SEQUENCING OF SEPARATION TRAINS LECTURE FOUR SEQUENCING OF SEPARATION TRAINS Ref: Seider, Seader and Lewin (2004), Chapter 7 4 - Separation Trains

Introduction Almost all chemical processes require the separation of chemical species (components), to: purify a reactor feed recover unreacted species for recycle to a reactor separate and purify the products from a reactor Frequently, the major investment and operating costs of a process will be those costs associated with the separation equipment For a binary mixture, it may be possible to select a separation method that can accomplish the separation task in just one piece of equipment. However, more commonly, the feed mixture involves more than two components, involving more complex separation systems 4 - Separation Trains

Instructional Objectives When you have finished studying this unit, you should: Be familiar with the more widely used industrial separation methods and their basis for separation. Understand the concept of the separation factor and be able to select appropriate separation methods for vapor and liquid mixtures. Understand how distillation columns are sequenced and how to apply heuristics to narrow the search for a near-optimal sequence. Be able to apply algorithmic methods to determine an optimal sequence of distillation-type separations. 4 - Separation Trains

Example 1. Specification for Butenes Recovery 4 - Separation Trains

Design for Butenes Recovery System Propane and 1-Butene recovery 100-tray column C3 & 1-Butene in distillate n-C4 and 2-C4=s cannot be separated by ordinary distillation (=1.03), so 96% furfural is added as an extractive agent (  1.17). n-C4 withdrawn as distillate. Pentane withdrawn as bottoms 2-C4=s withdrawn as distillate. Furfural is recovered as bottoms and recycled to C-4 4 - Separation Trains

Separation is Energy Intensive Unlike the spontaneous mixing of chemical species, the separation of a mixture of chemicals requires an expenditure of some form of energy Separation of a feed mixture into streams of differing chemical composition is achieved by forcing the different species into different spatial locations, by one or a combination of four common industrial techniques: the creation by heat transfer, shaft work, or pressure reduction of a second phase that is immiscible with the feed phase (ESA – energy separating agent) the introduction into the system of a second fluid phase (MSA – mass separating agent). This must be subsequently removed. the addition of a solid phase upon which adsorption can occur (MSA) the placement of a membrane barrier (ESA) 4 - Separation Trains

Common Industrial Separation Methods Phase of the feed Separating agent(s) Developed or added phase Separation principle Flash L and/or V Pressure reduction or heat transfer V or L difference in volatility Distillation (ordinary) Heat transfer or shaft work Gas absorption V Liquid absorbent L Stripping Vapor stripping agent Extractive distillation Liquid solvent and heat transfer V and L Azeotropic distillation Liquid entrainer and heat transfer 4 - Separation Trains

Common Industrial Sep.Methods (Cont’d) Separation Method Phase of the feed Separation agent Developed or added phase Separation principle Liquid-liquid extraction L Liquid solvent Second liquid Difference in solubility Crystalli-zation Heat transfer Solid Difference in solubility or m.p. Gas adsorption V Solid adsorbent difference in adsorbabililty Liquid adsorption Membrane L or V difference in permeability and/or solubility 4 - Separation Trains

Common Industrial Sep.Methods (Cont’d) Separation Method Phase of the feed Separation agent Developed or added phase Separation principle Supercritical extraction L or V Supercritical solvent Supercritical fluid Difference in solubility Leaching S Liquid solvent L Drying S and L Heat transfer V Difference in volatility Desublimation 4 - Separation Trains

Selecting Separation Method (1) The development of a separation process requires the selection of: Separation methods ESAs and/or MSAs Separation equipment Optimal arrangement or sequencing of the equipment Optimal operating temperature and pressure for the equipment Selection of separation method depends on feed condition : Vapor: partial condensation, cryogenic distillation , absorption, adsorption, gas permeation (membranes), desublimation Liquid: partial vaporization, distillation, stripping, extractive distillation, azeo-distillation, LL extraction, crystallization , adsorption, membrane separation (dialysis, reverse osmosis, ultrafiltration and pervaporation), supercritical extraction Solid: if slurry filtration, if wet  drying, if dry leaching 4 - Separation Trains

Selecting Separation Method (2) The separation factor, SF, defines the degree of separation achievable between two key components of he feed. This factor, for the separation of component 1 from component 2 between phases I and II, for a single stage of contacting, is defined as: (7.1) C = composition variable, I, II = phases rich in components 1 and 2. SF is generally limited by thermodynamic equilibrium. For example, in the case of distillation, using mole fractions as the composition variable and letting phase I be the vapor and phase II be the liquid, the limiting value of SF is given in terms of vapor-liquid equilibrium ratios (K-values) as: (7.2,3) 4 - Separation Trains

