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Makalah Termodinamika Pemicu 5 - höyryneste tasapaino VLE - Kelompok 5.M akalah Termodinamika Pemicu 5 - Höyryn Liquid Equilibria VLE - Kelompok 5.MAKALAH TERMODINAMIKA PEMICU 5 HÖYRYNSULKU nestetasapainojen Dosen Ir Kamarza Mulia, Ph D Disusun oleh KELOMPOK 6 Astrini Pradyasti 1306370404 Mega Puspitasari 1306370713 Pangiastika Putri Wulandari 1306370493 Rayhan Hafidz 1306409362 Sahala Harahap 1306423190 universitas INDONESIASSA depok 2015.Makalah Termodinamika Pemicu 5 Vapor-Liquid Equilibria Kelompok 6 ja KATA PENGANTAR Puji syukur kehadirat Tuhan Yang Maha Esa yang telah melimpahkan rahmat päivä hidayah-Nya sehingga kami dapat menyelesaikan makalah ini dengan baik Penulisan makalah ini bertujuan untuk memenuhi tugas mata kuliah Termodinamika Dalam makalah Ini, kami ingin memaparkan jawaban Pemicu 5 mengenai Höyry-Liquid Equilibria Kami mengucapkan terima kasep kepada Pak Kamarza Mulia, sebagai dosen mata kuliah Termodinamika Tidak lupa juoma kami mengucapkan terima kasih kepada semua pihak yang telah membantu jäsenen dukungan kepada kelompok kami sehingga dapat Menyelesaikan makalah ini Semoga makalah ini dapat bermanfaat bagi semua pihak Kami menyadari dalam pembuatan karya tulis ini masih terdapat kekurangan Oleh karena itu, kritik dan dan saran dari para pembaca yang membangun sangat kami harapkan Depok, Mei 2015 Penulis. Makalah Termodinamika Pemicu 5 Vapor-Liquid Equilibria Kelompok 6 ii DAFTAR ISI Kata Pengantar ja Daftar Isi ii Jawaban Pemicu 1 Daftar Pustukka 37.Makalah Termodinamika Pemicu 5 Höyry-Liquid Equilibria Kelompok 6 1 JAWABAN PEMICU 5 Ensimmäinen osa 40 100 VLE-mallit Aan, Boy ja Cia innoissaan aloittaa Hysis , Kemian-, öljy - ja kaasuteollisuudessa käytettävän kehittyneen kemiallisen simulaattorin. He tulivat selville, että Hysis 32 - vaihtoehdossa tai - mallissa tai korrelaatiossa on monia höyry-neste-tasapainopohjaisia VLE-paketteja, joten he valitsivat seitsemän mallia jatko-opintoihinsa Antoine, NRTL, Lee-Kesler-Plocker, Margules, NBS Steam, Peng-Robinson ja PRSV. Käyttämällä jako - ja valloittamismenetelmää he jakoivat seuraavan suunnitelman. Malleja yhdeksi tai useammaksi seuraavaksi VLE-malliksi Valtion yhtälö, spesifinen korrelaatio, aktiivisuuskertoimen malli, karkeuskerrointimalli, ennustava malli Valmista taulukko, joka näyttää kunkin VLE-mallin ominaisuudet. Tarkastellaan seuraavia näkökohtia tyypillinen sovellus, esimerkki sopivista seoksista VLE-mallinnukseen, sopivaan lämpötila - ja painealueeseen, tavat optimoida mallin parametrit, kuten binääri-vuorovaikutusparametrin käyttäminen Hyvää suunnitelmaa huolimatta valitettavasti nämä opiskelijat olivat jumissa ja kääntyneet auttamaan sinua. Miten autat heitä Ensinnäkin, lue artikkeli VLE Don t Gamble, Physical Properties for Simulations, Eric C Carison, Chemical Engineering Progress, lokakuu 1996, s. 35-46 Vastaus State equation Lee-Kesler-Plocker, Peng-Robinson ja PRSV Aspects Peng - Robinson PRSV Tyypilliset sovellukset Öljy - ja kaasuteollisuus TEG-dehydraatio TEG-dehydraatio aromaattisilla aineilla Kryogeeninen kaasun prosessointi Ilman erottaminen Atm raa'at tornit Vacuum t Korkeat H2-järjestelmät Kryogeeninen kaasukäsittely Ilmansuodatus Kemikaalijärjestelmät. Makalah Termodinamika Pemicu 5 Vapor-Liquid Equilibria Kelompok 6 2 Säiliöjärjestelmät Hydraattiesteet Raakajärjestelmät Esimerkki VLE-mallinnukseen sopivasta seoksesta Hiilivetyseokset, kuten n-heptaani ja n-heksaani Hiilivetyseokset , Parempi polaarinen laskenta kuin PR Sopiva lämpötila - ja painealue Lämpötila -271 ° C tai - 456 ° F Paine 100 000 kPa tai 15 000 psia Lämpötila -271 ° C tai - 456 ° F Paine 100 000 kPa tai 15 000 psia Parametrien optimointi Malli Sekoitussäännöt 1 Sekoitussäännöt 1 Sumberin gambar Nasri, Zakia ja Housam Binous Peng Robinsonin valtion yhtälön soveltaminen MATLABin Tunisian kansallisen ammattikorkeakoulun ja tekniikan avulla Metod Korelasi-korrelaatiomenetelmä. Makalah Termodinamika Pemicu 5 Höyry-Liquid Equilibria Kelompok 6 3 Korelasi Adalah hubungan timbal balik antara satu persamaan keidas kuuma persamaan keadaan lainnya Korelasi di termodinamika Dapat dikelompokan menjadi dua yaitu korelasi spesifik erityinen korrelaatio dan korelasi umum universaali korrelaatio Korelasi Spesifik erityinen korrelaatio Korelasi spesifik adalah korelasi yang digunakan spesifik dengan satu parametri misalnya untuk penentuan tekanan uap jenuh yang dikenal dengan persamaan Antoine Pada persaman ini tekanan uap paine höyry tergantung pada lämpötila System b Korelasi Umum universaali korrelaatio Korelasi umum didasari dari teori persaalaa kylläsin haavoittuva vastaava tila yang menyatakan bahwa besarnya suatu besaran termodinamika dari berbagai fluida akan sama jika dievaluasi pada kondisi tereduksi yang sama misalnya pada suhu tereduksi Tr a tau tekanan tereduksi Pr Prinsip keadaan sebanding ini merupakan korelasi Umum PVT untuk menentukan besaran termodinamika seperti faktor kompresibilitas Z dan entalpi h Dalam penggunaan persamaan keadaan sebating untuk fluida murni memerlukan 2 parametri dan senyawa ei polaarinen memerlukan 3 parametri Salah s Atu contoh pada korelasi umum misalnya korelasi umum Pitzer, Lee-Kesler LK 1 malli Persamaan Antoine Antoine malli Persamaan Antoine merupakan salah satu metode korlei sederhana yang umum digunakan untuk menentukan tekananan uap jenuh Dengan persaman sebagai berikut 1, Tekanan rendah sampai menengah dan suhu dibawah titik didih normaali yang berprilaku sebagai kaasu ihanteellinen Persamaan Antoine tidak dapat diberlakukan pada tekanan tinggi dan suhu diatas titik didih normaali Seperti telah dijelaskan bahwa Malli Antoine berlaku untuk sistem pada tekanan rendah Persamaan Antoine ini tidak dapat digunakan untuk memprediksi pada Kesetimbangan cair-uap VLE untuk system operasi pada tekanan tinggi dan malli ini juga tidak dapat diterapkan pada järjestelmä hiilikuituinen rengas Malli Antoine telah. Makalah Termodinamika Pemicu 5 Höyry-Liquid Equilibria Kelompok 6 4 diterapkan untuk järjestelmä fraksinasi hydrokarbonaatti berat pada rentang tekanan dan suhu rendah sa Tm dabs - h 2 dsqrt g - malli Antoine adalah sebagai berikut Lämpötila K Paine psa Paine kPa 1, artinya Pestimasi kita terlalu renda maka nilainya harus dinaikkan Jika nilai 0 tai kolme identtistä oikeaa juurikappaletta 0 jos levy 0 0 sitten tt dabs - h 2 dsqrt g 3 27 h 2 4 uu dabs - h 2 - dsqrt g 3 27 h 2 4 zv tt 1 3 - uu 1 3 - q 3 zl zv palautuspää, jos jos levy 0 0 sitten tt - h 2 dsqrt g 3 27 h 2 4 Uu - h 2 - dsqrt g 3 27 h 2 4 jos tt 0 0 sitten zv1 tt 1 3 muuten zv1 - dabs tt 1 3 endif jos uu 0 0 sitten zv2 uu 1 3 muut sv2 - dabs uu 1 3 endif zv zv1 zv2 - Q 3 zl zv palaa endif. Makalah Termodinamika Pemicu 5 Vapor-Liquid Equilibria Kelompok 6 33 Kolme todellista epäidenttiä juurta, välivaihe ei ole fyysisesti merkityksellinen xa - h 2 dsqrt - g 3 27 phi 3 1415926535 2 - datan xa dsqrt 1 - xa 2 z 1 2 dsqrt - g 3 dcos phi 3 - q 3 z 2 2 dsqrt - g 3 dcos phi 3 2 094395 - q 3 z 3 2 dsqrt - g 3 dcos phi 3 4 188790 - q 3 zl dmin1 z 1, z 2, z 3 zv dmax1 z 1, z 2, z 3 paluu END -------------------- -------------------------------------------- SUBROUTINE CUBICCOEF a, b, C, T, p, c2, c1, c0 implisiittinen kaksinkertainen tarkkuus ah, oz R 0 08314 ------------------------------ ---------------------------------- Tulo kertoo tilavuuden kuutiopolynomin kertoimet kuutiolle EOS c2 - RT - Bpp c1 - 2 b RT 3 b 2 p - ap c0 b 2 RT b 3 p - abp paluu END. Makalah Termodinamika Pemicu 5 Vapor-Liquid Equilibria Kelompok 6 34 d Mittasuunnitelma Psykologinen kaavion biner propaani ja n-butaani Tabel 1 Höyry - Nestemäisen tasapainon mittaukset propaani 1 butaanijärjestelmässä 303,15 K Sumber J Chem Eng Data 2008, 53, 2783 2786, Seong et ai. T 303,15 KP MPa xy 0,284 0,000 0,000 0,324 0,054 0,132 0,364 0,113 0,266 0,456 0,235 0,464 0,529 0,330 0,582 0,611 0,436 0,686 0,693 0,543 0,768 0,775 0,641 0,826 0,856 0,736 0,882 0,910 0,802 0,916 0,966 0,866 0,945 1,010 0,919 0,966 1,049 0,964 0,986 1,079 1 000 1 000 Berdasarkan variasi nilai tekanan P dengan kompozisi x dan y pada suhu konstan yaitu T 3 03 15 K ärj ärj ärj ärj ärj ärj ärj ärj ärj är nämnda nana, diperoleh grafik sebagai berikut. Makalah Termodinamika Pemicu 5 Vapor-Liquid Equilibria Kelompok 6 35 Pituus 1 Kaavio Psykologinen propaani 1 n-butaani 2 pada 303 15 K Sumber Dokumen Pribadi Kameran 1 merupakan kaavio Fasa yang menunjukkan hubungan antara tekanan dengan komposiivin uup dan cair dari järjestelmä biner propaani 1 n-butaani 2 pada suhu konstan 303 15 K Garis berwarna oranssi merupakan tempat terjadinya titik gelembung Bubblepoint Sementara garis berwaran biru merupakan tempat terjadinya titik embun Kohdepiste Kedua garis ini akan bertemu Joka on päättynyt ja joka on päässyt paineen alaisena, kun P1 on istunut P2-kertaiseksi ja seokseen lisättiin propaania P1: aan, jolloin seokseen lisättiin x1 1 x 1,07 MPa: n paineessa jauhettuna n-butaani P2: ssä lisättiin jakeita x1 0 yaitu 0,284 MPa Pyyhkäisevä puhallusmateriaali täyttyy höyryllä, joka on höyryllä kuivaa, ja höyryssä on kuumennettu höyry Kurv A ini lebih lineaarinen dari kurva P-x1 Sementara kurva P-x1 menunjukkan keadaan cair jenuh tyydyttynyt neste dengan daerah diatasnya merupakan subcooled neste Daerah yang berada diantara dua titik kurva tersebut merupakan daerah dua fasa Berdasarkan kaavio terlihat bahwa komposisi fraksi uap pada suatu tekanan tertentu lebih Taakse pada komposisi fraksi cair Akan tetapi perubahan komposisi fraksi uap lebih kecil dibandingkan komposisi fraksi cair ketika mengalami peningkatan ataupun penurunan tekanan Hal ini yang menyebabkan kurva P-y1 lebih lineaarinen Dari kondisi 0 0,1 0,2 0,3 0,4 0 , 5 0,6 0,7 0,8 0,9 1 1,1 1,2 0 0,1 0,2 0,3 0,4 0,5 0,6 0,7 0,8 0,9 1 1,1 PMP a X1, y1 kuumennettu höyryn alijäähdytetty neste. Makalah Termodinamika Pemicu 5 Höyry-Liquid Equilibria Kelompok 6 36 kesetimbangan pada kondisi tetap konstan selama proses, ketika tekanan mengalami penurunan maka jumlah uap akan meningkat sementara jumlah neste menurun. Makalah Termodinamika Pemicu 5 Vapor-Liquid Equilibria Kelompok 6 3 7 DAFTAR PUSTAKA Smith, JM Van Ness, HC Abbott, MM Abbott, M, M 2001 Johdatus kemian tekniikkaan Termodynamiikka SI yksiköissä Kuudes painos Mc Graw-Hills Eric C Carlson, Dont Gamble fysikaalisten ominaisuuksien simuloinnit Aspen Technology Inc. Distilasi Atmosfer PROSES DISTILASI Proses distilasi disebut juga penyulingan adalah proses pemisahan berdasarkan tingkat penguapan atau titik didih suatu kampuran Pada penyulingan minyak bumi yang berupa monikomponentti pemisahannya dasarkan pada trayek didih atau fraksi-fraksinya sehingga prosesnya sering disebut juga proses fraksinasi Prosessit distilasi secara dibedakan menjadi 3 yaitu 1 Distikasi Atmosfer 2 Distilasi Hampa Vaccum 3 Distilasi Bertekanan Pada Raakaöljy Minyak savu distilasi yang dipakai adalah Distilasi Atmosfer atau distilasi pada tekanan sedikit diatas tekanan atmosfer Uraian proses dari penglohan raakaöljy menjadi tuotteet BBM diatas adalah sebagai berikut 1 Raakaöljy dipanaskan tahap awal dalam pipa Pada peralatan Yang biasa disebut dengan alat penukar panas Lämmönvaihdin HE Raakaöljy dipanaskan dengan media