Liquid-Liquid Extraction

Name: Liquid-Liquid Extraction
Uploaded: 2017-06-29T23:32:30+00:00
Duration: PTM55S32
Channel: Caitlin Joseph
Description: Liquid-Liquid Extraction

Liquid-Liquid Extraction

Hierarchy of Separation Technologies
Physical Separations Decantation, Coalescing, Filtration, Demisting Evaporation Single Effect, Multiple Effect Distillation Simple, Azeotropic, Extractive, Reactive Extraction Simple, Fractional, Reactive Adsorption Pressure Swing, Temperature Swing Crystallization Melt, Solvent Membranes MF, UF, NF, RO Easy Difficult Difficulty Of Separation

Typical Applications Remove products and pollutants from dilute aqueous streams Wash polar compounds or acids/bases from organic streams Heat sensitive products Non-volatile materials Azeotropic and close boiling mixtures Alternative to high cost distillations

Extraction is Used in a Wide Variety of Industries
Chemical Washing of acids/bases, polar compounds from organics Pharmaceuticals Recovery of active materials from fermentation broths Purification of vitamin products Effluent Treatment Recovery of phenol, DMF, DMAC Recovery of acetic acid from dilute solutions Polymer Processing Recovery of caprolactam for nylon manufacture Separation of catalyst from reaction products Petroleum Lube oil quality improvement Separation of aromatics/aliphatics (BTX) Petrochemicals Separation of olefins/parafins Separation of structural isomers Food Industry Decaffeination of coffee and tea Separation of essential oils (flavors and fragrances) Metals Industry Copper production Recovery of rare earth elements Inorganic Chemicals Purification of phosphoric acid Nuclear Industry Purification of uranium

Removal of Organics From Water Distillation vs. Extraction
Organic Compound BP [°C] Water Solu. [%] Azeotrope B.P. [°C] Water [%] Typical Reduction Level Methylene Chloride 40 2.0 38.1 1.5 < 50 ppb Acetone 56.2 Infinite Non Azeotropic Methanol 64.5 Benzene 80.1 0.18 69.4 8.9 Toluene 110.8 0.05 85.0 20.2 Formaldehyde -21 < 1,000 ppm Formic Acid 100.8 107.1 22.5 < 500 ppm Acetic Acid 118.0 Pyridine 115.5 57 92.6 43 < 10 ppm Aniline 181.4 3.60 99.0 80.8 Phenol 8.20 99.5 90.8 Nitrobenzene 210.9 0.04 98.6 88.0 Dinitrotoluene (2,4) 300.0 0.03 99 – 100 > 90 Dimethyl Formamide 153.0 Dimethyl Acetamide 166.1 n-Methylpyrrolidone 202.0 Distillation Extraction

Simple Extraction Single Stage
B – 0 C – 1 100 Feed (F) A – 0 B – 50 C – 0 50 Solvent (S) C – 0.8 50.8 Extract (E) A – 99.0 C – 0.2 99.2 Raffinate (R) Fraction Unextracted Distribution Coefficient Extraction Factor

Cross Flow Extraction R1 R2 R3 R4 A C F + S = M1 R1 + S = M2
A + B F B + C E1 E2 E3 E4 M1 M2 M3 M4 B

Countercurrent Flow Extraction
A + B F B + C C E1 E2 E3 E4 F + S = M E1 + R4 = M F + S = E1 + R4 F – E1 = R4 – S = D Equations B D M S

Countercurrent Extraction
B + C Extract (E): Solute Rich Stream A + B Primary Interface Feed (F) Continuous Phase Dispersed Phase C Solvent (S) Raffinate (R): Solute Lean Stream A

Bench Scale Test Apparatus
Variable Speed Drive Thermometer Baffle Tempered Water In Drain 1 – Liter Flask Tempered Water Out

Equilibrium Curve -> Slope = m Operating Line -> Slope = FI/SI
Simple Extraction Graphical Solution Y X YBE YBS XBR XBF Equilibrium Curve -> Slope = m Operating Line -> Slope = FI/SI m = YB* XB* Distribution Coefficient on Solute Free Basis Process Scheme N F S E R xAS xBF 1.0 yAS yBS yCS xAR xBR xCR yAE yBE yCE Solute Free Basis FI SI EI RI XBF = xBF xAF YBS = yBF yAS+ yCS YBE = yBE yAR+ yCE XBR = xBR xAR+ xCR FI=F(xAR) SI=S(yAS+yCS) EI=E(yAE+yCE) RI=R(xAR+xCR)

