ERT 313 BIOSEPARATION ENGINEERING DISTILLATION Prepared by: Miss Hairul Nazirah Abdul Halim

Topic Outline 1.0Vapor-Liquid Equilibrium Relations 2.0Distillation: Introduction & Applications 3.0Types of Distillation

1.0Vapor – Liquid Equilibrium (VLE) Relations Raoult’s Law Raoult’s Law for V-L phase in equilibrium is defined as: p A = P A x A Where: p A is the partial pressure of component A in the vapor in Pa (atm) P A is the vapor pressure of pure A in Pa (atm) x A is the mol fraction of A in the liquid This law holds only for ideal solutions such as benzene-toluene, hexane-heptane and methanol-ethanol, which are usually substances very similar to each other.

Boiling-Point Diagrams and x-y Plots Often the VLE relations for a binary mixture of A and B are given as a boiling-point diagram Figure shown the benzene (A) – toluene (B) system at total pressure of kPa.

Example: Use of Raoult’s law for Boiling Point Diagram Calculate the vapor and liquid composition in equilibrium at 95 o C for benzene-toluene using the vapor pressure in Table at kPa.

2.0Distillation: Introduction & Applications The function of Distillation is to separate, by vaporization, a liquid mixture of miscible and volatile substances into individual/group components. Examples: a)The separation of a mixture of alcohol and water into its component b)The separation of crude petroleum into gasoline, kerosene and fuel oil

3.0Types of Distillation 2 types of operations: a)Batch distillation b)Continuous distillation 2 types of continuous distillation process: a)Flash distillation (without reflux) b)Rectification distillation (with reflux)

3.1Batch Distillation It is a simple distillation where the liquid is charged to a reboiler (still), is boiled slowly and the vapors are taken directly from the condenser. Batch Distillation is used in some small plant to recover volatile products from liquid solution

Batch Distillation with Reflux Batch distillation with a simple still does not give a good separation unless the relative volatility is high. Reflux is used to improve the performance of the batch still

3.2Continuous Operation: Flash Distillation Figure 21.1 shows the elements of a flash distillation plant.

3.3Continuous operation: Rectification Distillation 3.3.1Types of Plate Columns 3.3.2Action on an ideal plate 3.3.3Combination rectification and stripping 3.3.4Material balances in Plate Column 3.3.5Number of Ideal Plates (McCabe-Thiele Method) & Feed Plate Location 3.3.6Total & Minimum Reflux Ratio

3.3.1Types of Plate Columns 3 main types: –Sieve Plate Column –Bubble-cap Plate Column –Valve Tray Column Usually used in petroleum industry and chemical plant Tower diameter: 0.3 – 9 meter Number of plates from a few to about a hundred Plate spacing may vary from 150 mm to 2 m

Sieve Plate Column Sieve plate is designed to bring a rising stream of vapor into intimate contact with a descending stream of liquid

The liquid flows across the plate and passes over a weir to a downcomer The flow pattern on each plate is crossflow. The flow pattern in the column is countercurrent flow of liquid and vapor. The downcomers are the segment-shaped region between the curved wall of the column and the straight chord weir. Each downcomer usually occupies 10 – 15% of the column cross section, leaving 70 – 80% of the column area for bubbling and contacting. The vapor pass through the perforated region of the plate (occupies most of the space between downcomers)

Bubble Cap Plate

Valve-Tray

3.3.2Action on an Ideal Plate y n = concentration of vapor leaving plate x n = concentration of liquid leaving plate y n+1 = concentration of vapor entering plate x n+1 = concentration of liquid entering plate On an ideal plate, the vapor and liquid leaving the plate are brought into equilibrium. Consider plate n in the figure.

3.3.3 Combination rectification and stripping

3.3.4Material Balances in Plate Columns

Overall Material Balances for two-component systems Total material balance: Material balance on component A Eliminating B from these equations gives Eliminating D gives

Net Flow Rates Net Flow Rates in the Upper Section of the Column Material balance around the condenser and accumulator: Material balance for component A: A total material balance around the control surface I:

Net Flow Rates in the Lower Section of the Column

Operating Lines There are 2 operating lines: for rectification and stripping section. Rectification Section General operating line equation: Substitute: Dx D = V a y a – L a x a (21.12) Eliminate V n+1 from Eq by Eq , gives:

Stripping Section Material balance over control surface II Operating line for stripping section: Eliminate V m+1 from Eq by Eq , gives:

Reflux Ratio Reflux is the returning of a portion of the condensate to the reboiler. 2 quantities of reflux ratio: a) ratio of the reflux to the overhead product b) ratio of the reflux to the vapor *In this text R D will be used. R D, the reflux ratio, is an operating variable that can be controlled by adjusting the split between reflux and overhead product.