pemanas tuotteet yang akan di dinginkan atau memanfaatkan panas yang akan di buang Dari pemanfaatan panas suhu yang dapat di capai 219 OC 2 Selanjutnya Raakaöljy dipanaskan lebih lanjut dalam tungku dapur tanur atau Uunin kuivausrumpu, kuivausrumpu 330 OC 345 OC Raakaöljy dimasukkan dalam kolom fraksinasi, minyak yang mudah menguap berubah bentuk kaasu akan menguap päivä naik ke kolom bagian atas Semakin mudah menguap semakin naikissa Dalam perjalanan naik minu memerlukan energi, sehingga minyak seperti Aurinko dan minyak tanah akan mengembun lebih dulu tertampung diatas tray Uap minyak yang naik keatas akan dipertemukan dengan cairan yang sudah terbentuk menggunakan suatu alat yang disebut työkalu kontakta Suhu dalam kolom fraksinasi semakin keatas semakin rendah Suhu dasar pohja tidak jau beda dengan suhu masuk kolom, sedangkan Suhu puncak kolom top 100 OC 3 Cairan yang terbe Ntuk dikeluarkan dari tarjotin yang telah ditentukan sebagai tuote Tuotteen yang keluar panasnya dimanfaatkan terlebih dulu dengan menggunakan HE untuk memanaskan bahan baku Raakaöljy Setelah panasnya terserap maksimaalinen tuotesuunnittelu ja toimitusaika Pendingin atau Cooler dan kremudian disimpan dalam tanki 4 Tuotetta on varastossa 100% Kuumavalssattujen kondensaattoreiden, kuumavesikondensaattoreiden, kondensaattoreiden, kondensaattoreiden ja kondensaattoreiden valmistuksessa käytettävien kondensaattorien ja katalysaattoreiden valmistuksessa käytettävien katalysaattorien ja katalysaattorien valmistamiseksi. Jika kita mau belajar lebih dalam akan kita temuan bahwa proses CDU lebih komplekse dari yang saya tulis diatas Tuotteen Raaka tislaus yksikkö PRODUK PENGOLAHAN RAAKA DISTILLOINTI UNIT Sebagaimana yang dapat dilihat dari gambar proses yang terdahulu produk yang dihasilkan kilang yang diketahui awam adalah g As, bensin, minyak tanah kerosiini, aurinko, dan jäännös Jälkiplaneet yang terdahulu hania untuk menggambarkan seka awam bagaiman tuotteet kilang yang lebih dikenal dengan BBM itu dibuat, perlu diketahui bahwa sebenarnya tuotteet-tuotteet tersebut keluar dari proses belum merupakan produk jadi, tapi merupakan Bentuk-komponenttikomponentti yang harus di proses lagi dengan cara pencampuran sekoitus sehingga didapat produk yang dikehendaki Adapun produkum atau produk yang langsung keluar dari proses kilang adalah sebagai berikut LPG, kevyt naphta, raskaan naphta, kerosiini minyak tanah, LGO, HGO, dan Residue Untuk lebih jelasnya akan kita bahas satu persatu mulai keluar kolom dari alkuun sampai pohja hingga keluar tuotteet tersebut jadi Yang pertama Tuote Light End merupakan tuotteet top kolom, yang meliputi LPG, valo Naphta, ja Raskas Naphta Pemisahan tuotetta ini dapat lihan pada kaavio Urainan Proses Uapin kaveri, joka on päättynyt kolonni fraksinasi dikondensasikan, hasil kondensasi berupa naphta ya Kierrättävän vakaat karnaamiset kaasupullot Kaasusuodattimet, jotka on valmistettu stabilisaattorista, jotka toimivat kaasun päällä ja jotka toimivat kaasun päällä ja jotka on valmistettu C1-C2-hiilidioksidipäästöistä kaasun ja kaasun päästöjen välillä C3-C4 hitsauslaitteita nestekaasua sisältävän nestekaasun C4-butaani Tuotteen pohja stabilizer berupa naphta dipisahkan menjadi lihgt naphta dan heavy naphta di splitter Produk light naphta digunakan untuk komponen blending bensin atau digunakan sebagai pelarut semisal thinner Heavy naphta disamping digunakan untuk komponen blending juga digunakan untuk feed umpan proses Naphta Hydro Treater NHDT yang produknya disebut Sweet Naphta dan digunakan feed proses Platforming untuk menghasilkan Reformat yang merupakan Hight Okta number Mogas Component atau digunakan sebagai umpan proses selanjutnya Bensin yang kita kenal adalah merupakan hasil pencampuran Blending HOMC, L Naphta dan Heavy Naphta HOMC Hight Octane number Mogas Component atau komponen bensin dengan octane number tinggi, dihasilkan dari proses sukunder Produk selanjutnya adalah produk midle distillate yang akan saya sampaikan nanti Hal yang perlu diperhatikan pada proses pengolahan minyak CDU HAL-HAL YANG PERLU DIPERHATIKAN PROSES PENGOLAHAN MINYAK BUMI CDU DISTILLASI ATMOSFERIK Pada umumnya tujuan suatu proses produksi adalah ditujukan untuk memenuhi kebutuhan akan sesuatu, sehingga ada syarat atau baku mutu yang diharapkan Semisal kita pingin punya sepeda motor maka kita akan berpikir berapa jumlah, warna, cc, jenis yang kita inginkan Demikian juga pada pengolahan di kilang yang perlu kita perhatikan adalah hasil produk yang kita inginkan baik itu jumlah maupun baku mutunya Penetapan baku mutu produk dalam hal ini BBM ditentukan oleh dirjen migas, berdasarkan kebutuhan mesin dan standar lingkungan yang harus dipenuhi Untuk mendapatkan hasil distilasi yang sesuai dengan harapan, variable operasi yang perlu diperhatikan adalah suhu dan tekanan proses Pada proses distilasi yang sederhana letak k eluarannya draw off produk sudah diatur sedemikian rupa sehingga pengaturan suhu dialakukan pada masukan inlet kolom distilasi dan topnya, sedang pada draw off masing-masing produk akan teratur dengan sendirinya Tekanan top kolom dijaga tetap kurang lebih 0,3 kg cm2 untuk suhu inlet kolom berkisar antara 329 345 oC, pemanasan tidak boleh lebih dari 370OC karena pada suhu tersebut minyak bumi akan mengalami cracking patah rantainya sedangkan suhu top kolom dijaga 100oC Pada design kilang yang lebih modern tiap-tiap keluaran produk atau draw off memiliki beberapa fasilitas pangaturan seperti pump around dan reflux, sehingga pengaturan untuk mencapai baku mutu produk lebih flexible Kondisi yang lain yang perlu diperhatikan kebanyakan berhubungan dengan keselamatan safety , dan design masing-masing peralatan proses PROSES PENGOLAHAN MINYAK Ditinjau dari sifat proses pengolahan crude oil menjadi berbagai produk dikelompokkan menjadi 2 yaitu 1 Proses fisis Proses fisis adalah proses pengol ahan atau pemisahan minyak bumi dan turunannya, tanpa merubah struktur kimia dari komponen-komponen minyak bumi tersebut Atau proses yang terjadi adalah prose fisika saja Proses-proses tersebut diantaranya adalah - Proses Distilasi - Proses ekstraksi - Proses kristalisasi - Absorpsi 2 Proses kimia Proses kemis adalah proses pengolahan minyak bumi dan turunannya dengan merubah struktur kimia dari komponen minyak bumi tersebut Perubahan tersebut dapat berupa pemisahan rantai Cracking , peruraian, atau penggabungan komponen minyak bumi Proses-proses tersebut diantaranya adalah - Cracking - Reforming - Hydrotreating - Alkilasi - Polimerisasi - Dan lain-lain PROSES DISTILASI Proses distilasi disebut juga penyulingan adalah proses pemisahan berdasarkan tingkat penguapan atau titik didih suatu campuran Pada penyulingan minyak bumi yang berupa multi komponen pemisahannya di dasarkan pada trayek didih atau fraksi-fraksinya sehingga prosesnya sering disebut juga proses fraksinasi Proses distilas i secara umum dibedakan menjadi 3 yaitu Distikasi Atmosfer Distilasi Hampa Vaccum Distilasi Bertekanan Proses diatas dipilih berdasarkan bahan baku yang diolah Distillation Introduction Distillation separates chemicals by the difference in how easily they vaporize The two major types of classical distillation include continuous distillation and batch distillation, as the name says, continuously takes a feed and separates it into two or more products Batch distillation takes on lot or batch at a time of feed and splits it into products by selectively removing the more volatile fractions over time Other ways to categorize distillation are by the equipment type trays, packing , process configuration distillation, absorption, stripping, azeotropic, extractive, complex , or process type refining, petrochemical, chemical, gas treating In all cases, what must be kept in mind is that distillation involves both equipment and theory Sound analysis with basic principles underlies any successful d istillation process However, putting basics into practice requires real equipment Process design tells us what equipment needs to accomplish to meet our plant goals Equipment limits set what a specific unit can achieve Putting successful distillation units in place requires combining both the theoretical knowledge of the distillation fundamentals along with equipment understanding The Distillation Group puts both of these areas together to work in your process We approach troubleshooting, equipment design, process analysis, and revamps by combining knowledge of fundamentals and of how equipment really works This gives reliable results and effective and profitable plant operation The following information gives a short background to the rest of the distillation information in this site Historical Background Distillation has been around for a long time Earliest references are to Maria the Jewess who invented many types of stills and reflux Middle Ages and Renaissance uses of distillation included the manufacture of brandy and other spirits from wine Another early use was the manufacture of perfumes and essences Other early users of distillation include the Alchemists Of course, the history of distillation does not end there Today we use it for more than just spirits Many industries use distillation for critical separations in making useful products These industries include petroleum refining, beverages, chemical processing, petrochemicals, and natural gas processing The beverage industy is the one of the oldest users of distillation Distillation of ethanol for both consumption and other uses was one of the first major industries ever developed Ethanol has often been considered as a fuel At times, this has even been done F B Wright published a major work on production and distillation of fuel ethanol in 1906 A copy of the second edition 1907 from the DGI collection of historical material can be viewed or downloaded This is a large document 293 pages, 2 43M A smaller ve rsion using low resolution graphics is also available 1 47M Natural gas processing started using distillation in the early 1900 s An interesting historical document, Condensation of Gasoline from Natural Gas, documents some early steps in this industry Recent developments energy shortages have re-focused attention on major industrial energy users Distillation is a major energy consumer During the energy crisis of the 1970s much effort was put into making distillation more efficient A good example of this work is summarized in the Distillation Operations Manual from the Texas Industrial Commission Distillation Today Distillation Categories Distillation services can be sorted out into many different categories Here are some basic definitions System composition System refers to the chemical components present in the mixture being distilled The two main groups are binary distillation and multicomponent distillation Binary distillation is a separation of only two chemicals A good example is separating ethyl alcohol ethanol from water Most of the basic distillation teaching and a lot of theoretical work starts with looking at binary distillation it s a lot simpler Multicomponent distillation is the separation of a mixture of chemicals A good example is petroleum refining Crude oil is a very complex mixture of hydrocarbons with literally