Typical LLE Equilibrium Curve
Extract Composition (Wt Fract., Solute Free) Raffinate Composition (Wt Fract., Solute Free)

Graphical Determination of Theoretical Stages 95% Solute Extraction, S/F = 1.0 mass basis
(0.136, 0.114) Extract Composition (Wt Fract., Solute Free) Raffinate Composition (Wt Fract., Solute Free)

Graphical Determination of Theoretical Stages 98% Solute Extraction, S/F = 1.0 mass basis
(0.136, 0.118) Extract Composition (Wt Fract., Solute Free) Raffinate Composition (Wt Fract., Solute Free)

Kremser Equation Where: n = Number of theoretical stages required
xf = Conc. of solute in feed on solute free basis xn = Conc. of solute in raffinate on solute free basis ys = Conc. of solute in solvent on solute free basis m = Distribution coefficient E = Extraction factor = (m)(S/F)

Engineering Calculations Kremser Type Plot
XBR F1 S1 E1 R1 YBS XBF YBE E = Extraction Factor E = m (S1/F1) 1.0 0.8 0.6 0.4 0.3 0.2 0.1 0.08 0.06 0.04 0.03 0.02 0.01 0.008 0.006 0.004 0.003 0.002 0.001 0.0008 0.0006 0.0005 1 2 3 4 5 6 7 8 10 15 20 Number of Ideal Stages XBR/XBF = Fraction Unextracted E = 0.3 E = 20 E = 1.3

Typical Extraction System
B+C+(A) Feed A+B Extraction Raffinate Stripping Solvent Recovery C (A) C (A+B) Solvent C (A+B) A+(B+C) A (B+C) B (C)

Removal of Phenol from Wastewater
ppb Phenol Extraction Raffinate Stripping Solvent Recovery Wastewater Feed 0.1 – 8 % Phenol Raffinate Recycled Solvent Extract Phenol Biological Treatment Or Carbon Adsorption < 1 ppm Phenol

Recovery of Acetic Acid from Water Using a Low Boiling Solvent
Aqueous Feed % Acetic Acid Typical Solvents: Ethyl Acetate Butyl Acetate Extraction Raffinate Stripping Solvent Recovery Raffinate Recycled Solvent Extract Aqueous Raffinate

Recovery of Carboxylic Acids from Wastewater Using a High Boiling Point Solvent
Extraction Dehydration Solvent Recovery Water Feed 0.1 – 5 % Mixed Acids Acetic Acid 99%+ Purity Recovered Solvent Clean Up Acid Recovery Formic Acid Water Raffinate < 1,000 ppb

Neutralization/Washing of Acid or Base or Polar Compounds from Organic Stream
Water Extraction ** Organic Feed could contain caustic. Mid- Feed would be mild acid. Caustic (Mild)** Feed (Organic + Acid) ** Water + Salts

Series Extraction Extractor #1 Extractor #2 Feed A + B Extract B + C
Solvent 1 C Solvent 2 D Product B + D Raffinate A Extractor 1 & 2 May Differ By: - Temperature - pH - Solvent

Recovery of Caprolactam
Feed From Reaction Section Lactam Oil Ext. AQ Waste to Discharge Am. Sulphate Ext. Am. Sulph. Waste to Discharge Re-Extraction Lactam Oil to Recovery Water Lactam Oil Phase 65 – 70% Caprolactam Ammonium Sulphate Phase 2 – 3% Caprolactam Extract Raffinate Solvent

Phosphoric Acid Purification via Extraction
Raffinate to Disposal Scrub Extraction Re-Extraction Phosphoric Acid to Recovery Water Solvent Phosphate Rock Digester HCL Feed Recycle Scrub Solv.