Selecting Separation Method (3) For vapor-liquid separation operations that use an MSA that causes the formation of a non-ideal liquid solution (e.g. extractive distillation): (7.5) If the MSA is used to create two liquid phases, such as in liquid-liquid extraction, the SF is referred to as the relative selectivity, b , where: (7.6) In general, MSAs for extractive distillation and liquid-liquid extraction are selected according to their ease of recovery for recycle and to achieve relatively large values of SF. 4 - Separation Trains

Relative volatilities for equal cost separators Ref: Souders (1964) 4 - Separation Trains

Sequencing of Ordinary Distillation Columns Use a sequence of ordinary distillation (OD) columns to separate a multicomponent mixture provided:  in each column is > 1.05. The reboiler duty is not excessive. The tower pressure does not cause the mixture to approach the TC of the mixture. Column pressure drop is tolerable, particularly if operation is under vacuum. The overhead vapor can be at least partially condensed at the column pressure to provide reflux without excessive refrigeration requirements. The bottoms temperature for the tower pressure is not so high that chemical decomposition occurs. Azeotropes do not prevent the desired separation. 4 - Separation Trains

Algorithm to Select Pressure and Condenser Type 4 - Separation Trains

Number of Sequences for Ordinary Distillation Equation for number of different sequences of P  1 ordinary distillation (OD) columns, NS, to produce P products: (7.9)  P # of Separators  Ns 2 1 3 4 5 14 6 42 7 132 8 429 4 - Separation Trains

Example 2 – Sequences for 4-component separation 4 - Separation Trains

Example 2 – Sequences for 4-component separation 4 - Separation Trains

Identifying the Best Sequences using Heuristics The following guidelines are often used to reduce the number of OD sequences that need to be studied in detail: Remove thermally unstable, corrosive, or chemically reactive components early in the sequence. Remove final products one-by-one as distillates (the direct sequence). Sequence separation points to remove, early in the sequence, those components of greatest molar percentage in the feed. Sequence separation points in the order of decreasing relative volatility so that the most difficult splits are made in the absence of other components. Sequence separation points to leave last those separations that give the highest purity products. Sequence separation points that favor near equimolar amounts of distillate and bottoms in each column. 4 - Separation Trains

Class Exercise Design a sequence of ordinary distillation columns to meet the given specifications. 4 - Separation Trains

Class Exercise – Possible Solution Guided by Heuristic 4, the first column in position to separate the key components with the greatest SF. 4 - Separation Trains

Complex Columns for Ternary Mixtures In some cases, complex rather than simple distillation columns should be considered when developing a separation sequence. Ref: Tedder and Rudd (1978) 4 - Separation Trains

Regions of Optimality ESI  1.6 ESI  1.6 LECTURE FOUR Regions of Optimality As shown below, optimal regions for the various configurations depend on the feed composition and the ease-of-separation index: ESI = AB/ BC ESI  1.6 ESI  1.6 4 - Separation Trains

Sequencing of V-L Separation Systems When simple distillation is not practical for all separators in a multicomponent mixture separation system, other types of separators must be employed and the order of volatility or other separation index may be different for each type. (7.10) If they are all two-product separators and if T equals the number of different types, then the number of possible sequences is now given by: For example, if P = 3, and ordinary distillation, extractive distillation with either solvent I or solvent II, and LL extraction with solvent III are to be considered, then T = 4, and applying Eqns (7.9) and (7.10) gives 32 possible sequences (for ordinary distillation alone, NS = 2). 4 - Separation Trains

Example 3 (Example 1 Revisited) Species b.pt.(C) Tc (C) Pc, (MPa) Propane A -42.1 97.7 4.17 1-Butene B -6.3 146.4 3.94 n-Butane C -0.5 152.0 3.73 trans-2-Butene D 0.9 155.4 4.12 cis-2-Butene E 3.7 161.4 4.02 n-Pentane F 36.1 196.3 3.31 For T = 2 (OD and ED), and P = 4, NS = 40. However, since 1-Butene must also be separated (why?), P = 5, and NS = 224. Clearly, it would be helpful to reduce the number of sequences that need to be analyzed. Need to eliminate infeasible separations, and enforce OD for separations with acceptable volatilities. 4 - Separation Trains

Example 3 (Example 1 Revisited) Adjacent Binary Pair ij at 65.5 oC Propane/1-Butene (A/B) 2.45 1-Butene/n-Butane (B/C) 1.18 n-Butane/trans-2-Butene (C/D) 1.03 cis-2-Butene/n-Pentane (E/F) 2.50 Splits A/B and E/F should be by OD only (  2.5) Split C/D is infeasible by OD ( = 1.03). Split B/C is feasible, but an alternative method may be more attractive. Use of 96% furfural as a solvent for ED increases volatilities of paraffins to olefins, causing a reversal in volatility between 1-Butene and n-Butane, altering separation order to ACBDEF, and giving C/B = 1.17. Also, split (C/D)II with  = 1.7, should be used instead of OD. Thus, splits to be considered, with all others forbidden, are: (A/B…)I, (…E/F)I, (…B/C…)I, (A/C…)I , (…C/B…)II, and (…C/D…)II 4 - Separation Trains