thousands of different molecules Nearly all commercial distillation is multicomponent distillation The theory and practice of multicomponent distillation can be very complex Processing Mode Processing mode refers to the way in which feed and product are introduced and withdrawn from the process Distillation occurs in two modes, continuous distillation and batch distillation Continuous distillation is feed is sent to the still all the time and product is drawn out at the same time The idea in continuous distillation is that the amount going into the still and the amount leaving the still should always equal each other at any given point in time Batch distillation is when the amount going into the still and the amount going out of the still is not supposed to be the same all the time The easiest example to use is like old fashioned spirit making The distiller fills a container at the start, then heats it, as time goes by the vapors are condensed to make the alcoholic drink When the proper quantity of overhead drink is made, the distiller stops the still and empties it out ready for a new batch This is only a simple case, in industrial usage what goes on gets very complex Both continuous and batch distillation are very important to industry Continuous distillation is most often used with big volume products like jet fuel, benzene, plastic monomers Batch distillation is most often used with smaller volume products and in plants that make lots of different things and use the same still for many products in different batches Processing sequence Fractionation systems have different objectives The major processing objectives se t the system type and the equipment configuration needed The common objectives include removing a light component from a heavy product, removing a heavy component from a light product, making two products, or making more than two products We will call these major categories are called stripping, rectification, fractionation, and complex fractionation This terminology may be a little confusing because we also use the terms stripping and fractionation when we discuss heat flow options through the unit This confusion results from historical use of the terms and you just need to keep the context in mind when reading or discussing the material With a little practice you will find that the reason for using the same terms is that many of the systems called stripping or fractionation systems have the same characteristics regardless of using a processing sequence or heat flow analysis of the unit Stripping systems remove light material from a heavy product Rectification systems remove heavy mat erial from a light product Fractionation systems remove a light material from a heavy product and a heavy material from a light product at the same time Complex fractionation makes multiple products from either a single tower or a complex of towers combined with recycle streams between them A good example of a multiple product tower is a refinery crude distillation tower making rough cuts of naphtha gasoline , kerosene jet fuel , and diesel from the same tower A good example of a complex tower with internal recycle streams is a Petlyck baffle tower making three onspecifications products from the same tower System type The behavior of the chemicals in the system also determines the system configuration for the objectives The three major problems that limit distillation processes are close-boilers, distributed keys, and azeotropes Other problems that may require using special system configurations include heat sensitive materials Close boiler systems include chemicals that boil at temper atures very close to each other So many stages of distillation or so much reflux may be required that the chemicals cannot be separated economically A good example is separation of nitro-chloro-benzenes Up to 600 theoretical separation stages with high reflux may be required to separate different isomers Distributed keys are systems where some chemicals that we do not want in either the heavy or the light product boil at a temperature between the heavy and the light product Azeotropic systems are those where the vapor and the liquid reach the same composition at some point in the distillation No further separation can occur Ethanol-water is a perfect example Once ethanol composition reaches 95 at atmospheric pressure , no further ethanol purification is possible Close boilers and distributed keys are economic problems The compounds can be separated, but it costs a lot Azeotropic systems are fundamental thermodynamic problems At the distillation conditions, the products can only be dist illed to a certain point, no further Different ways to get around these problems include using other techniques membranes, crystallization, adsorption, adduction, extraction, precipitation , using complex distillation configurations, changing system conditions, or adding extra chemicals to the process Adding extra chemicals includes azeotropic distillation, extractive distillation, or salt distillation System type Azeotropic and extractive distillation use the addition of a mass separating agent MSA to modify the thermodynamic behavior of the system Many different azeotropic and extractice distillation configurations are in use Azeotropic distillation uses a MSA that forms a minimum boiling azeotrope with some of the feed components is used The azeotrope is taken overhead and the MSA rich phase decanted and returned to the column as reflux Extractive distillation uses a MSA that increases the volatility difference between the compounds to be separated A good example is sulfolane to inc rease the relative volatility difference between similar molecular weight aromatic and paraffinic hydrocarbons The sulfolane unit combines liquid-liquid extraction, extractive distillation, and solvent stripping in one process Salt distillation adds a salt to the system to modify the thermodynamic behavior of the system The salt is normally added to the liquid supply of a batch distillation system All of these types of systems are normally considered complex systems Other equipment is needed to separate and reuse the added MSA Very complex configurations can result Good understanding of system thermodynamics is required to predict behavior Heat flow Energy transfer is required to make separations work Heat flow refers to the arrangement of the distillation column to its heat source and heat sink The major categories are fractionation distillation , absorption, stripping, and contacting This terminology may be a little confusing because we also use the terms stripping and fractionation when we discuss processing sequence options in distillation This confusion results from historical use of the terms and you just need to keep the context in mind when reading or discussing the material With a little practice you will find that the reason for using the same terms is that many of the systems called stripping or fractionation systems have the same characteristics regardless of using a processing sequence or heat flow analysis of the unit Fractionation refers to units that have both a reboiler and a condenser Something is attached to the bottom of the tower to put heat into the tower and something attached to the top of the tower to take heat out of the is what is normally called distillation Absorption is a unit that has no method at the top of the tower to take heat out An external stream is supplied from outside the system to absorb material from the vapor Stripping is a unit that has no method at the bottom of the tower to put heat in An external stream is supplied fro m outside the system to strip material from the liquid Contacting is a unit that has neither a method at the top of the tower to remove heat nor a method at the bottom of the tower to put heat in Two streams run countercurrent to each other Both streams are generated outside the mass-transfer system What can make things unclear is that these terms have both other meanings and can be used imprecisely Also, towers can have intermediate heat input and heat removal equipment in the middle This confuses the picture But we will use the strict definitions above An absorber is a tower without a condenser A stripper is a tower without a reboiler A contactor has neither and a fractionator has both Reaction Reactive distillation uses a reaction in the distillation equipment to help the separation The reaction may or may not use a catalyst DMT manufacture uses reactive distillation without a catalyst One process to make methy-tert-butyl-ether uses a catalyst inside the distillation tower The react ion changes the composition, allowing the distillation to work better Equipment Type Distillation equipment includes two major categories, trays and packing Trays force a rising vapor to bubble through a pool of descending liquid Packing creates a surface for liquid to spread on The thin liquid film has a high surface area for mass-transfer between the liquid and vapor Photograph Gallery Distillation units come in many different configurations The configuration depends upon the service, capital versus operating cost optimization, and technology available when the unit is constructed To see a selection of different units visit our photo gallery Distillation Laboratory display of distillation 1 A heating device 2 Still pot 3 Still head 4 Thermometer Boiling point temperature 5 Condenser 6 Cooling water in 7 Cooling water out 8 Distillate receiving flask 9 Vacuum gas inlet 10 Still receiver 11 Heat control 12 Stirrer speed control 13 Stirrer heat plate 14 Heating Oil sand bath 15 Stirring means e g shown , anti-bumping granules or mechanical stirrer 16 Cooling bath Distillation is a method of separating mixtures based on differences in their volatilities in a boiling liquid mixture Distillation is a unit operation, or a physical separation process, and not a chemical reaction Commercially, distillation has a number of applications It is used to separate crude oil into more fractions for specific uses such as transport, power generation and heating Water is distilled to remove impurities, such as salt from seawater Air is distilled to separate its components notably oxygen, nitrogen, and argon for industrial use Distillation of fermented solutions has been used since ancient times to produce distilled beverages with a higher alcohol content The premises where distillation is carried out, especially distillation of alcohol, are known as a distillery History Distillation apparatus of Zosimus, from Marcelin Berthelot, Collection des anciens alchimistes grecs 3 vol Paris, 1 887-1888 Early types of distillation were known to the Babylonians in Mesopotamia in what is now Iraq from at least the 2nd millennium BC 2 Archaeological excavations in northwest Pakistan have yielded evidence that the distillation of alcohol was known in the Indian subcontinent since 500 BC, 3 but only became common between 150 BC - 350 AD 3 Primitive tribes of India used a method of distillation for producing Mahuda liquor This crude and ancient method is not very effective 4 Distillation was later known to Hellenistic alchemists from the 1st century AD, 5 