Organo-Metallic Catalyst Recovery
Extraction Feed Makeup Organic Catalyst Preparation Reactor Separator Water Effluent (1 ppm Cobalt) (200 ppm Cobalt) Cobalt Organo-Metallic Product Slipstream Organic

Fractional Extraction Process Scheme
(A-Rich) YAE,YBE XAS2,XBS2 NR XAF,XBF NS XAS1,XBS1 (B-Rich) XAR,XBR

Extraction of Flavors and Aromas
Typical Products: Orange Oil Lemon Oil Peppermint Oil Cinnamon Oil Oil Essential Extract Extraction Solvent 1 Distillation Aqueous Alcohol Solvent 2 Distillation Essential Oil Hydrocarbon

Separation of Structural Isomers
Typical Applications: m. p. - Cresol Xylenols 2 , 6 - Lutidine 3 , 4 - Picoline Solvent 1 Distillation Solvent 2 Distillation Extraction Mixed Isomer Feed Isomer 1 Isomer 2 pH Adjust (Optional) Reflux Solvent 1 Recycle Solvent 2 Recycle Aqueous Raffinate Recycle

Major Types of Extraction Equipment
Mixer Settlers Column Contactors Centrifugal Used primarily in the metals industry due to: - Large flows - Intense mixing - Long Residence time - Corrosive fluids - History Used primarily in the pharmaceutical industry due to: - Large flows - Intense mixing - Long Residence time - Corrosive fluids - History Static Agitated Spray Packed Tray Pulsed Rotary Reciprocating Rarely used Used in: - Refining - Petrochemicals Example: - Random - Structured - SMVPTM Used in: - Refining - Petrochemicals Example: - Sieve Used in: - Nuclear - Inorganics - Chemicals Example: - Packed - Tray - Disc & Donut Example: - RDC - Scheibel Used in: - Chemicals - Petrochemicals - Refining - Pharmaceutical Example: - Karr

Mix / Decant Tank Characteristics
Mix – Settle – Phase separate in a single tank Batch Processing only Requires multiple solvent additions for more than one stage (crossflow operation) Typically used for small capacity operations or intermittent processing Feed Inlet Outlet Sight Glass

Mixer / Settlers Characteristics Handle very high flowrates
Good for processes with relatively slow reactions (residence time required) Provide intense mixing to promote mass transfer Require large amount of floor space Suitable when few theoretical stages required Large solvent inventory (and losses) Light Phase In Heavy Phase Out

Centrifugal Extractor
Characteristics Countercurrent flow via centrifugal force Low residence time ideally suited for some pharmaceutical applications Handles low density difference between phases Provide up to several theoretical stages per unit High speed device requires maintenance Susceptible to fouling and plugging due to small clearances

Packed Column Characteristics
High capacity: M3/M2-hr (Random) gal/ft2-hr (Random) M3/M2-hr (Structured) ,000-2,000 gal/ft2-hr (Structured) Poor efficiency due to backmixing and wetting Limited turndown flexibility Affected by changes in wetting characteristics Limited as to which phase can be dispersed Requires low interfacial tension for economic usefulness Not good for fouling service Feed (F) Solvent (S) Extract (E) Raffinate (R)

Sieve Tray Column Characteristics
High capacity: M3/M2-hr ,250 gal/ft2-hr Good efficiency due to minimum backmixing Multiple interfaces can be a problem Limited turndown flexibility Affected by changes in wetting characteristics Limited as to which phase can be dispersed Feed (F) Solvent (S) Extract (E) Primary Interface Raffinate (R)

RDC Extractor Characteristics Reasonable capacity: 20-30 M3/M2-hr
Limited efficiency due to axial backmixing Suitable for viscous materials Suitable for fouling materials Sensitive to emulsions due to high shear mixing Reasonable turndown (40%) Vessel Walls Shaft Stators Rotors Light Phase In Heavy Phase Out Drive Motor Gearbox Interface Control

Scheibel Column Characteristics
Reasonable capacity: M3/M2-hr gal/ft2-hr High efficiency due to internal baffling Good turndown capability (4:1) and high flexibility Best suited when many stages are required Not recommended for highly fouling systems or systems that tend to emulsify Light Phase In Heavy Phase Out Gearbox Variable Speed Drive Interface Control Vessel Walls Rotating Shaft Turbine Impeller Horizontal Inner Baffle Outer Baffle

Scheibel Column Internal Assembly

Karr Reciprocating Column
Characteristics Highest capacity: M3/M2-hr ,500 gal/ft2-hr Good efficiency Good turndown capability (4:1) Uniform shear mixing Best suited for systems that emulsify Light Phase Inlet Sparger Heavy Phase Out Interface Control Teflon Baffle Plate Tie Rods & Spacers Center Shaft Spider Plate Perforated Plate Metal Baffle Drive Assembly Seal

