for the SMB-SFC (SMB-supercritical fluid chromatography) process, where the elution strength can be influenced by a pressure gradient (Clavier and Nicoud, 1995; Clavier et al., 1996). Nowadays, there are more gradient-variants that allows the variation solvent elution strength by changing the temperature, the pH-value, the content of salt or the modifier concentration (Jensen et al., 2000; Antos and Seidel-Morgenstern, 2001; Migliorini et al., 2001; Abel et al., 2002; Antos and Seidel-Morgenstern, 2002; Abel et al., 2004; Ziomek and Antos, 2005; Mun and Wang, 2008a), or as in Rodriguess group with the purification of proteins by Ion Exchange-SMB (IE-SMB) (Li et al., 2007; Li et al., 2008). Also worth of note is the MCSGP (Multicolumn Counter-current Solvent Gradient Puri fication) process (Aumann and Morbidelli, 2006; Strohlein et al., 2006; Aumann and Morbidelli, 2007; Aumann et al., 2007; Aumann and Morbidelli, 2008; Mller-Spth et al., 2008), commercialized by ChromaCon AG (Zrich, Switzerland), which combines two chromatographic separation techniques, the solvent gradient batch and continuous counter-current SMB for the separation of multicomponent mixtures of biomolecules. 2.7. Hybrid-SMB: SMB combined with other processes It is possible to improve the performance of SMB units by integrating it with other different separation techniques. The more simple application of this approach is to combine in series the two different processes and then recycle back the outlets between (or within) the different units (Lorenz et al., 2001; Amanullah et al., 2005; Kaspereit et al., 2005; Amanullah and Mazzotti, 2006; Gedicke et al., 2007). Among these, an interesting hybrid SMB was presented by M. Bailly et al., (2005; Abdelmoumen et al., 2006), the M3C process; or the similar process: Enriched Extract operation (EE-SMB) (Paredes et al., 2006), in which a portion of the extract product is concentrated and then re-injected into the SMB at the same, or near to, the collection point. The use of SMB-PSA apparatus is also referred in the literature for gas phase separations, (Rao et al., 2005; Sivakumar, 2007; Kostroski and Wankat, 2008). The use of two SMB units with concentration steps between, for the separation of bi nary mixtures, was also developed under the denomination of hybrid SMB-SMB process (Jin and Wankat, 2007a). 2.8. The SMBR multifunctional reactor The integration of reaction and separation steps in one single unit has the obvious economical advantage of reducing the cost of unit operations for downstream purification steps. Besides reactive distillation, reactive extraction or membrane reactors, the combination of (bio)chemical reaction with SMB chromatographic separator has been subject of considerable attention in the last 15 years. This integrated reaction-separation technology adopts the name Simulated Moving Bed Reactor (SMBR). Several applications have been published considering the SMBR: the enzymatic reaction for higher-fructose syrup production (Hashimoto et al., 1983; Azevedo and Rodrigues, 2001; Borges da Silva et al., 2006; S Gomes et al., 2007a); meter a dos FOS the esterification from acetic acid and -phenethyl alcohol and subsequent separation of the product -phenetyl acetate (Kawase et al., 1996), or methyl acetate ester (Lode et al., 2001; Yu et al., 2003a); the synthesis and separation of the methanol from sy ngas (Kruglov, 1994); the esterification of acetic acid with ethanol (Mazzotti et al., 1996b); the lactosucrose production (Kawase et al., 2001); the MTBE synthesis (Zhang et al., 2001); the diethylacetal (or dimethylacetal) synthesis (Silva, 2003; Rodrigues and Silva, 2005; Silva and Rodrigues, 2005a; Pereira et al., 2008); the ethyl lactate synthesis from lactic acid and ethanol (Pereira et al., 2009a; Pereira et al., 2009b); the biodiesel synthesis (Geier and Soper, 2007) falta uma; or the isomerization and separation of p-xylene (Minceva et al., 2008) faltam os franceses, are examples that prove the promising potential of this technique. Depending on the reactive system some interesting arrangements of the general SMBR setup can be found in the literature, a more detailed review of several SMBR applications can be found elsewhere (Minceva et al., 2008). 2.9. Multicomponent separations The application of SMB technology to multicomponent separations has also been an important research topic in the last years. The common wisdom for such multicomponent process is the simple application of SMB cascades (Nicolaos et al., 2001a, 2001b; Wankatt, 2001; Kim et al., 2003; Kim and Wankat, 2004); nevertheless, there are some non-conventional operation modes that proved to have interesting performance, as the one introduced by the Japan Organo Co. (www.organo.co.jp), called JO process (or Pseudo-SMB); this process was discussed in detail (Mata and Rodrigues, 2001; Borges da Silva and Rodrigues, 2006, , 2008) and (Kurup et al., 2006a). The process is characterized by a 2-steps operation: (a) in the first step the feed is introduced while the intermediary product is recovered with the whole unit working as a fixed bed; (b) during the second step the feed stopped, the unit works as a standard SMB and the less and more retained products are collected, see Annex I for details. The u se of two different adsorbents (Hashimoto et al., 1993), two different solvents (Ballanec and Hotier, 1992), or a variation of the working flow rates during the switching period (Kearney and Hieb, 1992), were also proposed. 2.10. SMB Gas and Super Critical phases Most of the industrial applications of SMB technology operate in the liquid phase; nevertheless, SMBs can also be operated under supercritical conditions; where a supercritical fluid, typically CO2, is used as eluent offering a number of advantages namely reduction of eluent consumption, favourable physicochemical properties and lower pressure drop and higher column efficiency (Clavier and Nicoud, 1995; Clavier et al., 1996; Denet and Nicoud, 1999; Depta et al., 1999; Denet et al., 2001; Johannsen et al., 2002; Peper et al., 2002; Peper et al., 2007). Also in the gas phase the recent developments have been remarkable (Storti et al., 1992; Mazzotti et al., 1996a; Juza et al., 1998; Biressi et al., 2000; Cheng and Wilson, 2001; Biressi et al., 2002; Rao et al., 2005; Lamia et al., 2007; Mota et al., 2007b; Sivakumar, 2007; Kostroski and Wankat, 2008). Meter a do propano propylene 3. SMB design, modeling, simulation and optimization Over the last 50 years, design, modeling, and optimization of chromatographic separation processes have been frequent research subjects. As consequence, several modeling methods, strategies and approaches have been developed, the more relevant are reviewed in this section. 