6 7 and the later development of large-scale distillation apparatus occurred in response to demands for spirits 5 According to K B Hoffmann the earliest mention of destillatio per descensum occurs in the writings of Aetius, a Greek physician from the 5th century 8 Hypatia of Alexandria is credited with having invented an early distillation apparatus, 9 and the first clear description of early apparatus for distillation is given by Zosimos of Panopolis in the fourth century 7 The invention of highly effective pure distillation is credited to Arabic and Persian chemists in the Middle East from the 8th century They produced distillation processes to isolate and purify chemical substances for industrial purposes such as isolating natural esters perfumes and producing pure alcohol 10 The first among them was Jabir ibn Hayyan Geber , in the 8th century, who is credited with the invention of numerous chemical apparatus and processes that are still in use today In particular, his alembic was the first still with retorts which could fully purify chemicals, a precursor to the pot still, and its design has served as inspiration for modern micro-scale distillation apparatus such as the Hickman stillhead 11 The isolation of ethanol alcohol as a pure compound through distillation was first achieved by the Arab chemist Al-Kindi Alkindus 12 Petroleum was first distilled by the Persian alchemist Muhammad ibn Zakar ya Rzi Rhazes in the 9th century, for producing kerosene, 13 while steam distillation was invented by Avicenna in the early 11th century, for producing essential oils 14 As the works of Middle Eastern scribes made their way to India and became a part of Indian alchemy, several texts dedicated to distillation made their way to Indian libraries 15 Among these was a treatise written by a scholar from Bagdad in 1034 titled Ainu-s-Sana ah wa Auna-s-Sana ah 15 Scholar Al-Jawbari travelled to India 16 By the time of the writing of the Ain-e-Akbari, the process of distillation was well known in India 17 Distillation was introduced to medieval Europe through Latin translations of Arabic chemical treatises in the 12th century 18 In 1500, German alchemist Hieronymus Braunschweig published Liber de arte destillandi The Book of the Art of Distillation 19 the first book solely dedicated to the subject of distillation, followed in 1512 by a much expanded version In 1651, John French published The Art of Distillat ion the first major English compendium of practice, though it has been claimed 20 that much of it derives from Braunschweig s work This includes diagrams with people in them showing the industrial rather than bench scale of the operation Distillation As alchemy evolved into the science of chemistry, vessels called retorts became used for distillations Both alembics and retorts are forms of glassware with long necks pointing to the side at a downward angle which acted as air-cooled condensers to condense the distillate and let it drip downward for collection Later, copper alembics were invented Riveted joints were often kept tight by using various mixtures, for instance a dough made of rye flour 21 These alembics often featured a cooling system around the beak, using cold water for instance, which made the condensation of alcohol more efficient These were called pot stills Today, the retorts and pot stills have been largely supplanted by more efficient distillation methods in most indus trial processes However, the pot still is still widely used for the elaboration of some fine alcohols such as cognac, Scotch whisky, tequila and some vodkas Pot stills made of various materials wood, clay, stainless steel are also used by bootleggers in various countries Small pot stills are also sold for the domestic production 22 of flower water or essential oils Early forms of distillation were batch processes using one vaporization and one condensation Purity was improved by further distillation of the condensate Greater volumes were processed by simply repeating the distillation Chemists were reported to carry out as many as 500 to 600 distillations in order to obtain a pure compound 23 In the early 19th century the basics of modern techniques including pre-heating and reflux were developed, particularly by the French 23 , then in 1830 a British Patent was issued to Aeneas Coffey for a whiskey distillation column 24 , which worked continuously and may be regarded as the archetype of modern petrochemical units In 1877, Ernest Solvay was granted a U S Patent for a tray column for ammonia distillation 25 and the same and subsequent years saw developments of this theme for oil and spirits With the emergence of chemical engineering as a discipline at the end of the 19th century, scientific rather than empirical methods could be applied The developing petroleum industry in the early 20th century provided the impetus for the development of accurate design methods such as the McCabe-Thiele method and the Fenske equation The availability of powerful computers has also allowed direct computer simulation of distillation columns Applications of distillation The application of distillation can roughly be divided in four groups laboratory scale, industrial distillation, distillation of herbs for perfumery and medicinals herbal distillate , and food processing The latter two are distinctively different from the former two in that in the processing of beverages, the distillati on is not used as a true purification method but more to transfer all volatiles from the source materials to the distillate The main difference between laboratory scale distillation and industrial distillation is that laboratory scale distillation is often performed batch-wise, whereas industrial distillation often occurs continuously In batch distillation, the composition of the source material, the vapors of the distilling compounds and the distillate change during the distillation In batch distillation, a still is charged supplied with a batch of feed mixture, which is then separated into its component fractions which are collected sequentially from most volatile to less volatile, with the bottoms remaining least or non-volatile fraction removed at the end The still can then be recharged and the process repeated In continuous distillation, the source materials, vapors, and distillate are kept at a constant composition by carefully replenishing the source material and removing fracti ons from both vapor and liquid in the system This results in a better control of the separation process Idealized distillation model The boiling point of a liquid is the temperature at which the vapor pressure of the liquid equals the pressure in the liquid, enabling bubbles to form without being crushed A special case is the normal boiling point, where the vapor pressure of the liquid equals the ambient atmospheric pressure It is a common misconception that in a liquid mixture at a given pressure, each component boils at the boiling point corresponding to the given pressure and the vapors of each component will collect separately and purely This, however, does not occur even in an idealized system Idealized models of distillation are essentially governed by Raoult s law and Dalton s law, and assume that vapor-liquid equilibria are attained Raoult s law assumes that a component contributes to the total vapor pressure of the mixture in proportion to its percentage of the mixture and its vapor pressure when pure, or succinctly partial pressure equals mole fraction multiplied by vapor pressure when pure If one component changes another component s vapor pressure, or if the volatility of a component is dependent on its percentage in the mixture, the law will fail Dalton s law states that the total vapor pressure is the sum of the vapor pressures of each individual component in the mixture When a multi-component liquid is heated, the vapor pressure of each component will rise, thus causing the total vapor pressure to rise When the total vapor pressure reaches the pressure surrounding the liquid, boiling occurs and liquid turns to gas throughout the bulk of the liquid Note that a mixture with a given composition has one boiling point at a given pressure, when the components are mutually soluble An implication of one boiling point is that lighter components never cleanly boil first At boiling point, all volatile components boil, but for a component, its percentage in the v apor is the same as its percentage of the total vapor pressure Lighter components have a higher partial pressure and thus are concentrated in the vapor, but heavier volatile components also have a smaller partial pressure and necessarily evaporate also, albeit being less concentrated in the vapor Indeed, batch distillation and fractionation succeed by varying the composition of the mixture In batch distillation, the batch evaporates, which changes its composition in fractionation, liquid higher in the fractionation column contains more lights and boils at lower temperatures The idealized model is accurate in the case of chemically similar liquids, such as benzene and toluene In other cases, severe deviations from Raoult s law and Dalton s law are observed, most famously in the mixture of ethanol and water These compounds, when heated together, form an azeotrope, which is a composition with a boiling point higher or lower than the boiling point of each separate liquid Virtually all liqu ids, when mixed and heated, will display azeotropic behaviour Although there are computational methods that can be used to estimate the behavior of a mixture of arbitrary components, the only way to obtain accurate vapor-liquid equilibrium data is by measurement It is not possible to completely purify a mixture of components by distillation, as this would require each component in the mixture to have a zero partial pressure If ultra-pure products are the goal, then further chemical separation must be applied When a binary mixture is evaporated and the other component, e g a salt, has zero partial pressure for practical purposes, the process is simpler and is called evaporation in engineering Batch distillation A batch still showing the separation of A and B Heating an ideal mixture of two volatile substances A and B with A having the higher volatility, or lower boiling point in a batch distillation setup such as in an apparatus depicted in the opening figure until the mixture is boilin g results in a vapor above the liquid which contains a mixture of A and B The ratio between A and B in the vapor will be different from the ratio in the liquid the ratio in the liquid will be determined by how the original mixture was prepared, while the ratio in the vapor will be enriched in the more volatile compound, A due to Raoult s Law, see above The vapor goes through the condenser and is removed from the system This in turn means that the ratio of compounds in the remaining liquid is now different from the initial ratio i e more enriched in B than the starting liquid The result is that the ratio in the liquid mixture is changing, becoming richer in component B This causes the boiling point of the mixture to rise, which in turn results in a rise in the temperature in