Karr Column Plate Stack Assembly

Pulsed Extractor Characteristics Reasonable capacity: 20-30 M3/M2-hr
Best suited for nuclear applications due to lack of seal Also suited for corrosive applications since can be constructed out or non-metals Limited stages due to backmixing Limited diameter/height due to pulse energy required Light Phase In Heavy Phase Out Interface Control Timer Pulse Leg Solenoid Valves Compressed Air Exhaust Liquid

Comparison Plot of Various Commercial Extractors
1 2 4 6 10 20 40 60 100 0.2 0.4 .06 Scheibel Karr RDC Graesser Kuhni RZE PFK PSE FK MS SE Efficiency / Stages per Meter Capacity M3/(M2 HR) Graesser = Raining Bucket MS = Mixer Settler SE = Sieve Plate FK = Random Packed PFK = Pulsed Packed PSE = Pulsed Sieve Plate RDC = Rotating Disc Contactor RZE = Agitated Cell Karr = Karr Recipr. Plate Kuhni = Kuhni Column Scheibel = Scheibel Column Key

Column Selection Criteria Static Column
A static column design may be appropriate when: Interfacial tension is low to medium: up to dynes/cm Only a few theoretical stages are required, and reduction in S/F is not an economic benefit No operational flexibility required There is a large difference in solvent to feed rates

Column Selection Criteria Agitated Column
Agitated columns are generally more economical when: More than 2-3 theoretical stages are required Interfacial tension is moderate to high, although low interfacial tensions may also be economical A reduction in solvent usage is beneficial to the process economics The process requires a wide turndown as well as the ability to handle a range of S/F ratios

Column Selection Criteria Rotating Disc Contactor (RDC)
Systems with moderate to high viscosity, i.e. > 100 cps Systems that are residence time controlled, for example, slow mass transfer rate with few theoretical stages required Systems with a high tendency towards fouling

Column Selection Criteria Scheibel Column
Systems that require a large number of stages due to either theoretical stage requirements or low mass transfer rates Low volume applications in which a relatively small column is required Systems that process relatively easily, without a tendency to emulsify and/or flood

Column Selection Criteria Karr Reciprocation Plate Column
Difficult systems that tend to emulsify and/or flood easily Systems in which the hydraulic behavior varies significantly through length of the column Sometimes requiring non-metallic internals, such as Teflon due to wetting characteristics or corrosive materials Fouling applications that may have tars formations and/or solids precipitation

The Three Cornerstones of Successful Extraction Applications
Successful Application Proper Solvent Selection Selection Based on: Sound thermodynamic principles Sound economic principles Availability Recoverability Sound environmental principles Toxicity Safety Meaningful Pilot Tests Accurate Scale-Up Testing Based on: Actual feed stocks Full process including solvent recovery Wide range of operating conditions Scale-Up Based on: Proven techniques Proper safety factors

Organic Group Interactions
Solvent Class Solute Class 1 2 3 4 5 6 7 8 9 10 11 12 Phenol - + Acid, thiol Alcohol, water Active H on multihalogen Ketone, amide with no H on N, sulfone, phosphine oxide Tertiary amine Secondary amine Primary amine, ammonia, amide, with 2H on N Ether, oxide, sulfoxide Ester, aldehyde, carbonate, phosphate, nitrate, nitrite, nitrile Aromatic, olefin, halogen, aromatic multihalogen, paraffin without active H, manahalogen paraffin Paraffin, carbon disulfide 1 - 4 = H donor groups 5 – 12 = H acceptor groups 12 = Non-H bonding groups

Liquid-Liquid Extraction Scale-Up
Theoretical scale-up is difficult Complexity of processes taking place within an extractor Droplet Breakup Coalescence Mass Transfer Axial and radial mixing Effects of impurities Best method of design: Pilot testing followed by empirical scale-up

Pilot Plant Configuration
Determine type of column to be used based on process considerations Use the same kind of equipment for the production unit Determine diameter and height of pilot column based on experience Type of Column Diameter Height Packed 3” to 4” 3’ to 6’ per Theoretical Stage (TS) Tray 4” to 6” 4’ to 5’ Trays per TS Karr 1” 1’ to 3’ per TS Scheibel 3” 3 to 6 Actual Stages per TS (Approx. 3” to 6”)

Continuous Extraction Pilot Plant Arrangement
Hot Oil Feed Solvent Variable Speed Drive Raffinate Extract

KMPS Pilot Plant Services Group
KMPS maintains a pilot plant dedicated to extraction R & D and applications testing