3.1. Design strategies The design of an SMB based separation involves taking decisions at many levels, from the configuration of the unit (number of columns per section, column and particle size) to operating conditions (feed concentration, switching time, internal flow rates). Although simulation can be exhaustively done until the right combination of parameters is found for the expected performance, it is useful to have a design method that will provide a preliminary estimation of the optimum operating point, followed by simulation and/or optimization, (S Gomes et al., 2009a). The equivalence between TMB and SMB can be quite useful in the SMB design procedure. Recalling the role of each SMB section (Figure 2c), one can state a set of constraints that will limit the feasible region and allow a complete separation (recover of the more retained species (A) in the extract stream, the less retained one (B) in the raffinate port, and regeneration of the solid in section I as fluid in section IV). Where represents the solid flow rate, the average solid concentration of species in section and the bulk fluid concentration of species in section . The flow rates constraints in Eq. 1b and 1.c will identify the separation region (section II and III), while Eq. (1 a) and Eq. (1 d) the regeneration one (section I and IV). Usually, the fluid and solid velocities in each section are combined into one only operating parameter, such as the from Morbidellis group or the , as used by Ruthven (1989). The identification of constrains, Eq. (1 a) to Eq. (1 d), led to the appearance of several design methodologies, which are usually approximated and/or graphical, providing a better insight to the possible operating regions. From the plates theory and McCabe-Thiele diagrams (Ruthven and Ching, 1989); passing by the analytical solutions for a linear adsorption isotherms system in presence of mass transfer resistances (Silva et al., 2004); to the determination of waves velocities as in the Standing Wave Design (SWD) methodology (Ma and Wang, 1997; Mallmann et al., 1998; Xie et al., 2000; Xie et al., 2002; Lee et al., 2005). A particular emphasis should be given to the strategy developed for binary and multicomponent separations modeled by linear and non-linear isotherms as in (Storti et al., 1989b; Storti et al., 1 993; Mazzotti et al., 1994; Storti et al., 1995; Mazzotti et al., 1996c; Mazzotti et al., 1997b; Chiang, 1998; Migliorini et al., 2000; Mazzotti, 2006b), the so-called Triangle Theory, where the term is treated by assuming that the adsorption equilibrium is established everywhere at every time (Equilibrium Theory, (Helfferich, 1967; Klein et al., 1967; Tondeur and Klein, 1967; Helfferich and Klein, 1970), resulting in a feasible separation region formed by the above constraints Eq. (1 b) and Eq. (1 c), which in the case of linear isotherms takes the shape of a right triangle in the plane, Figure 4, (or a triangle shaped form with rounded lines in non-linear isotherms case), and a rectangular shape in the plane. Recently, this methodology was also extended for the design of SMB units under reduced purity requirements, in which the separation triangle boundaries are stretched to account for different extract and/or raffinate purities (Kaspereit et al., 2007; Rajendran, 2008). Figure 4 Triangle Theory, separation and regeneration regions for linear isotherms, where represents the Henry constant for linear adsorptions isotherms (A: the more retained and B: the less retained species), is the intraparticle porosity; case of (S,R)Tetralol enantiomers, see Section 4.3.2. Nevertheless, the inclusion of mass transfer resistances can deeply affect the result of the design. By taking into account all mass transfer resistances, and running successive simulations, it is possible obtain more detailed separation/regeneration regions, as well as the separation study carried out for three different sections (II, III and I) or (II, III and IV) allowing the analysis of solvent consumption or solid recycling, as proposed in the Separation Volume methodology, (Azevedo and Rodrigues, 1999; Rodrigues and Pais, 2004a), or the influence of the solid flow rate in the separation region (Zabka et al., 2008a). 3.2. Modeling and simulation Generally, one can model a chromatographic separation process, and consequently an SMB unit, by means of two major approaches: by a cascade of mixing cells; or a continuous flow model (plug flow or axial dispersed plug flow, making use of partial differential equations derived from mass, energy and momentum balances to a differential volume element ), (Rodrigues and Beira, 1979; Ruthven and Ching, 1989; Tondeur, 1995; Pais et al., 1998). Each of these approaches can include mass transfer resistances, thermal, and/or pressure drop effects. Nevertheless, most of the recent literature concerning SMB processes just makes use of the continuous approach, detailing the particle diffusion and/or film mass transfer (the Detailed Particle Model), or using approximations to the intraparticle mass transfer rate in a similar way as the Linear Driving Force (LDF) approach presented by Glueckauf (1955a), (Guiochon, 2002). One can argue that an SMB unit is no more than the practical implementation of the continuous counter current TMB process, Figure 2. Consequently, the equivalence between the TMB and a hypothetical SMB with an infinite number of columns can be used in the modeling and design of SMB units. However TMB model approach will just give reasonable results if a considerable number of columns per section is present. The SMB model approach represents an SMB unit as a sequence of columns described by the usual system equations for an adsorptive fixed bed (each column ), thus represented by a PDE system. Nevertheless, the nodes equations can be stated to each section, making use of the equivalence between the interstitial velocity in the TMB and SMB, and thus: The issue here is that, due to the switch of inlet and outlet lines, the boundary conditions to a certain column are not constant during a whole cycle but change after a period equal to the switching time. Since the model equations are set to each column , one will obtain the concentration of species in the begin of each section , , from the following node mass balances: Considering now . This set of equations continues to progress in a similar way (shifting one column per ), until , repeating then from the first switch. As for the TMB model approach, both the Detailed Particle Model and LDF approach can be used with the SMB model approach; nevertheless, and for the sake of simplicity, just the last is detailed in this work. The LDF approximation can now be obtained from , and thus obtaining for the bulk fluid mass balance: and for the mass balance in the particle, with the respective initial: and boundary conditions: where the adsorption equilibrium isotherm is: As a consequence one obtains discontinuous solutions, reaching not a continuous Steady State but a Cyclic Steady State (CSS). By applying the SMB model approach, both the Detailed Particle as LDF strategies, to the case study mentioned before, one obtains the CSS concentration profiles over a complete switching time, Figure 6. 