the vapor, which results in a changing ratio of A B in the gas phase as distillation continues, there is an increasing proportion of B in the gas phase This results in a slowly changing ratio A B in the distillate I f the difference in vapor pressure between the two components A and B is large generally expressed as the difference in boiling points , the mixture in the beginning of the distillation is highly enriched in component A, and when component A has distilled off, the boiling liquid is enriched in component B Continuous distillation Main article Continuous distillation Continuous distillation is an ongoing distillation in which a liquid mixture is continuously without interruption fed into the process and separated fractions are removed continuously as output streams as time passes during the operation Continuous distillation produces at least two output fractions, including at least one volatile distillate fraction, which has boiled and been separately captured as a vapor condensed to a liquid There is always a bottoms or residue fraction, which is the least volatile residue that has not been separately captured as a condensed vapor Continuous distillation differs from batch distillation in the respect that concentrations should not change over time Continuous distillation can be run at a steady state for an arbitrary amount of time Given a feed of in a specified composition, the main variables that affect the purity of products in continuous distillation are the reflux ratio and the number of theoretical equilibrium stages practically, the number of trays or the height of packing Reflux is a flow from the condenser back to the column, which generates a recycle that allows a better separation with a given number of trays Equilibrium stages are ideal steps where compositions achieve vapor-liquid equilibrium, repeating the separation process and allowing better separation given a reflux ratio A column with a high reflux ratio may have fewer stages, but it refluxes a large amount of liquid, giving a wide column with a large holdup Conversely, a column with a low reflux ratio must have a large number of stages, thus requiring a taller column Continuous distillation require s building and configuring dedicated equipment The resulting high investment cost restricts its use to the large scale General improvements Both batch and continuous distillations can be improved by making use of a fractionating column on top of the distillation flask The column improves separation by providing a larger surface area for the vapor and condensate to come into contact This helps it remain at equilibrium for as long as possible The column can even consist of small subsystems trays or dishes which all contain an enriched, boiling liquid mixture, all with their own vapor-liquid equilibrium There are differences between laboratory-scale and industrial-scale fractionating columns, but the principles are the same Examples of laboratory-scale fractionating columns in increasing efficiency include Air condenser Vigreux column usually laboratory scale only Packed column packed with glass beads, metal pieces, or other chemically inert material Spinning band distillation system Laboratory scale distillation Laboratory scale distillations are almost exclusively run as batch distillations The device used in distillation, sometimes referred to as a still, consists at a minimum of a reboiler or pot in which the source material is heated, a condenser in which the heated vapour is cooled back to the liquid state, and a receiver in which the concentrated or purified liquid, called the distillate, is collected Several laboratory scale techniques for distillation exist see also distillation types Simple distillation In simple distillation, all the hot vapors produced are immediately channeled into a condenser that cools and condenses the vapors Therefore, the distillate will not be pure its composition will be identical to the composition of the vapors at the given temperature and pressure, and can be computed from Raoult s law As a result, simple distillation is usually used only to separate liquids whose boiling points differ greatly rule of thumb is 25 C , 26 or t o separate liquids from involatile solids or oils For these cases, the vapor pressures of the components are usually sufficiently different that Raoult s law may be neglected due to the insignificant contribution of the less volatile component In this case, the distillate may be sufficiently pure for its intended purpose Fractional distillation For many cases, the boiling points of the components in the mixture will be sufficiently close that Raoult s law must be taken into consideration Therefore, fractional distillation must be used in order to separate the components well by repeated vaporizationcondensation cycles within a packed fractionating column This separation, by successive distillations, is also referred to as rectification 27 As the solution to be purified is heated, its vapors rise to the fractionating column As it rises, it cools, condensing on the condenser walls and the surfaces of the packing material Here, the condensate continues to be heated by the rising hot vapor s it vaporizes once more However, the composition of the fresh vapors are determined once again by Raoult s law Each vaporization-condensation cycle called a theoretical plate will yield a purer solution of the more volatile component 28 In reality, each cycle at a given temperature does not occur at exactly the same position in the fractionating column theoretical plate is thus a concept rather than an accurate description More theoretical plates lead to better separations A spinning band distillation system uses a spinning band of Teflon or metal to force the rising vapors into close contact with the descending condensate, increasing the number of theoretical plates 29 Steam distillation Main article Steam distillation Like vacuum distillation, steam distillation is a method for distilling compounds which are heat-sensitive 30 This process involves using bubbling steam through a heated mixture of the raw material By Raoult s law, some of the target compound will vaporize in accordanc e with its partial pressure The vapor mixture is cooled and condensed, usually yielding a layer of oil and a layer of water Steam distillation of various aromatic herbs and flowers can result in two products an essential oil as well as a watery herbal distillate The essential oils are often used in perfumery and aromatherapy while the watery distillates have many applications in aromatherapy, food processing and skin care Dimethyl sulfoxide usually boils at 189 C Under a vacuum, it distills off into the receiver at only 70 C Perkin triangle distillation setup 1 Stirrer bar anti-bumping granules 2 Still pot 3 Fractionating column 4 Thermometer Boiling point temperature 5 Teflon tap 1 6 Cold finger 7 Cooling water out 8 Cooling water in 9 Teflon tap 2 10 Vacuum gas inlet 11 Teflon tap 3 12 Still receiver Vacuum distillation Some compounds have very high boiling points To boil such compounds, it is often better to lower the pressure at which such compounds are boiled instead of increasi ng the temperature Once the pressure is lowered to the vapor pressure of the compound at the given temperature , boiling and the rest of the distillation process can commence This technique is referred to as vacuum distillation and it is commonly found in the laboratory in the form of the rotary evaporator This technique is also very useful for compounds which boil beyond their decomposition temperature at atmospheric pressure and which would therefore be decomposed by any attempt to boil them under atmospheric pressure Molecular distillation is vacuum distillation below the pressure of 0 01 torr 31 0 01 torr is one order of magnitude above high vacuum, where fluids are in the free molecular flow regime, i e the mean free path of molecules is comparable to the size of the equipment The gaseous phase no longer exerts significant pressure on the substance to be evaporated, and consequently, rate of evaporation no longer depends on pressure That is, because the continuum assumptions of fl uid dynamics no longer apply, mass transport is governed by molecular dynamics rather than fluid dynamics Thus, a short path between the hot surface and the cold surface is necessary, typically by suspending a hot plate covered with a film of feed next to a cold plate with a clear line of sight in between Molecular distillation is used industrially for purification of oils Air-sensitive vacuum distillation Some compounds have high boiling points as well as being air sensitive A simple vacuum distillation system as exemplified above can be used, whereby the vacuum is replaced with an inert gas after the distillation is complete However, this is a less satisfactory system if one desires to collect fractions under a reduced pressure To do this a pig adaptor can be added to the end of the condenser, or for better results or for very air sensitive compounds a Perkin triangle apparatus can be used The Perkin triangle, has means via a series of glass or Teflon taps to allows fractions to be i solated from the rest of the still, without the main body of the distillation being removed from either the vacuum or heat source, and thus can remain in a state of reflux To do this, the sample is first isolated from the vacuum by means of the taps, the vacuum over the sample is then replaced with an inert gas such as nitrogen or argon and can then be stoppered and removed A fresh collection vessel can then be added to the system, evacuated and linked back into the distillation system via the taps to collect a second fraction, and so on, until all fractions have been collected Short path distillation Short path vacuum distillation apparatus with vertical condenser cold finger , to minimize the distillation path 1 Still pot with stirrer bar anti-bumping granules 2 Cold finger - bent to direct condensate 3 Cooling water out 4 cooling water in 5 Vacuum gas inlet 6 Distillate flask distillate Short path distillation is a distillation technique that involves the distillate travelling a sho rt distance, often only a few centimeters, and is normally done at reduced pressure 32 A classic example would be a distillation involving the distillate travelling from one glass bulb to another, without the need for a condenser separating the two chambers This technique is often used for compounds which are unstable at high temperatures or to purify small amounts of compound The advantage is that the heating temperature can be considerably lower at reduced pressure than the boiling point of the liquid at standard pressure, and the distillate only has to travel a short distance before condensing A short path ensures that little compound is lost on the sides of the apparatus The Kugelrohr is a kind of a short path distillation apparatus which often contain multiple chambers to collect distillate fractions Other types The process of reactive distillation involves using the reaction vessel as the still In this process, the product is usually significantly lower-boiling than its reactant s As the