Possible Extraction Column Configurations
Solvent is Light Phase E E B + C B + C F F A + B A + B Primary Interface Solvent Dispersed Solvent Continuous Primary Interface S S C C R R A A Solvent is Heavy Phase A A R R S C S C Primary Interface Solvent Dispersed Solvent Continuous Primary Interface F A + B F A + B E E B + C B + C

Factors Effecting which Phase is Dispersed
Flow Rate For Sieve Tray and Packed Columns – disperse the higher flowing phase For all other columns – disperse lower flowing phase Viscosity For efficiency – disperse less viscous phase For capacity – disperse more viscous phase Viscous drop Diffusion rate inside the drop is inhibited by viscosity Viscous continuous phase Drop rise or fall will be inhibited

Surface Wetting Want the continuous phase to preferentially set the internals – this minimizes coalescence and therefore maximizes interfacial area. Importance of maintaining droplets Assume – 30% holdup of dispersed phase in 1 M3 of solution Droplets coalesce. Interfacial area lost. Droplets retain shape. Maximizes interfacial area. Droplet Diameter [m] Droplet Volume [M3] Number Droplets Droplet SA [M2] Interfacial Area [M2/M3] 100 0.3 7.16x1010 1.26x10-7 9022 300 2.65x109 1.13x10-6 2995 500 5.73x108 3.14x10-6 1796

Marangoni Effect Coalescence is enhanced by mass transfer from droplets continuous phase A + B C A C + B Mass Transfer Direction Dispersed Continuous (d c) Droplets tend to coalesce Must be counteracted by additional energy Continuous Dispersed (c d) Droplets tend to repel each other Less energy required to maintain dispersion

Growing Uncontrolled Interface
Interface Behavior Actions to control unstable interface As extraction proceeds, interface normally grows in thickness and forms a “rag” layer that stabilizes at some thickness If rag layer continues to grow, some action must be taken Rag Layer Light Phase Dispersed Heavy Phase Dispersed Growing Uncontrolled Interface 1 2 Filter Rag Draw Continuously withdraw a portion of the interface and pass through a filter to remove interfacial contamination Reverse Phases Often a stable interface can be controlled by reversing which phase is dispersed

Entrainment Entrainment involves carrying over a small portion of one phase out the wrong end of the column. Entrainment is controlled by: 1.) Increased settling time inside the column 2.) Coalescer inside the column 3.) Coalescer external to the column E F R S OR 1 2 3

Flooding Flooding – the point where the upward or downward flow of the dispersed phase ceases and a second interface is formed in the column. Flooding can be caused by: Increased continuous phase flow rate which increases drag on droplets Primary Interface f F1 S E R F2 Second Interface F2 > F1

Flooding f2 > f1 F1 S E R F2 Flooding can be caused by:
Increased agitation speed which forms smaller droplets which cannot overcome flow of the continuous phase Decreased interfacial tension – forms smaller drops – same effect as increased agitation Primary Interface f1 F1 S E R f2 F2 Second Interface f2 > f1

Pilot Tests Static Columns (Packed, Tray)
f F S D H Static Columns (Packed, Tray) Agitated Columns (Scheibel, Karr) N, S/F D, H (F+S) N, S/F D, H (F+S),f Process Factors Column Variable Variable F+S HETS Flood MIN HETS

Extractor Flow Patterns
Ideal Plug Flow Actual Flow This “axial” or “back” mixing causes concentration gradients that decrease driving force and therefore increase HETS Y X

Generalized Scale-up Procedure
Pilot Scale Commercial Scale f2 f1 Q1 Q2 Feed Rate Feed Rate H1 H2 D1 Basic Scale-up Relationships: D2/D1 = K1(Q2/Q1 )^M1 H2/H1 = K2(D2/D1 )^M2 f2/f1 = K3(D2/D1)^M3 D2 Where: K1, M1 = Capacity Scale-up Factors K2, M2 = Efficiency Scale-up Factors K3, M3 = Power Scale-up Factors

Application – Scheibel Column
Extraction of nitrated organics from spent acid stream using an organic solvent Reduce nitrated organic compounds from 3.9% to less than 50 ppm S/F ratio fixed by process at 3.9 Equilibrium data indicated that 4.5 theoretical stages required Commercial design: 3,900 lb/hr (270 GPH) spent acid feed

Scheibel Column Pilot Plant Setup Nitrated Organics Extraction
Hot Oil Spent Acid Feed MCB Solvent Aqueous Raffinate Organic Extract Interface Variable Speed Drive