3.3. Performance parameters The performance of the SMB unit for a given separation is usually characterized by the following parameters: purity, recovery, productivity per the amount adsorbent volume and eluent/desorbent consumption per mass of treated product. The definitions of all these performance parameters, for the case of a binary mixture, are given bellow: Purity (%) of the more retained (A) species in extract and the less retained one (B) in the raffinate stream, over a complete cycle (from to ): Recovery (%) of more retained (A) species in extract and the less retained one (B) in raffinate stream, again over a complete cycle: the productivity per total volume of adsorbent : the eluent/desorbent consumption : These parameters hold for both SMB and TMB model approaches; nevertheless, one can simplify: in the SMB model strategy the same equations can be stated for a switching time period (from to ) if the unit is symmetrical, i.e., there are no differences between each switching time period (either due to the implementation of non-conventional modes of operation, or to the use of more detailed models accounting for dead volumes or switching time asymmetries); in the TMB model approach there is no need of the integral calculation, since the solutions from this model strategy are continuous and thus, the performance parameters constant over the time (at the steady state). 3.4. Optimization Usually one can classify the optimization of SMB units according to the type of objective functions: (i) optimization of performance parameters (productivity, adsorbent requirements or desorbent/eluent consumption for given purities and/or recovery requirements); (ii) optimization based on the separation cost. In case (i) each objective function, based on a different set of performance parameters, can lead to a different optimum solution; therefore multi-objective functions procedure should be considered; in the second case (ii) all those different performance parameters can be homogenized/normalized by the separation cost, where separation dependent costs (adsorbent, plant, desorbent/eluent recovery cost, desorbent/eluent recycling, feed losses) and separation independent costs (wages, labour, maintenance, among others) are taken into account and weighted by cost factors, which sometimes are difficult to characterize (Jupke et al., 2002; Chan et al., 2008). To solve these problems, the use of powerful optimization algorithms, such as: IPOPT (Interior Point OPTimizer, (Wa?chter and Biegler, 2006), employed for liquid as gas phase SMB separations (Kawajiri and Biegler, 2006b, 2006a; Mota et al., 2007a; Mota and Esteves, 2007; Rodrigues et al., 2007b; Kawajiri and Biegler, 2008a, 2008b); the commercial package gOPT from gPROMS with a Single (or Multiple) Shooting-Control Vector Parameterization, used in the two level optimization of an existing Parex unit (Minceva and Rodrigues, 2005), for ageing analysis (S Gomes et al., 2008b) and gas phase separation of propane/propylene (S Gomes et al., 2009a) or for optimal economic design (Chan et al., 2008); the Non-dominated Sorting Genetic Algorithm (NSGA) or the Jumping Gene based algorithms (Deb, 2001), such as NSGA-II-JG, applied by several groups to optimize SMB units, from p-xylene to chiral separations (Zhang et al., ; Zhang et al., 2002a; Subramani et al., 2003b; Zhang et al., 2003a; Wongso et al., 2004; Kurup et al., 2005; Wongso et al., 2005; Kurup et al., 2006c; Paredes and Mazzotti, 2007; Lee et al., 2008; Mun and Wang, 2008b), is recurrent, either in the refinement of the design strategies mentioned before, or as a diagnosis method (such as the use of superstructures SMB considering several hypothetic inlet/outlet recycles), allowing the identification of new SMB configurations or modes of operation. 4. Design, construction and operation of SMB units The design, construction and operation of a new lab-scale flexible SMB unit, the FlexSMBLSRE detailed elsewhere (aper aiche sa gome), is addressed in this section. 4.1. Design and construction 4.1.1. Valves and pumps design As mentioned before, there are several ways to operate an SMB unit; therefore, when designing a new SMB unit, particularly for research purposes, one should take into account its flexibility as a key objective (Chin and Wang, 2004). If one considers an SMB unit as a certain number of packed columns interconnected and feedcontrolled by a specific valves and pumps arrangement, it will be easy to understand that the key factor related with an SMB unit expandability and flexibility is in fact its valves system. An extensive review on the different SMB units valves schemes patented over the years can be found elsewhere (Chin and Wang, 2004). The FlexSMB-LSRE is based on a two SD (SelectDeadend flow path) valves per stream in the extract and raffinate currents, one SD per stream in the feed and eluent/desorbent currents and one twoway valve per column as detailed in Figure 6.2. Figure 6.2 FlexSMB-LSRE pumps and valves scheme under a 6 columns configuration, operating a during the first step of a [1221] classic SMB. Bold lines are the active connections; thick lines are stagnant volumes. (alterar a figura) By using this valves and pumps scheme, it is possible to operate most of the non-conventional SMB operating modes and perform columns re-configuration simply by changing some parameters in the automation routines on the computer interface. 4.1.2. Construction When assembling an SMB unit one should take into account that tubing and other equipment will introduce dead volumes; pumps and valves distribution may introduce dead volumes asymmetries, and thus the unit might present in the end some peculiarities which can limit its performance. Therefore, when constructing the FlexSMB-LSRE a preliminary work was undertaken to study possible equipment and columns positing. As result, the tubing and equipment dead volumes were reduced by using of 1mm i.d. tubes and short dead end valves (SD, Valco Instruments Co., Inc.) were employed. To reduce the dead volumes asymmetries, tubes with the same length were used for the same function and all columns assembled in a carousel scheme, Figure 6.4. Photo do SMB To reduce the pumps flow rates fluctuations (fluid inlets, outlets and internal flow rates), four HPLC pumps (VWR International, USA) were used, assisted by two Coriolis flow meters (Bronkhorst High-Tech B.V., Netherlands). One purge valve was installed at the outlet of raffinate stream that together with a purge valve installed next to the extract pump serves to manually regulate the total system pressure, as well as security valves. To avoid variations related to the ports switching velocity asymmetries a distributed connection scheme for the SD valves was used. The FlexSMB-LSRE can operate with a maximum number of columns of 12. For a 6 columns apparatus, all columns were connected to the 12 ways SD valves using just the odd valve connecting positions (i.e., 1,3,,9, 11) in order to reduce the switching time discrepancies. All equipment is connected to an integrated power supply that assures protection from electrical fluctuations as a possible current discharge. 