product is formed from the reactants, it is vaporized and removed from the reaction mixture This technique is an example of a continuous vs a batch process advantages include less downtime to charge the reaction vessel with starting material, and less workup Pervaporation is a method for the separation of mixtures of liquids by partial vaporization through a non-porous membrane Extractive distillation is defined as distillation in the presence of a miscible, high boiling, relatively non-volatile component, the solvent, that forms no azeotrope with the other components in the mixture Flash evaporation or partial evaporation is the partial vaporization that occurs when a saturated liquid stream undergoes a reduction in pressure by passing through a throttling valve or other throttling device This process is one of the simplest unit operations, being equivalent to a distillation with only one equilibrium stage Codistillation is distillation which is performed on mixtures in w hich the two compounds are not miscible The unit process of evaporation may also be called distillation In rotary evaporation a vacuum distillation apparatus is used to remove bulk solvents from a sample Typically the vacuum is generated by a water aspirator or a membrane pump In a kugelrohr a short path distillation apparatus is typically used generally in combination with a high vacuum to distill high boiling 300 C compounds The apparatus consists of an oven in which the compound to be distilled is placed, a receiving portion which is outside of the oven, and a means of rotating the sample The vacuum is normally generated by using a high vacuum pump Other uses Dry distillation or destructive distillation, despite the name, is not truly distillation, but rather a chemical reaction known as pyrolysis in which solid substances are heated in an inert or reducing atmosphere and any volatile fractions, containing high-boiling liquids and products of pyrolysis, are collected The destru ctive distillation of wood to give methanol is the root of its common name - wood alcohol Freeze distillation is an analogous method of purification using freezing instead of evaporation It is not truly distillation, but a recrystallization where the product is the mother liquor, and does not produce products equivalent to distillation This process is used in the production of ice beer and ice wine to increase ethanol and sugar content, respectively It is also used to produce applejack Unlike distillation, freeze distillation concentrates poisonous congeners rather than removing them Azeotropic distillation Main article Azeotropic distillation Interactions between the components of the solution create properties unique to the solution, as most processes entail nonideal mixtures, where Raoult s law does not hold Such interactions can result in a constant-boiling azeotrope which behaves as if it were a pure compound i e boils at a single temperature instead of a range At an azeotrope, th e solution contains the given component in the same proportion as the vapor, so that evaporation does not change the purity, and distillation does not effect separation For example, ethyl alcohol and water form an azeotrope of 95 6 at 78 1 C If the azeotrope is not considered sufficiently pure for use, there exist some techniques to break the azeotrope to give a pure distillate This set of techniques are known as azeotropic distillation Some techniques achieve this by jumping over the azeotropic composition by adding an additional component to create a new azeotrope, or by varying the pressure Others work by chemically or physically removing or sequestering the impurity For example, to purify ethanol beyond 95 , a drying agent or a desiccant such as potassium carbonate can be added to convert the soluble water into insoluble water of crystallization Molecular sieves are often used for this purpose as well Immiscible liquids, such as water and toluene, easily form azeotropes Commonly, these azeotropes are referred to as a low boiling azeotrope because the boiling point of the azeotrope is lower than the boiling point of either pure component The temperature and composition of the azeotrope is easily predicted from the vapor pressure of the pure components, without use of Raoult s law The azeotrope is easily broken in a distillation set-up by using a liquid-liquid separator a decanter to separate the two liquid layers that are condensed overhead Only one of the two liquid layers is refluxed to the distillation setup High boiling azeotropes, such as a 20 weight percent mixture of hydrochloric acid in water, also exist As implied by the name, the boiling point of the azeotrope is greater than the boiling point of either pure component To break azeotropic distillations and cross distillation boundaries, such as in the DeRosier Problem, it is necessary to increase the composition of the light key in the distillate Breaking an azeotrope with unidirectional pressure manipu lation The boiling points of components in an azeotrope overlap to form a band By exposing an azeotrope to a vacuum or positive pressure, it s possible to bias the boiling point of one component away from the other by exploiting the differing vapour pressure curves of each the curves may overlap at the azeotropic point, but are unlikely to be remain identical further along the pressure axis either side of the azeotropic point When the bias is great enough, the two boiling points no longer overlap and so the azeotropic band disappears This method can remove the need to add other chemicals to a distillation, but it has two potential drawbacks Under negative pressure, power for a vacuum source is needed and the reduced boiling points of the distillates requires that the condenser be run cooler to prevent distillate vapours being lost to the vacuum source Increased cooling demands will often require additional energy and possibly new equipment or a change of coolant Alternatively, if posit ive pressures are required, standard glassware can not be used, energy must be used for pressurization and there is a higher chance of side reactions occurring in the distillation, such as decomposition, due to the higher temperatures required to effect boiling A unidirectional distillation will rely on a pressure change in one direction, either positive or negative Pressure-swing distillation Further information Pressure-Swing Distillation section on the main Azeotrope page Pressure-swing distillation is essentially the same as the unidirectional distillation used to break azeotropic mixtures, but here both positive and negative pressures may be employed clarification needed This has an important impact on the selectivity of the distillation and allows a chemist citation needed to optimize a process such that fewer extremes of pressure and temperature are required and less energy is consumed This is particularly important in commercial applications Pressure-swing distillation is emplo yed during the industrial purification of ethyl acetate after its catalytic synthesis from ethanol Industrial distillation Typical industrial distillation towers Main article Continuous distillation Large scale industrial distillation applications include both batch and continuous fractional, vacuum, azeotropic, extractive, and steam distillation The most widely used industrial applications of continuous, steady-state fractional distillation are in petroleum refineries, petrochemical and chemical plants and natural gas processing plants Industrial distillation 27 33 is typically performed in large, vertical cylindrical columns known as distillation towers or distillation columns with diameters ranging from about 65 centimeters to 16 meters and heights ranging from about 6 meters to 90 meters or more When the process feed has a diverse composition, as in distilling crude oil, liquid outlets at intervals up the column allow for the withdrawal of different fractions or products having dif ferent boiling points or boiling ranges The lightest products those with the lowest boiling point exit from the top of the columns and the heaviest products those with the highest boiling point exit from the bottom of the column and are often called the bottoms Diagram of a typical industrial distillation tower Large-scale industrial towers use reflux to achieve a more complete separation of products Reflux refers to the portion of the condensed overhead liquid product from a distillation or fractionation tower that is returned to the upper part of the tower as shown in the schematic diagram of a typical, large-scale industrial distillation tower Inside the tower, the downflowing reflux liquid provides cooling and condensation of the upflowing vapors thereby increasing the efficacy of the distillation tower The more reflux that is provided for a given number of theoretical plates, the better the tower s separation of lower boiling materials from higher boiling materials Alternatively, the more reflux that is provided for a given desired separation, the fewer the number of theoretical plates required Such industrial fractionating towers are also used in air separation, producing liquid oxygen, liquid nitrogen, and high purity argon Distillation of chlorosilanes also enables the production of high-purity silicon for use as a semiconductor Section of an industrial distillation tower showing detail of trays with bubble caps Design and operation of a distillation tower depends on the feed and desired products Given a simple, binary component feed, analytical methods such as the McCabe-Thiele method 27 34 or the Fenske equation 27 can be used For a multi-component feed, simulation models are used both for design and operation Moreover, the efficiencies of the vaporliquid contact devices referred to as plates or trays used in distillation towers are typically lower than that of a theoretical 100 efficient equilibrium stage Hence, a distillation tower needs more trays than the number of theoretical vapor-liquid equilibrium stages In industrial uses, sometimes a packing material is used in the column instead of trays, especially when low pressure drops across the column are required, as when operating under vacuum Large-scale, industrial vacuum distillation column 35 This packing material can either be random dumped packing 1-3 wide such as Raschig rings or structured sheet metal Liquids tend to wet the surface of the packing and the vapors pass across this wetted surface, where mass transfer takes place Unlike conventional tray distillation in which every tray represents a separate point of vapor-liquid equilibrium, the vapor-liquid equilibrium curve in a packed column is continuous However, when modeling packed columns, it is useful to compute a number of theoretical stages to denote the separation efficiency of the packed column with respect to more traditional trays Differently shaped packings have different surface areas and void space between packin gs Both of these factors affect packing performance Another factor in addition to the packing shape and surface area that affects the performance of random or structured packing is the liquid and vapor distribution entering the packed