Estimating Annualized Cost, CA For each separation, CA is estimated assuming 99 mol % recovery of light key and heavy key in distillate and bottom, respectively. The following steps are followed: Set distillate and bottoms column pressures using Estimate number of stages, feed stage and initial guess of reflux ratio (R = 1.2 Rmin) by using a short-cut distillation method (e.g., DSTWU in Aspen plus). Select tray spacing (typically 2 ft.) and calculate column height, H (assume an overall efficiency equal to 75%). Estimate reboiler duty, condenser duty and column diameter by a rigorous distillation method (e.g., RadFrac in Aspen plus) Estimate installed cost of tower (see Chapter 16). Size and cost ancillary equipment (condenser, reboiler, reflux drum). Sum total capital investment, CTCI. Compute annual cost of heating and cooling utilities (CCOS). Compute CA assuming ROI (typically r = 0.33). CA = CCOS + r CTCI 4 - Separation Trains

(A/B…)I, (…E/F)I, (…B/C…)I, (A/C…)I , (…C/B…)II, and (…C/D…)II 1st Branch of Sequences Sequence Cost, $/yr 1-5-16-28 900,200 1-5-17-29 872,400 1-6-18 1,127,400 1-7-19-30 878,000 1-7-20 1,095,600 Species Propane A 1-Butene B n-Butane C trans-2-Butene D cis-2-Butene E n-Pentane F 4 - Separation Trains

(A/B…)I, (…E/F)I, (…B/C…)I, (A/C…)I , (…C/B…)II, and (…C/D…)II 2nd Branch of Sequences Sequence Cost, $/yr 2-(8,9-21) 888,200 2-(8,10-22) 860,400 Species Propane A 1-Butene B n-Butane C trans-2-Butene D cis-2-Butene E n-Pentane F 4 - Separation Trains

(A/B…)I, (…E/F)I, (…B/C…)I, (A/C…)I , (…C/B…)II, and (…C/D…)II 3rd Branch of Sequences Sequence Cost, $/yr 3-11-23-31 878,200 3-11-24 1,095,700 3-12-(25,26) 867,400 3-13-27 1,080,100 Species Propane A 1-Butene B n-Butane C trans-2-Butene D cis-2-Butene E n-Pentane F 4 - Separation Trains

(A/B…)I, (…E/F)I, (…B/C…)I, (A/C…)I , (…C/B…)II, and (…C/D…)II 4th Branch of Sequences Sequence Cost, $/yr 4-14-15 1,115,200 Species Propane A 1-Butene B n-Butane C trans-2-Butene D cis-2-Butene E n-Pentane F 4 - Separation Trains

Lowest Cost Sequence Sequence Cost, $/yr 2-(8,10-22) 860,400 4 - Separation Trains

Marginal Vapor Rate Method When the number of products is more than four, using the annualized cost method is very difficult and time- consuming. One of the less rigorous method for OD that can produce good results is Marginal Vapor Rate (MV) that proposed by Modi and Westerberg (1992). The difference in costs between the separation in the absence of nonkey components and the separation in the presence of nonkey components, defined as Marginal Annualized Cost (MAC). A good approximation of MAC is the MV, which is the corresponding difference in molar vapor rate passing up the column. The sequence with the minimum sum of column MVs is selected. Vapor rate is a good measure of cost because it is a major factor in determining column diameter, reboiler and condenser areas, and reboiler and condenser duties. 4 - Separation Trains

Estimating Marginal Vapor Rate, MV For each separation, MV is estimated assuming feed at bubble point and 99.9 mol % recovery of light key and heavy key in distillate and bottom, respectively. The following steps are followed: Set distillate and bottoms column pressures using Estimate distillate rate (D), by using a short-cut distillation method (e.g., DSTWU in Aspen plus with R=1.2 Rmin). Calculate the up column vapor rate as V=D(R+1). Calculate the MV (The difference in vapor rate between the separation in the absence of nonkey components and the separation in the presence of nonkey components) 4 - Separation Trains

Example 4 Use the marginal vapor rate (MV) method to determine a sequence for the hydrocarbon specified in the figure, except: Ignore the given temperature and pressure of the feed Assume a recovery of 99.9% in each column 4 - Separation Trains

A=isobutane, B= n-butane, C=isopentane, D= n-pentane Example 4 A=isobutane, B= n-butane, C=isopentane, D= n-pentane 4 - Separation Trains

Separation Trains - Summary On completing this unit, you should: Be familiar with the more widely used industrial separation methods and their basis for separation. Understand the concept of the separation factor and be able to select appropriate separation methods for liquid mixtures. Understand how distillation columns are sequenced and how to apply heuristics to narrow the search for a near-optimal sequence. Be able to apply algorithmic methods to determine an optimal sequence of distillation-type separations. Next week: Azeotropic Distillation 4 - Separation Trains