4.1.3. Automation The automation of any laboratorial/industrial unit is a critical task, and as it concerns to an SMB unit, it is probably even more crucial. In fact, a relevant part of these units flexibility relies in its automation and control routines. The LabView (National Instruments, USA) platform, was chosen to automate the FlexSMB-LSRE unit and thus to connect the computer to all controllable equipment: (valves, pumps and flow meters). A LabView based application was then used to provide a user friendly interface between the operator and the equipment, Figure XX. 4.1.4. Columns packing and characterization The common modeling strategies assume that all SMB columns have identical characteristics. However, it is quite difficult to find several columns manufactured with the same specifications (column tubes may have slightly different geometric dimensions, thus, different retention times for a given flow rate), as well as one should take into account that packing procedure is quite irreproducible, and therefore, it results on local fluctuations of the packing density) (Mihlbachler et al., 2001; Mihlbachler et al., 2002). Consequently, once the operator introduces the theoretical optimized operating parameters, the differences between columns arise and different values from the ones expected can appear. Therefore, packing of SMB columns should be carefully done and columns should be repacked if do not present acceptable reproducibly good characterization results. For the FlexSMB-LSRE columns used for the case studies presented in the next Sections, the slurry packing method as chosen and each column packed by means of Analytical Slurry Packer from Alltech Associates Inc. (USA). For each column a slurry of approx. 18.5g of Chiral AD 20m, amylose tris-(3,5 dimethylphenylcarbamate coated onto 20m silica-gel), provided by Chiral Technologies Europe (France) in approx. 36ml of 2-propanol (GC-grade from Sigma-Aldrich Chemie, Germany) was prepared (pure 2-propanol was chosen as slurry solvent taking into account its physical proprieties, namely its viscosity). For the case studies shown on this work, The column was filled with solvent (2-propanol) and the slurry poured its upper reservoir. Then, the analytical slurry packer pump was connected to the upper reservoir and operated for 10min, at a max solvent pressure of 20bar (approx. 300ml.min-1), the solvent used was a mixture of -hexane/2-propanol, 90/10%, volumetric fraction, (GC-grade from Sigma-A ldrich Chemie, Germany). The reservoir was opened and the excess solvent drained again; the column disconnected from the reservoir and the excess of solid in the top of the column cut with a blade. Each column was evaluated for HETP numbers, tracer experiments were performed by injecting pulses of 100ml of a solution of 0.00667+/-0.00001g of TSO (Trans Stilbene Oxide, racemic mixture standard for this type of operations) and 0.00700+/0.00001g of TTBB (1,3,5 TriTert ButyBenzol, considered non adsorbed) in 25.00+/-0.05ml of heptane-2-propanol (95%-5%, volume fraction) mobile phase. An average HETP value of 0.03cm was found and the retention times obtained from the experiments has a maximum deviation of 5% among all the columns. Therefore, and accounting with the packing supplier specifications, the columns were considered suitable for the SMB operation. 4.2. Operation The technology demonstration stage is a quite important step in the RD flow sheet, and in fact, when it accounts to equipment development it is probably the most important one. To operate and demonstrate some of the potential of the FlexSMB-LSRE unit, a set of different experiments was planned regarding both linear as non-linear adsorption isotherms, under different modes of operation (classic and non-conventional). However, the operation of SMB units is not as straightforward as other batch techniques, and a particular attention must also be directed for some aspects not accounted (or simplified) in the modeling stage. 4.2.1. Real SMB units modeling and design It should be taken into account that the performance of a real SMB unit differs from the ones described by the commonly used modeling and design strategies. There are several factors that can influence the precision of the SMB model predictions, such as: uncertainty in adsorption equilibrium kinetics and hydrodynamics data (diffusivity, axial dispersion coefficients etc.) and bed voidage (packing asymmetries), as well as, extra column dead volumes (tubing, equipment, asymmetries), variation in the port switching velocity (asymmetries and delays), fluctuations in pump flow rates (fluid inlets, outlets and internal), which are not accounted for it in the most commonly used SMB models (Mun et al., 2006). Consequently, if one runs an experimental SMB unit based on the operating parameters obtained by a simple mathematical model, such as the one described in Section CCC, the experimental results may not match the ones that were predicted by the model. Concerning the uncertainty in the equilibrium isotherm data, kinetics data, and even the asymmetries of columns packing, the more precise, and/or accurate, these factors are, better will be the SMB model predictions. Therefore, detailed and precise measurements of all these parameters have to be done a priori, so that they introduce a minimal discrepancy between the SMB model results and the experiments itself. The remaining deviation factors, such as the tubing and equipment dead volumes, pumps and valves asymmetries, related to each SMB unit design and equipment particularities should be taken into account before starting to construct a new SMB unit, as detailed before. However, even after all the work done on the FlexSMB-LSRE unit, the unit still has: 11.5% of dead volumes; the port switching velocity variation (delay) can represent around 0.8 seconds; the fluctuation of the pumps flow rates are still considerable. If the average internal flow rates in each section are kept constant during the SMB operation (as assumed by some SMB design procedure) the SMB performances would not be affected, despite their considerable local variations. This is due to the cyclic mode of operation of these units, leading to compensation of these variations with time. Nevertheless, there are still two major issues concerning the prediction of the SMB performances: the unit SMB design features related with the dead volumes and the switching time asymmetries or delay. To deal with discrepancies between the real SMB operation and that predicted with commonly used models that account only for the presence of SMB columns (and do not consider the surrounding equipment features) one can apply different compensation strategies. For instance, the asynchronous port shift in the Licosep units (Hotier and Nicoud, 1995; Hotier and Nicoud, 1996; Blehaut and Nicoud, 1998), and simplified by switching time compensating strategy ( Sa gOmes). The second strategy was discussed by several authors, within the Triangle Theory spectrum (Migliorini et al., 1999b; Katsuo et al., 2009), or in the case of the Standing Wave Theory (Mun et al., 2003a; Mun et al., 2006). The switching time compensating measure accounts only for equipment dead volumes, the switching time delay or asymmetry is still not compensated when this measure is used. They can be included in the switching time compensation measure as true delay in the switching time, as follows: For the FlexSMB-LSRE: Where represents the switching time for an ideal SMB unit with zero dead volumes, the total dead volumes in section , ml.min1, the units average flow rate and the sub switching time delay (see Figure 6.14). The corrected separation region using the extension to the switching time compensating measure is shown in Figure 6.17. As can be observed in Figure 6.17, the SMB-zero dead volumes separation region corrected by the dead volumes and switching time delay (asymmetries) almost matches the one obtained with the detailed model. By this means it is possible to easily obtain a precise and realistic separation region without running tedious simulations related with the more detailed SMB models. 