bed The number of theoretical stages required to make a given separation is calculated using a specific vapor to liquid ratio If the liquid and vapor are not evenly distributed across the superficial tower area as it enters the packed bed, the liquid to vapor ratio will not be correct in the packed bed and the required separation will not be achieved The packing will appear to not be working properly The height equivalent of a theoretical plate HETP will be greater than expected The problem is not the packing itself but the mal-distribution of the fluids entering the packed bed Liquid mal-distribution is more frequently the problem than vapor The design of the liquid distributors used to introduce the feed and reflux to a packed bed is critical to making the packing perform to it maximum efficiency Methods of evaluating the effectiveness of a liquid distributor to evenly distribute the liquid entering a packed bed can be found in references 36 37 Considerable work as been done on this topic by Fractionation Research, Inc commonly known as FRI 38 Distillation in food processing Distilled beverages Main article Distilled beverage Carbohydrate-containing plant materials are allowed to ferment, producing a dilute solution of ethanol in the process Spirits such as whiskey and rum are prepared by distilling these dilute solutions of ethanol Components other than ethanol, including water, esters, and other alcohols, are collected in the condensate, which account for the flavor of the beverage Distillation Basic Theory Part 01 Distilasi adalah suatu proses yang melibatkan campuran liquid atau uap yang terdiri dari dua atau lebih komponen dipisahkan menjadi fraksi komponen yang diinginkan, dengan memasukan dan mengeluarkan panas Pemisahan kompo nen dari campuran liquid dengan distilasi tergantung pada titik didih masing-masing komponen Dan juga tergantung pada konsentrasi, karena masing-masing mempunyai karakteristik titik didih Sehingga proses distilasi tergantung pada karakteristik tekanan uap campuran liquid Dalam kolom distilasi akan terdapat transfer panas atau energi yang tentu akan menaikan tekanan uap, di mana tekanan uap berhubungan dengan titik didih Liquid akan mendidih pada saat tekanan uapnya sama dengan lingkungannya Kemudahan liquid untuk mendidih tergantung pada jumlah komponen volatile yang ada pada liquid Liquid dengan tekanan uap tinggi high volatility akan menguap pada temperatur yang lebih rendah Distilasi terjadi karena adanya perbedaan komponen volatility pada campuran liquid Perpindahan massa pada kolom distilasi terjadi pada suatu stage dengan memanfaatkan kesetimbangan fasa uap-cair dari suatu komponen Tekanan uap liquid pada temperatur tertentu terjadi kesetimbangan antara molekul meninggalkan atau masuk permukaan liquid Cairan dan uap yang tidak berada dalam kondisi setimbang akan dikontakkan hingga terjadi perpindahan massa dan produk dalam stage tersebut akan mendekati kondisi kesetimbangan Komponen-komponen volatile diharapkan akan banyak berada pada uap yang meninggalkan stage dibandingkan dengan uap yang memasuki stage, sebaliknya diharapkan cairan yang meninggalkan stage akan memiliki komponenkomponen volatile Bila proses ini dilakukan berulang-ulang diharapkan akan di dapatkan derajat pemisahan yang tinggi Distilasi secara umum dapat dibedakan menjadi 1 Distilasi Atmosferik Dilakukan pada tekanan sedikit diatas tekanan atmosfir Minyak dipanaskan sampai temperatur tertentu sebelum terjadi perengkahan Aplikasi Crude Distillation Unit 2 Distilasi Vakum Untuk minyak berat bertitik didih tinggi yang jika dipanaskan lebih lanjut pada tekanan atmosfir akan terjadi perengkahan Dilakukan pada tekanan dbawah satu atmosfir vakum Aplikasi Vacuum Unit 3 Distilasi Bertekanan Unt uk minyak yang sudah menguap pada temperatur kamar Aplikasi Light End Unit Debutanizer, Depropanizer, naptha splitter Sistem kompleks adalah adalah sistem yang terdiri dari banyak sekali komponen sehingga tidak layak untuk menentukan komposisi campuran tersebut dinyatakan dalam komponenkomponen murninya Contohnya adalah campuran petroleum Pada umumya analisa penentuan titik didih pada campuran petroleum menggunakan dua cara, yaitu distilasi ASTM American Society for Testing and Material dan distilasi TBP True Boiling Point 1 Distilasi TBP Disebut distilasi 15 5, kolom eqivalent dengan 15 tahap plate perbandingan refluks 5 1 Derajat kemurnian relatif tinggi, setiap komponen terpisahkan dengan baik dari komponen ringan sampai dengan komponen berat Kondisi operasi, tekanan atmospferik temperatur sampai dengan 316 oC 600 o F , kemudian dilanjutkan dengan tekanan vacum dengan tujuan mencegah perengkahan fraksi minyak yang berat Volume minyak mentah 1000-5000 cc sehingga volume distilat e setiap fraksi banyak dan cukup untuk analisa kualitas fraksi 2 Distilasi ASTM atau distilasi Engler Derajat kemurnian relatif rendah tidak ada kolom refluks Hasil distilasi ASTM dapat digunakan untuk menganalisa minyak mentah Analisa cepat Banyak digunakan untuk mengontrol operasi Untuk minyak mentah dan produk produk minyak mentah Volume 100 cc Tekanan atmosferik Pemanasan diatur sedemikian rupa pada 5 10 menit diperoleh tetesan pertama, hasil dikumpulkan dengan kecepatan 4 5 cc per menit Temperature uap tetesan pertama disebut IBP Initial Boiling Point Temperature selanjutnya dicatat setelah hasil distillate terkumpul 5 ml, 10 ml dan setiap mendapat 10 ml distilate berikutnya Temperature uap maksimum pada tetesan terakhir disebut End Point Campuran dalam fasa cair yang dipanaskan dalam suatu kolom bejana akan mengalami keseimbangan fase uap dan fase cair yang berlangsung singkat, peristiwa ini disebut Equilibrium Flash Vaporization EFV Kurva Equlibrium Flash Vaporizat ion dibuat berdasarkan data Distilasi TBP atau Distilasi ASTM dengan bantuan grafik Kurva EFV bermanfaat untuk menetukan performance dari unit Flash Distillation pada campuran kompleks Variabel Operasi Variabel-variabel yang mempengaruhi operasi kolom stripper adalah sebagai berikut 1 Temperatur umpan masuk kolom Temperatur umpan mempengaruhi jumlah komponen yang teruapkan pada flash zone, bila temperatur terlalu rendah, maka akan banyak fraksi ringan yang jatuh ke produk bawah dan sebaliknya bila terlalu tinggi fraksi berat akan terikut ke atas 2 Tekanan kolom Tekanan kolom akan berpengaruh terhadap temperatur penguapan cairan, bila tekanan kolom rendah maka temperatur yang dibutuhkan juga rendah 3 Sifat fisik umpan Semakin banyak fraksi berat pada umpan, maka dibutuhkan energi yang lebih besar untuk memisahkannya 4 Refluks Refluks berfungsi untuk menurunkan beban pendinginan pada kondensor, dengan pendinginan ini secara tidak langsung refluks mempengaruhi perolehan produk Bila laju r efluks terlalu tinggi dkhawatirkan fraksi ringan akan terikut pada fraksi di bawahnya dan begitu juga sebaliknya Pengertian Distilasi Distilasi adalah suatu cara pemisahan larutan dengan menggunakan panas sebagai pemisah atau separating agent Jika larutan yang terdiri dari dua buah komponen yang cukup mudah menguap, misalnya larutan benzena-toluena, larutan n-Heptan dan n-Heksan dan larutan lain yang sejenis didihkan, maka fase uap yang terbentuk akan mengandung komponen yang lebih menguap dalam jumlah yang relatif lebih banyak dibandingkan dengan fase cair Jadi ada perbedaan komposisi antara fase cair dan fase uap, dan hal ini merupakan syarat utama supaya pemisahan dengan distilasi dapat dilakukan Kalau komposisi fase uap sama dengan komposisi fase cair, maka pemisahan dengan jalan distilasi tidak dapat dilakukan Proses distilasi dalam kilang minyak bumi merupakan proses pengolahan secara fisika yang primer yang mengawali semua proses-proses yang diperlukan untuk memproduksi BBM dan Non-BBM Proses distilasi ini dapat menggunakan satu kolom atau lebih menara distilasi, misalnya residu dari menara distilasi dialirkan ke menara distilasi hampa atau ke menara distilasi bertekanan Secara fundamental semua proses-proses distilasi dalam kilang minyak bumi adalah sama Semua proses distilasi memerlukan beberapa peralatan yang penting seperti - Kondensor dan Cooler - Menara Fraksionasi - Kolom Stripping Proses pemisahan secara distilasi dengan mudah dapat dilakukan terhadap campuran, dimana antara komponen satu dengan komponen yang lain terdapat dalam campuran a Dalam keadaan standar berupa cairan, saling melarutkan menjadi campuran homogen b Mempunyai sifat penguapan relatif cukup besar c Tidak membentuk cairan azeotrop Pada proses pemisahan secara distilasi, fase uap akan segera terbentuk setelah sejumlah cairan dipanaskan Uap dipertahankan kontak dengan sisa cairannya dalam waktu relatif cukup dengan harapan pada suhu dan tekanan tertentu, antara uap dan sisa cairan aka n berada dalam keseimbangan, sebelum campuran dipisahkan menjadi distilat dan residu Fase uap yang mengandung lebih banyak komponen yang lebih mudah menguap relatif terhadap fase cair, berarti menunjukkan adanya suatu pemisahan Sehingga kalau uap yang terbentuk selanjutnya diembunkan dan dipanaskan secara berulang-ulang, maka akhirnya akan diperoleh komponen-komponen dalam keadaan yang relatif murni Keseimbangan Uap Cair Untuk dapat menyelesaikan soal-soal distilasi harus tersedia data-data keseimbangan uapcair sistim yang dikenakan distilasi Data keseimbangan uap-cair dapat berupa tabel atau diagram Tiga macam diagram keseimbangan yang akan dibicarakan, yaitu Diagram Titik didih Diagram titik didih adalah diagram yang menyatakan hubungn antara temperatur atau titik didih dengan komposisi uap dan cairan yang berkeseimbangan Di dalam diagram titik didih tersebut terdapat dua buah kurva, yaitu kurva cair jenuh dan uap jenuh Kedua kurva ini membagi daerah didalam diagram menjadi 3 bagia n, yaitu 1 Daerah satu fase yaitu daerah cairan yang terletak dibawah kurva cair jenuh 2 Daerah satu fase yaitu daerah yang terletak datas kurva uap jenuh 3 Daerah dua fase yaitu daerah uap jenuh dan cair jenuh yang terletak di antara kurva cair jenuh dan kurva uap jenuh Diagram Keseimbangan uap-cair Diagram keseimbangan uap-cair adalah diagram yang menyatakan hubungan keseimbangan antara komposisi uap dengan komposisi cairan Diagram keseimbangan uapcair dengan mudah dapat digambar, jika tersedia titik didihnya Diagram Entapi-komposisi Diagram entalpi-komposisi adalah diagram yang menyatakan hubungan antara entalpi dengan komposisi sesuatu sistim pada tekanan tertentu Didalam diagram tersebut terdapat dua buah kurva yaitu kurva cair jenuh dan kurva uap jenuh Setiap titik pada kurva cair jenuh dihubungkan dengan gari hubung tie line dengan titik tertentu pada kurva uap jenuh, dimana titik-titik tersebut dalam keadaan keseimbangan Dengan adanya kedua kurva tersebut, daerah didalam diag ram terbagi menjadi 3 daerah, yaitu 1 Daerah cairan yang terletak dibawah kurva cair jenuh 2 Daerah uap yang terletak diatas kurva uap jenuh 3 Daerah cair dan uap yang terletak diantara kurva cair jenuh dengan kurva uap jenuh Dibawah kurva cair jenuh terdapat isoterm-isoterm yang menunjukkan entalpi cairan pada berbagai macam komposisi pada berbagai temperatur 2 2 Macam-macam Distilasi Distilasi berdasarkan prosesnya terbagi menjadi dua, yaitu 1 Distilasi kontinyu 2 Distilasi