For constant molal overflow (divide Eq by D): Eq is the operating line of the rectifying section.

Condition of Feed The conditions of the vapor rate or the liquid rate may change depending of the thermal condition of the feed. Various types of feed conditions: 1.Cold feed : It is assumed that the entire feed stream adds to the liquid flowing down the column. 2.Feed at bubble point: no condensation is required to heat the feed. 3.Feed partial vapor: the liquid portion of the feed becomes part of the L and the vapor portion becomes part of V 4.Feed saturated vapor the entire feed becomes part of the V 5.Feed superheated: part of the liquid from the rectifying column is vaporized to cool the feed to a state of saturated vapor.

Feed types can be characterized by the use of a single factor, q q is the moles of liquid flow in the stripping section Various types of feed conditions: 1.Cold feed, q > 1 2.Feed at bubble point (saturated liquid), q = 1 3.Feed partially vapor, 0 < q < 1 4.Feed at dew point (saturated vapor), q = 0 5.Feed superheated vapor q < 0

Feed line Equation If x q = x F, and y q =x F then; The point of intersection of the two operating lines lies on the straight line of slope (q/q -1) and intercept (x F, y F ) Where the value of q for cold-liquid feed is: Feed Line

Where the value of q for superheated vapor feed is:

Effect the feed condition on feed line –If the feed is a cold liquid, the feed line slopes will be upward and to the right; –if the feed is a saturated liquid, the line is vertical; –if the feed is a mixture of liquid and vapor, the lines slopes upward and to the left and the slope is the negative of the ratio of the liquid to the vapor; –if the feed is saturated vapor the line is horizontal and –if the feed is superheated vapor. The lines slope downward and to the left.

Construction of Operating Lines Construction the operating lines: 1.Locate the feed line 2.Calculate the y-axis intercept x D /(R D + 1) of the rectifying line and plot that line through the intercept and the point (x D, x D ) 3.Draw the stripping line through point (x B,x B ) and the intersection of the rectifying line with the feed line.

3.3.5Number of Ideal Plates & Feed Plate Location Number of Ideal Plates After the operating lines have been plotted, the construction of the number of ideal trays is found by the usual step-by-step construction. The process can begin at the top of the rectifying line or at the bottom of stripping line Feed Plate location The feed plate is the intersection of operating lines.

Heating & Cooling Requirement If saturated steam is used as the heating medium, the steam required at the reboiler is:

If water is used as the cooling medium in the condenser and the condensate is not subcooled, the cooling water requirement is:

3.3.6Total & Minimum Reflux Ratio Total Reflux The slope of rectifying line increase with R D When R D is infinite, V = L, the slope is 1 (this condition is called total reflux) The operating line for rectification = operating line for stripping = 45 o line At total reflux the no. of plates required is minimum but the tower diameter is infinite The rate of feed, overhead and bottom products are zero. Since there is no feed in a column operating under total reflux, there is no discontinuity between the upper and lower sections.

Minimum Reflux The number of plates becomes very large as the R D becomes smaller. At definite minimum (minimum reflux ratio, R m ) the number of plates becomes infinite. This corresponds to the minimum vapor flow in the tower, and hence minimum reboiler and condenser sizes. The slope of rectifying line decrease with R D The slope closer to the equilibrium line. When both of operating lines touch the equilibrium line, a ‘pinch point’ occurs where the no. of steps required becomes infinite. The slope of rectification operating line is as follows:

Multicomponent Distillation Separation of more than two components The general principles of design for multicomponent distillation towers are the same as described for binary system. The calculation of equilibrium stages uses mass and enthalpy balances and VLE. In binary distillation, one tower is used to separate the two components A and B. In multicomponent mixture of n components, n – 1 fractionators will be required for separation. For example, for 3 components mixture of A, B and C where A is the most volatile and C is least volatile, two column will be needed as shown in Figure