4.2.2. Separation of racemic mixture of (S,R)Tetralol enantiomers (linear Isotherms) by conventional SMB As case study it is presented the resolution of a racemic mixture of (S,R)Tetralol 9(S,R)-()-1,2,3,4 Tetrahydro-1-naphthol) at the concentration of 1.0g.dm3 in a heptane/2propanol (95%/5% volumetric fraction) solvent basis, using the 6 stainless steel columns packed with CSP Chiralpak AD (diameter particle size of 20m). a) Determination of adsorption and kinetic parameters Since the racemic mixture to be separated would be prepared at 1.0g.dm3, near diluted conditions, the adsorption equilibrium was represented by means of a linear formula characterized by an Henry constant for each enantiomer , . Consequently, the sorption parameters were determined by means of pulse experiments in a stainless steel column (=25cm and I.D.=0.46cm) packed with Chiralpak AD (diameter particle size of 20m) also using the Analytical Slurry Packer as described before. A racemic solution of 0.5g.dm3 (S,R)Tetralol (minimum 99% purity, Fluka Chemie, Switzerland) was prepared in a heptane/2propanol (95%/5% volumetric fraction, also from Sigma Aldrich, previously degassed and filtrated trough a 0.2m and 50mm I.D. NL 16-membrane filter (Schleicher Schuell, Germany), and loaded into a 10l loop that was then injected by means of a Knauer injection valve installed on a Gilson HPLC unit. The consequent peaks were measured by means of a UV detector set at 270nm. The procedure was rep eated for four different flow rates (4.4ml.min1; 8.5ml.min1; 12.5ml.min1; and 16.6ml.min1). The peaks retention times () were then deducted from the equipment dead volumes (0.50ml for the injector and 0.01ml for the detector) and plotted in function of the measured flow rate, Figure 6.18. The slopes obtained from both regression lines (Figure 6.18) were then used to determine the Henry adsorption constants of both enantiomers from and thus obtaining (R=A and S=B): and . The same overall mass transfer coefficient as defined in Zabka and Rodrigues (2007), was used to lump both the intraparticle as film mass transfer resistances and defined by . Where was calculated from the Linear Driving Force (LDF) approximation suggested by Glueckauf (1955b) (with the effective pore diffusivity define by , the pore porosity, , the particle porosity obtained from , the molecular diffusivity calculated by the Wilke-Chang equation (1955) and extended to mixed solvents by Perkins and Geankoplis (1969) with the absolute temperature, the solution viscosity, calculated according to Teja and Rice method for liquid mixtures (1981), the solute molar volume and obtained form where are the molar fractions, the molar masses and are the association factors constants which account for solute-solvent interactions); and obtained from , with the Sherwood number, the Schmidt number defined by and the Reynolds number: . The contribution of molecular diffusion to axial dispersion is assumed to be negligible and therefore the axial dispersion coefficient ( obtained from, (Zabka and Rodrigues, 2007). b) Determination operating parameters and operation After the determination of the equilibrium adsorption parameters it was possible to draw both the theoretical separation as the regeneration regions for the separation under study and choose suitable operating conditions, Taking into account the equipment limitations as maximum pressure drop allowable (20bar), it was possible to calculate the following operating parameters: ml.min-1, =6.0ml.min-1, =1.0ml.min-1, =4.5ml.min-1, =2.5ml.min-1, =2.95min. Applying the dead volumes and switching time delay correction (from eq. 6.3) it was found that the switching time compensating measure should be about 4% (based on an average flow rate of 25.0ml.min1), and thus correcting the switching time for 3.05min. About 5dm3 of nheptane/2propanol (95%/5% volumetric fraction) solution was prepared and filtrated as mentioned before. This mixture served as Eluent as well as solvent for the preparation of 1dm3 of the racemic mixture of (S,R)Tetralol at 1.0g.l1 used as Feed. The extract and raffinate flow rates were monitored by means of the total recovered mass in each outlet over complete cycles and weighted on a laboratorial balance with 0.01g of precision. The extract flow rate was also measured by means a Coriolis flow meter installed for control purposes at the extract stream outlet. The recycle flow rate was monitored by the other Coriolis flow meter. The experimental average flow rates, as well as geometric features, number of columns and SMB configuration are reported in Table 6.9. Table 6.9 Experimental operating conditions for the (S,R)Tetralol racemic mixture separation . Columns and packing parameters = 10cm = 2.0cm = 0.4 = 0.5g.dm3 20m SMB operating conditions (measured) 3.05min 28.7ml.min1 24.3ml.min1 25.3ml.min1 22.9ml.min1 Eluent Extract Feed Raffinate 5.8ml.min1 4.4ml.min1 1.0ml.min1 2.4ml.min1 The different model equations presented in this work were numerically solved using the gPROMS v2.3.6 a commercial package from Process Systems Enterprise (www.psenterprise.com), by applying the OCFEM (Orthogonal Collocation on Finite Elements) with 2 collocation points per element, 50 elements in each column for the axial coordinate and 3 collocation points and 5 elements for the radial discretization (when necessary). After the axial and/or radial discretization step, the time integration is performed by the ordinary differential equation solver SRADAU a fully-implicit Runge-Kutta method that implements a variable time step, the resulting system is then solved by the gPROMS BDNSOL (Block decomposition NonLinear SOLver). An absolute and relative tolerance value was set to 105. The separation was undertaken throughout 28 cycles. During the operation, samples of extract and raffinate average concentrations were withdrawn (referent to a complete cycle, namely: cycle 2; 4; 6; 8; 10; 13; 15; 17; 19; 27), To plot the FlexSMB-LSRE concentration profile, from cycle 20 to cycle 25, a single sample in each cycle was withdrawn for 10 seconds, at the middle of the switching time period , by means of a 6 ports sampling valve installed on the outlet of column 6 for internal profile sample I, III, IV and V; and at the extract and raffinate ports for profiles samples VI and II, respectively, see Annex VIII. The same procedure was then repeated in cycle 27, but now with all sampling apparatus occurring within the same cycle. Both sampling procedures resulted in almost the same concentration profile, proving that collecting six samples per cycle will not influence too much the SMB internal profiles. In Figure 6.21 the internal concentration profile obtained from cycle 20 to 27.. The simulated results fit well the experimental ones, even the secondary plateau noted next to the left of major plateau of the more retained species in section II and the right of the major plateau of the less retained species in section III (related with dead volumes of both extract and raffinate lines), are well predicted by the extended dead volumes model used. All samples (extract and raffinate average concentrations, as well as internal profiles) were loaded into a 10l loop and then injected by means of a Knauer injection valve installed on a Gilson HPLC unit into an analytical column CHIRALCEL OBH (25cm and 0.46cm I.D., supplied by Chiral Technologies, France) using as mobile phase the same solution used for eluent purposes. The consequent peaks were measured by means of a UV detector set at 270nm and concentrations determined according with calibration curve obtained from linear regression of Area vs. Concentration ( of 5 standards (g.dm-3, of each enantiomer) with a with a All experiments (separation with the SMB unit and analytical procedures) were run at laboratorial conditions (approximately 25C). 