batch Berdasarkan basis tekanan operasinya terbagi menajdi tiga, yaitu 1 Distilasi atmosferis 0,4-5,5 atm mutlak 2 Distilasi vakum 300 mmHg pada bagian atas kolom 3 Distilasi tekanan 80 psia pada bagian atas kolom Berdasarkan komponen penyusunnya 1 Distilasi sistem biner 2 Distilasi sitem multi komponen Berdasarkan sistem operasinya terbagi dua, yaitu 1 Single-stage Distillation 2 Multi stage Distillation Distilasi Vakum Distilasi vakum adalah distilasi yang tekanan operasinya 0,4 atm 300 mmHg absolut Distilasi yang dilakukan dalam tekanan operasi ini biasanya karena beberapa alasan yaitu a Sifat penguapan relatif antar komponen biasanya meningkat seiring dengan menurunnya boiling temperature Sifat penguapan relatif yang meningkat memudahkan terjadinya proses separasi sehingga jumlah stage teoritis yang dibutuhkan berkurang Jika jumlah stage teoritis konstan, rasio refluks yang diperlukan untuk proses separasi yang sama dapat dikurangi Jika kedua variabel di atas konstan maka kemurnian produk yang dihasilkan akan meningkat b Distilasi pada temperatur rendah dilakukan ketika mengolah produk yang sensitif terhadap variabel temperatur Temperatur bagian bawah yang rendah menghasilkan beberapa reaksi yang tidak diinginkan seperti dekomposisi produk, polimerisasi, dan penghilangan warna c Proses pemisahan dapat dilakukan terhadap komponen dengan tekanan uap yang sangat rendah atau komponen dengan ikatan yang dapat terputus pada titik didihnya d Reboiler dengan temperatur yang rendah yang menggunak an sumber energi dengan harga yang lebih murah seperti steam dengan tekanan rendah atau air panas Distilasi Multikomponen Perhitungan distilasi multikomponen lebih rumit dibandingkan dengan perhitungan distilasi biner karena tidak adapat digunakan secara grafis Dasar perhitungannya adalah penyelesaian persamaan-persamaan neraca massa, neraca energi dan kesetimbangan secara simultan Bila distilasi melibatkan C komponen dengan N buah tahap kesetimbangan maka jumlah persamaan yang terlibat dalam perhitungan adalah N C persamaan neraca massa, N C relasi kesetimbangan dan N persamaan neraca energi Perhitungan distilasi multikomponen dilakukan dengan 2 tahap 1 Perhitungan awal, dilakukan dengan metode pintas Shortcut Calculation Perhitungan awal digunakan untuk analisis kualitatif dari suatu kolom distilasi atau perhitungan awal rancangan dengan tujuan 1 Memperkirakan komposisi produk atas dan bawah Tekanan sistem Jumlah tahap kesetimbangan Lokasi umpan masuk 2 Perhitungan tahap demi tahap dilakukan dengan metode eksak yang merupakan penyelesaian banyak persamaan aljabar Metode sederhana dengan kalkulator Metode MESH dengan program komputer Single-stage Distillation Single-stage Distillation biasa juga disebut dengan flash vaporization atau equilibrium distillation, dimana campuran cairan diuapkan secara parsial Pada keadaan setimbang, uap yang dihasilkan bercampur dengan cairan yang tersisa, namun pada akhirnya uap tersebut akan dipisahkan dari kolom seperti juga fase cair yang tersisa Distilasi jenis ini dapat dilakukan dalam kondisi batch maupun kontinyu 2 3 Tray Tower Tray tower merupakan bejana vertikal dimana cairan dan gas dikontakkan melalui plateplate yang disebut sebagai tray Fungsi dari penggunaan tray adalah untuk memperbesar kontak antara cairan dan gas sehingga komponen dapat dipisahkan sesuai dengan rapat jenisnya, dalam bentuk gas atau cairan Jumlah tahapan atau tray dalam suatu kolom tergantung pada tingginya kesulitan pemisahan zat yang akan dilakukan dan juga ditentukan berdasarkan perhitungan neraca massa dan kesetimbangan Efisiensi tray dan jumlah tray yang sebenarnya ditentukan oleh desain yang digunakan dan kondisi operasi, sedangkan diameter kolom bergantung pada jumlah gas dan cairan yang melewati kolom per unit waktu Untuk mendapatkan produk yang baik diperlukan alat kontak antara uap dengan cairan Beberapa jenis alat kontak antara uap dengan cairan adalah bubble cap tray, grid tray, sieve tray dan valve tray Sieve Tray Sieve tray merupakan jenis tray yang paling sederhana dibandingkan jenis tray yang lain dan lebih murah daripada jenis bubble cap Pada Sieve tray uap naik ke atas melalui lubang-lubang pada plate dan terdispersi dalam cairan sepanjang plate Cairan mengalir turun ke plate di bawahnya melalui down comer dan weir Meskipun sive tray mempunyai kapasitas yang lebih besar pada kondisi operasi yang sama dibandingkan dengan bubble cap, namun sieve tray mempunyai satu kekurangan yang cukup serius pada kecepatan uap yan g relatif lebih rendah dibandingkan pada kondisi operasi normal Pada sieve tray, aliran uap berfungsi mencegah cairan mengalir bebas ke bawah melalui lubang-lubang, tiap plate di desain mempunyai kecepatan uap minimum yang mencegah terjadinya peristiwa dumps atau shower yaitu suatu peristiwa dimana cairan mengalir bebas mengalir ke bawah melalui lubang-lubang pada plate Kecepatan uap minimum ini yang harus amat sangat diperhatikan dalam mendesain sieve tray dan menjadi kesulitan tersendiri dalam kondisi operasi sieve tray sama besarnya dengan bubble cap pada kondisi desain yang sama, namun menurun jika kapasitasnya berkurang di bawah 60 dari desain Sectional construction Seksi plate dipasang pada cincin yang dilas di sekeliling dinding kolom bagian dalam dan pada balok-balok penyangga Lebar balok penyangga dan cincin sekitar 50 mm, dengan jarak antar satu balok dengan yang lainnya sekitar 0 6 m Balok penyangga dipasang horizontal sebagai penyangga plate, biasanya di bentuk dari lembara n yang dilipat atau dibentuk Satu bagian dari plate di desain bisa di pindahkan yang berfungsi sebagai manway Hal ini bertujuan untuk mengurangi jumlah manway yang dapat mengurangi biaya konstruksi Downcomers Downcomer terdapat pada semua equilibrium-stage trays, bertujuan sebagai media cairan untuk mengalir dari tray atas ke tray di bawahnya Downcomer di desain untuk menyediakan kapasitas penanganan cairan yang cukup untuk kolom distilasi dan pada waktu yang sama untuk memenuhi luas minimum dari area cross-sectional, sehingga area aktif dari pada tray akan maksimum Jenis-jenis downcomer dapat dilihat pada gambar di bawah jenis yang paling sederhana dan murah dalam konstruksi dan paling memuaskan untuk berbagai macam tujuan Channel downcomer dibentuk dari plat rata yang kemudian disebut apron yang dipasang dengan posisi ke bawah dari outlet weir Apron biasanya vertikal, namun bisa juga agak miring untuk meningkatkan area plate untuk perforation Flooding Flooding terjadi jika busa pada plate berakumulasi melebihi penyangga downcomer Downcomer kemudian mengandung campuran yang mempunyai densitas yang lebih rendah dari cairan murni, kapasitasnya berkurang, level cairan meningkat pada downcomer sampai akhirnya mencapai tray di atasnya dan selanjutnya akan mencapai keadaan dimana cairan memenuhi kolom Weep Point Weep point bisa diartikan sebagai kecepatan minimum uap yang dapat memberikan kestabilan kondisi operasi Tray spacing Tray spacing merupakan jarak antara satu tray dengan tray yang lainnya Biasanya sekitar 6 inci lebih pendek dari bubble cap tray Sieve tray beroperasi pada spacing sekitar 9 inci sampai 3 inci Yang biasa digunakan adalah sekitar 12-16 inci Hole Size, arrangement and Spacing Diameter lubang dan pengaturannya bervariasi tergantung kebutuhan dan keinginan dari yang mendesain Yang biasa dipakai untuk kegiatan komersil yaitu diameter dan 1 inci Diameter lubang direkomendasikan untuk self cleaning yaitu 3 16 inci Diameter inci bisa digunakan untuk ber bagai macam kebutuhan termasuk yang melibatkan fouling dan cairan yang mengandung solid tanpa kehilangan efisiensi Diameter 1 8 inci sering digunakan untuk kondisi vakum Pengaturan posisi lubang atau arrangement bisa berupa triangular pitch segitiga atau square pitch segiempat , lebih jelasnya bisa dilihat pada gambar di bawah jarak antar lubang dua kali diameter maka cenderung akan mengalami unstable operation Jarak lubang yang direkomendasikan adalah 2 5 do sampai 5 do, dan yang paling direkomendasikan 3 8 do Active Hole Area Ialah luasan total pada plate termasuk di dalamnya ialah perforated area dan calming zone Perforated Area Perforated area atau hole area ialah area pada plate dimana masih terdapat lubang-lubang tempat kontaknya cairan dan uap Calming Zone Ialah area pada plate yang tidak terdapat lubang-lubang Height of Liquid Over Outlet Weir, how Batas minimum tinggi weir adalah 0 5 inci, dengan 1-3 inci yang paling direkomendasikan Untuk lebih jelasnya biasa dilihat pada gam bar di bawah ini Untuk menentukan jumlah tahap yang dibutuhkan pada distilasi multi komponene diperlukan dua kunci, yaitu Light Key Component LK dan Heavy Key Component HK komponen Light Key Component adalah komponen fraksi ringan pada produk bawah dalam jumlah kecil tapi tidak dapat diabaikan Heavy Key Component adalah komponen fraksi berat pada produk atas dalam jumlah kecil yang tidak dapat diabaikan LK dan HK diperlukan untuk mengetahui distribusi komponen lain Jumlah tahap yang diperlukan untuk pemisahan juga tergantung pada rasio refluks perbandingan refluks yang digunakan R Dengan menaikkan reflux akan menurunkan jumlah tahap yang dibutuhkan dan menurunkan capital cost tetapi hal ini akan menaikkan kebutuhan steam serta operating cost Sehingga diperlukan nilai rasio optimum yang memberikan biaya operasi yang rendah Untuk mendapatkan beberapa sistem nilai rasio optimum antara 1,2 sampai 1,5 kali refluks minimum Efisiensi Tray Efisiensi tray adalah pendekatan fraksional terhadap k ondisi kesetimbangan yang dihasilkan oleh tray aktual Untuk itu dibutuhkan pengukuran terhadap kesetimbangan seluruh uap dan cairan yang berasal dari tray, namun karena kondisi dari beberapa lokasi pada tray berbeda antara tray sartu dengan yang lain, digunakan pendekatan titik efisiensi akibat perpindahan massa tray Untuk menghitung efisiensi dari pemisahan umpan menjadi produk atas dan produk bawah digunakan tahapan-tahapan sebagai berikut 1 Menentukan jumlah plate minimum dengan metode Fenske 2 Menetukan jumlah refluk minimum dengan metode Underwood 3 Menentukan jumlah plate teoritis dengan metode a Grafik Gilliland gambar menara destilasi.
Cara Cepat Pembagian binaariset asetukset. Vuonna 1998 perustettu Edotek toimii asiakkaille aina pieniltä aloitusyrityksiltä suurille organisaatioille, kuten Ison-Britannian puolustusministeriölle ja Euroopan avaruusjärjestölle. Joten kuinka paljon tiedät tai et tiedä Kemia ja materiaalit, jos tarvitset apua, soita meille Cara Cepat Pembagian binaariset vaihtoehdot Tässä suhteessa hän hylkää käsitteen binaarisen vastustuksen, jonka mukaan naiset ja perubahan ovat kypsiä, Naisten ja naispuolisten naispuolisten naispuolisten naispuolisten naispuolisten naispuolisten naispuolisten naispuolisten naispuolisten naispuolisten naispuolisten naispuolisten naispuolisten naispuolisten naispuolisten naispuolisten naispuolisten naispuolisten naispuolisten naispotilaiden kanssa. Kemikaalit, metallit Voimme toimia sinä puhtaasti konsulttien roolissa, jotka tarjoavat teknisiä tietoja tai tulevat Mukana käsissä testityötä ongelman ratkaisemiseksi Cara Cepat Pembagian binaariset vaihtoehdot Dengan Amazi...
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