Scheibel Column Pilot Plant Test Results Nitrated Organics Extraction
11 600 78 235 380 36 9 15 70 185 300 10 13 650 83 328 84 18 3 776 500 80 2 159 91 5 963 43 4 148 700 74 7 563 73 6 54 82 Column Temp [°C] 400 Agitation Speed [RPM] 47 150 240 12 16 8 856 1 Raffinate - Nit. Org. Conc. [PPM] MCB Feed [cc/min] Acid Feed [cc/min] # of Stages Run

Scheibel Column Scale-up Procedure Nitrated Organics Extraction
600 14” Dia. = 430 GPH/FT2 530 Rate in Commercial Column For Dia. ≥ 18” Column Capacity For Dia. < 18” 300 [GPH/FT2] [GPH/FT2] 100 157 5 10 15 20 [GPH/FT2] [IN] Rate in 3” Dia. Pilot Scheibel Column Scheibel Column Diameter

Scheibel Column Pilot Plant Scale-up Nitrated Organics Extraction
Diameter = 14” (D1) Expanded Head Diameter = 20” (D2) Bed Height = 9’-6” (A) Overall Height = 16’-4” (B) A D1 D2 B

Application – Karr Column Alcohol Extraction from Acrylates
Extraction of methanol from an acrylate stream using water as the solvent Reduce methanol from 2.5% to less than 0.1% S/F ratio specified by client as 0.32 wt. basis Equilibrium data: distribution coefficient generated by KMPS, with average value of 5.3 Commercial design: 36,900 lb/hr (4,660 GPH) acrylate feed

Karr Column Pilot Plant Setup Alcohol Extraction from Acrylates
1” Dia. x 8’ Plate Stack Plate Spacing from Top: ’ of 2” ’ of 4” ’ of 6” 316SS Shaft, Plates & Spacers Variable Speed Drive Hot Oil Raffinate (Acrylate Phase) Extract (H2O + Alcohol) Water Feed Acrylate Feed (methyl or ethyl) Interface

Karr Column Pilot Plant Test Results Methanol Extraction from Acrylate
Run Plate Stack Feed Rate [cc/min] Water Feed Rate [cc/min] Agitator Speed [SPM] Interface Raffinate Conc. Alcohol Raffinate Conc. Water 1 150 45 100 Bottom 0.124 2.55 2 75 0.165 2.83 3 110 0.169 2.78 4 140 0.112 2.72 5 180 54 0.203 2.90 6 125 0.146 3.08 7 0.118 2.66 8 200 0.078 2.73 9 210 63 175 0.084 2.65 Notes: Karr column with 1” dia. X 6’ plate stack height. Plate stack #1 is constant 2” plate spacing. Plate stack #2 has variable spacing, from top: 4’ of 2”, 1’ of 4”, 1’ of 6” spacing. Feed is acrylate with approximately 2.5% methanol

Karr Column Pilot Plant Scale-up Procedure Methanol Extraction from Acrylate
Select optimal run from test results * Run 8: Feed Rate = 150 cc/min Solvent Rate = 45 cc/min Specific Throughput (Q) = 560 GPH/FT2 Production column design * Diameter – direct scale-up based on specific throughput * Height – HCOMM = ƒ (H)PILOT * Agitation Speed – SPMCOMM = ƒ (SPM)PILOT

Karr Column Pilot Plant Scale-up Procedure Methanol Extraction from Acrylate
HCOMM = (DCOMM / DPILOT)0.38 x HPILOT HCOMM = (45/1)0.38 x (6 feet) = 26 feet SPMCOMM = (DPILOT / DCOMM)0.14 x SPMPILOT SPMCOMM = (1/45)0.14 x (200 SPM) = 117 SPM Where: * HCOMM = Height Commercial Column * HPILOT = Height Pilot Column * DCOMM = Diameter Commercial Column * DPILOT = Diameter Pilot Column * SPMCOMM = Commercial Strokes Per Minute * SPMPILOT = Pilot Strokes Per Minute

Karr Column Pilot Plant Scale-up Methanol Extraction from Acrylate
D1 D2 B Diameter = 45” (D1) Expanded Head Diameter = 68” (D2) Plate Stack = 26’-0” (A) Overall Height = 36’-8” (B)

Extraction Experience
KMPS has supplied over 300 extraction columns.

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Liquid-Liquid Extraction

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