4.3. Control of SMB units In recent years the control of SMB units has also been wide investigated (Erdem et al., 2004b; Engell, 2007; Grossmann et al., 2008a; Grossmann et al., 2008b). Several reports on dynamic control strategies include nonlinear control strategies such as: the input-output linearizing control, where the controller action is based on a nonlinear state estimator using the TMB model (Kloppenburg and Gilles, 1999a); and model predictive control (MPC) (Natarajan and Lee, 2000; Erdem et al., 2004a; Dietz and Corriou, 2008); or design on the basis of neural networks (Wang et al., 2003). Also a model based SMB control where an optimal trajectory is calculated off-line was proposed by (Klatt et al., 2000; Klatt et al., 2002) and from wave reconstruction (Kleinert and Lunze, 2008). A more recent strategy based on the nonlinear wave propagation phenomena aims to control the central sections of the SMB unit by controlling the position of the concentration fronts (Schramm et al., 2003a). The control o f chromatographic processes (SMB included) by means of the standard control procedures (P, PI or PID controllers), but detecting characteristic points of the unit where the history of a specific variable of the fractions of the mixture to be separated will be representative for the control action was also addressed (Valery and Morey, 2009). 5. Conclusions

Production Consumption And The City Essay - 1742 Words

PRODUCTION CONSUMPTION AND THE CITY Castells’s earlier writings were much focused towards the urban studies and his writings addressed many challenges, issues and the problems in the urban studies. His writings challenged the present existing orthodoxies in the society by developing many arguments and intense interest. And later on many emerging European theorists started to propound their own agendas for studying the urban. â€Å"In The Urban Question† castell’s approach was:- (i) Ahistorical (ii) Ethnocentric (iii) Functionalist ï  ¶ AHISTORICAL Althusserian Structural paradigm dismissed or ignored the history but also was not in the favor to the explanation of the history in which social influence can be follow only to the specific events, rather than being built in the results of the combinations of the events. According to Althusserian history is something that is problematic for the human as a subject such as change happens through the actions of the human beings and to the method of empiricism that the knowledge comes only from the experiences. Therefore history clearly against the â€Å"Scientific† method of theoretical practices. But Castells rejected Althusserian’s this view and focused on the need of the history for theoretical formalism. This he described as the â€Å"Theorized Histories†. Later castells criticized his own idea of â€Å"coding† observations into conceptual categories without the understanding of the reasons which gave rise to them. So the question arises that how anShow MoreRelatedPopulation Growth Is A Crisis Or Not?1273 Words   |  6 Pagesdemands of production and consumption are high. According to the BBC horizon documentary (2009), number of current population is about seven billion, seven times more than the last 10,000 years. 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Advantages of Science Free Essays

Assignment #3 WAQAR AHMED KHAN (5757) Q1. Write a function power ( a, b ), to calculate the value of a raised to b. static void Main(string[] args) { Console. We will write a custom essay sample on Advantages of Science or any similar topic only for you Order Now WriteLine(â€Å"enter number with power is to be calculated†); int a = Convert. ToInt16(Console. ReadLine()); Console. WriteLine(â€Å"enter power†); int b = Convert. ToInt16(Console. ReadLine()); Program p = new Program(); double c=p. power(a, b); Console. WriteLine(a+ † rase to the power â€Å"+b+ â€Å"=†+c); } private double power(int a, int b) { double power = Math. Pow(a, b); return power; } Q2. Write a general-purpose function to convert any given year into its roman equivalent. Example: Roman equivalent of 1988 is mdcccclxxxviii Roman equivalent of 1525 is mdxxv static void Main(string[] args) { Console. WriteLine(â€Å"enter the year†); int number=Convert. ToInt16(Console. ReadLine()); Program p=new Program(); string samsung=p. ToRoman(number); Console. WriteLine(samsung); } private string ToRoman(int number) { if ((number 0) || (number 3999)) throw new ArgumentOutOfRangeException(â€Å"insert value betwheen 1 and 3999†); if (number 1) return string. Empty; f (number = 1000) return â€Å"M† + ToRoman(number – 1000); if (number = 900) return â€Å"CM† + ToRoman(number – 900); if (number = 500) return â€Å"D† + ToRoman(number – 500); if (number = 400) return â€Å"CD† + ToRoman(number – 400); if (number = 100) return â€Å"C† + ToRoman(number – 100); if (number = 90) return â€Å"XCâ₠¬  + ToRoman(number – 90); if (number = 50) return â€Å"L† + ToRoman(number – 50); if (number = 40) return â€Å"XL† + ToRoman(number – 40); if (number = 10) return â€Å"X† + ToRoman(number – 10); if (number = 9) return â€Å"IX† + ToRoman(number – 9); if (number = 5) return â€Å"V† + ToRoman(number – 5); if (number = 4) return â€Å"IV† + ToRoman(number – 4); if (number = 1) return â€Å"I† + ToRoman(number – 1); throw new ArgumentOutOfRangeException(â€Å"something bad happened†); } Q3. Any year is entered through the keyboard. Write a function to determine whether the year is a leap year or not. static void Main(string[] args) { Console. WriteLine(â€Å"enter the year†); int a = Convert. ToInt16(Console. ReadLine()); Program p=new Program(); . leap(a); } private void leap(int a) { if (a%4! =0 a%100==0 a%400==0) { Console. WriteLine(â€Å"this year is a lea p year†); } else Console. WriteLine(â€Å"this is not a leap year†); } Q4. Write a function that receives 5 integers and returns the sum, average and standard deviation of these numbers. int a, b, c, d, e; Console. WriteLine(â€Å"enter first number†); a = Convert. ToInt16(Console. ReadLine()); Console. WriteLine(â€Å"enter second number†); b = Convert. ToInt16(Console. ReadLine()); Console. WriteLine(â€Å"enter third number†); c = Convert. ToInt16(Console. ReadLine()); Console. WriteLine(â€Å"enter forth number†); = Convert. ToInt16(Console. ReadLine()); Console. WriteLine(â€Å"enter fifth number†); e = Convert. ToInt16(Console. ReadLine()); Program p = new Program(); int f = p. sum(a, b, c, d, e); int g = p. average(f); double h = p. standard_deviation(a, b, c, d, e, f, g); Console. WriteLine(â€Å"sum of numbers are=†+f); Console. WriteLine(â€Å"averge of numbers are=†+g); Console. WriteLine(â€Å"stardard deriva tion of numbers is=†+h); } private double standard_deviation(int a, int b, int c, int d, int e, int f, int g) { double i, j, k, l, m,deri,squ; i = a – g; j = b – g; k = c – g; l = d – g; m = e – g; i = Math. Pow(i, 2); j = Math. Pow(j, 2); = Math. Pow(k, 2); l = Math. Pow(l, 2); m = Math. Pow(m, 2); deri = (i + j + k + l + m) / g; squ = Math. Sqrt(deri); return squ; } private int average(int f) { int avg = f / 5; return avg; } private int sum(int a, int b, int c, int d, int e) { int sum = a + b + c + d + e; return sum; } Q5. If we list all the natural numbers below 10 that are multiples of 3 or 5, we get 3, 5, 6 and 9. The sum of these multiples is 23. Find the sum of all the multiples of 3 or 5 below 1000. int sum = 0; for (int i = 3; i 1000; i++) { if (i % 3 == 0 || i % 5 == 0) { sum += i; Console. WriteLine(sum. ToString()); } Q6. A palindromic number reads the same both ways. The largest palindrome made from the product of two 2-digit numbers is 9009 = 91 99. Find the largest palindrome made from the product of two 3-digit numbers. int maxPalindrome = 0; for (int i = 100; i 1000; i++) { for (int j = i; j 1000; j++) { int product = i * j; if (product. IsPalindrome() product maxPalindrome) { maxPalindrome = product; } } } System. Console. WriteLine(maxPalindrome); } } public static class Extensions { public static bool IsPalindrome(this int i) { Listchar chars = new Listchar(i. ToString(). ToCharArray()); chars. Reverse(); return i == int. Parse(new string(chars. ToArray())); How to cite Advantages of Science, Essay examples

Business Process and Modelling

Questions: 1. What is the most common Organizational Structure? How did the structure evolve? What are the benefits and drawbacks associated with the implementation of such a structure? 2.What is a functional information system? What is their value to an organization? What are their main drawbacks?3.What is an enterprise information system? How do these systems differ from functional systems? What is their value to organization? 4.Explain the difference between the functional view and process view of Organizations. Why is the process view important today? 5.Within the procurement process what is a three way match used for? What is used to complete the match? 6.Explain the difference between a Bill of Material and Product Routing? 7.Identify some of the key problems associated with the manual, or paper-based, business process. How does an enterprise system eliminate or reduce the impact of these problems. 8.Explain the difference between a Made to Order and Made to Stock strategy. What are the perceived advantages and disadvantages of each approach? 9.What impact has globalization had on an organization? How do they respond? 10.What does it mean when it is said that a product may have several views? What is a view and what are they used? 11.In the SAP environment, explain the difference between Organizational, Master and Transactional data? Provide examples. 12.Explain the four common material types in an ERP System? Answer: 1. Organizational structure is part of the strategic management approach use by the management while embracing their management functions, it refers to how activities such as the supervision, task allocation, and coordination are redirected towards achieving the set organizational structure. It is also explained to be achieving the organizational objectives through people in their working environment(Frank, 2014). The functional structure is commonly used organizational structure, it is the type of the organizational structure in which organizational activities are grouped into groups and department such as finance, information communication department, and marketing. It is commonly used by large and small organizations(Yu, 2013). By grouping the organizational activities into group enhances utilization of the human resource strategic management approach such as motivation and job performance appraisal to employee. The grouped department in the organization will also be able to make the right decisional making which will ensure proper operation in the organization. The disadvantage is that practical offices may turn out to be excessively effective, regularly dismissing the association(Doumeingts, 2016). 2. A functional information system is an approach that provides significance information relating specific groups and activities and other vital information regarding the management controls. The functional information system in an organization plays a key role in making fundamental decisions that will lead to achieving the organizational goals and objectives. Decision-making process implies making decision which will be functional while planning the future operations of the organization. An information system is an organization facilitated the noble operations which will lead the form into gaining the competitive advantage in a business environment. It also allows the organization faces important communication process. Information systems may not work legitimately which influences the running of the business. This can bring about framework separate, intruding on smooth operations and buyer disappointment. Deficient information systems can convey wrong information to different systems which could make issues for the business and its clients. Information systems are additionally vulnerable to hackers and frauds. 3. Enterprise systems support the whole procedure as opposed to parts of the procedure. Moreover, enterprise systems are not only backing the execution of individual exercises in a procedure, they additionally help the association coordinate work across the functional units. This coordination further decreases delays, avoids excess stock, and expands visibility. Apparently the intricacy of dealing with the information across whole procedures, it is not practical to depend on physically associating useful data frameworks by printing data from one framework and rekeying it into the following framework. In this way, notwithstanding moving from storehouses to procedures, associations should likewise move from practically engaged data frameworks to coordinated venture frameworks(Bannister, 2015). 4. The functional view of an organization is focusing on the skills and the expertise relevant to fulfill certain business functions at the different organizational level. While the process view of the organization is based on the different stages of production process in the organization. Communication in functional view of the organization takes place at the departmental level, while in process view communication and related decision take place in the process stages(Doumeingts, 2016). Process view is commonly used strategic management in todays business environment, it allows managers to establish and focus on the relevant skill required in the production process of the organization(Frank, 2014). 5. The three-way match is a payment verification approach that is used by accounting and procurement department while procuring supplies to the organization, it implies when one party A receives an invoice it will be the same with one party B is having. The documents used in the three-way match are invoice, purchase order, and receive report(Tang, 2016). 6. Bill of material is embraced to be an essential part of manufacturing, it comprises list of part, sub-assemblies, and assemblies used in creating the final products. The bill of material explains what to be bought as well as instruction of how to assemble the products. While product routing in manufacturing explains the steps and procedures which will be used in creating the final products. Routing states the process and related task required while creating to new final products(Morecroft, 2015). 7.The manual business process is influenced by the different key problem, this limits the operation of the organization. The manual business system takes more efforts and physical space to track the paper documents when errors are to be corrected the data are to be completed and redone rather being updated. Customer service may is also affected by the essentiality of manual and paper business process in the organization, accessing the customer information may be difficult since the customer details are stored in different places(Davenport, 2013). To eliminate this manual works, the company should adopt the use of new technology such as accounting packages and other related softwares, this will seek toward reducing and eliminating fully the key problem associated with the manual business process(Frank, 2014). 8. Make to order (MTO) is a business production strategy that normally allows the customers to buy products that are customized to their determinations. This strategy just makes the final products once the customer places an order. This creates an extra time for the customer to get the product, yet considers more adaptable customization contrasted with obtaining from retailers. Make to order (MTO) strategy eases the issues of over the top inventory that is normal with the conventional make to stock (MTS) strategy. Therefore the advantage of Make to order is to reduce production of excess stock to the market(Fleischmann, 2014). While the Made to Stock strategy is a traditional production strategy used by many business organization to match the level of production and inventory in relation to the customer demands and forecast, Made to Stock strategy requires to the company to exceptionally make an accurate forecast of demands in the market in order to determine the level of stock to be produced. One of the drawbacks of Made to Stock strategy is that it only relies on the accuracy of the forecasted demands(Frank, 2014). 9. Globalization is defined to be the integration of people, business organization, and governments. The process of globalization is created as a result of agreement between firm and the governments, this is to improve the operation of every business organization(Yu, 2013). Adopting of new innovation and technology is one of the response and the positive impact of globalization on the organization, this implies when the organization used different technology to undertake their business activities. Expansion in the market environment is also amongst the response of the globalization in relation to the impact on the organizations. Low-Priced Workforce and Raw Materials is an impact of globalization to operating business organization, it implies when the company responds to the effects of low labor and raw material. An organization may access the important factors by entering into an agreement with other operation firms from different regions(Cross, 2016). 10. Product view is explained to be an element of marketing information system. It is defined to be process of understating the product concepts, design requirement, product target market, pricing and positioning strategy. The product view allows the customer and all the stakeholders to review the product in the market, their views may be used to improve the image, design and the specification of the product(Frank, 2014). 11. Systems Applications and Products allows the organization to track business operation in relation to customer and their interaction with the business. Organizational data refers to the data relating to the structure and mode of the organization. Examples include sales and raw material data. Transactional data are data that support the daily operation of an organization, they comprise the automotive systems that facilitate daily business process. Example include payment methods and discount received and allowed(Fleischmann, 2014). Master data plays a primary role in business process, it refers to the key organizational entities that are utilized by a few useful groups and are regularly put away in various data frameworks over a business enterprise. Moreover, master data represents the business entities around which the organization business transactions are executed and the essential components around which analysis are conducted. An example includes data relating to employee performance, product, and supplies(Bannister, 2015). 12. Raw materials. Ordinarily, raw materials are obtained from a seller and are not sold to end-clients(Yu, 2013). Semi-Finished products. They are normally created from crude materials and are utilized to deliver finished merchandise. Cases: front wheel gatherings. Finished goods. This is made by the production procedure from different materials, for example, raw and semi-finished products. Trading goods. Like raw materials, these are purchased from a merchant. Additional preparing of the material preceding exchanging is not performed. Work Cited Bannister, R. B. J. a. J. H., 2015. Conceptual Product Planning. In 2015 26th Annual SEMI Advanced Semiconductor Manufacturing Conference (ASMC) (pp. . IEEE.. s.l.:s.n. Cross, D., 2016. Globalization and Medias Impact on Cross Cultural Communication: Managing Organizational Change. Handbook of Research on Effective Communication, Leadership, and Conflict Resolution. s.l.:s.n. Davenport, T., 2013. Process innovation: reengineering work through information technology.. s.l.:Harvard Business Press. Doumeingts, G. a. B. J. e., 2016. Modelling techniques for business process re-engineering and benchmarking. s.l.:Springer. Fleischmann, A. B. E., 2014. Subject-oriented business process management. Springer Publishing Company, Incorporated.. s.l.:s.n. Frank, U., 2014. Multi-perspective enterprise modeling: foundational concepts, prospects and future research challenges. Software Systems Modeling,. In: s.l.:s.n., pp. 941-962. Geissdoerfer, M. B. N. a. H., 2016. Design thinking to enhance the sustainable business modelling processA workshop based on a value mapping process. Journal of Cleaner Production, 135(4), pp. 1218-1232. Gerlitz, L., 2016. Design management as a domain of smart and sustainable enterprise: business modelling for innovation and smart growth in industry 4.0." entrepreneurship and sustainability issues .. s.l.:s.n. Jonsson, P. a. M. S., 2016. Advanced material planning performance: a contextual examination and research agenda.. International Journal of Physical Distribution Logistics Management, , 46(9). Morecroft, J., 2015. Strategic modelling and business dynamics: A feedback systems approach.. ed. s.l.:John Wiley Sons.. Tang, M. a. L. B., 2016. Special issue on financial and business modelling and simulation. International Journal of Modelling and Simulation, pp. 1-1. Yu, E. H. J. .., 2013. Business modeling for business intelligence. Synthesis Lectures on Data Management. s.l.:s.n.