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Used Chlorobenzene, Co2 Plant, Desalination Plant, Edc Vcm Plants, Ethyl Acetate Plant, Ethylene Oxi
Posted at: TradersCity --> Offers to Sell and Export
Posted on: Sat 27 Oct, 2007 4:52 am
Used Chlorobenzene, Co2 Plant, Desalination Plant, Edc-vcm Plants, Ethyl Acetate Plant, Ethylene Oxide Plant
Chlorobenzene Facility
Overview / Process Details:
Recently Closed Facility That Includes The Following Complete Processes Is Now Available For Immediate Relocation: Monochlorobenzene (mcb) 130m Lbs/year Paradichlorobenzene (pdcb) 39m Lbs/year Orthodichlorobenzene (odcb) 13m Lbs/year Paranitrochlororbenzene (pncb) 69m Lbs/year Orthonitrochlorobenzene (oncb) 51m Lbs/year The Plant Was Operated By A Major Mutli-national Chemical Producer And Was Kept In Excellent Operating Condition. Nitroaniline Plant This Complete Facility Is Immediately Available For Relocation. Paranitroaniline (pna) 12m Lbs/year Orthonitroaniline (ona) 10m Lbs/year
Product Info:
Ncb Isomer Control Technology/equipment Overview Process: Nitrate Mono-chlorobenzene To Make Para, Ortho, Meta Nitrochlorobenzenes. Ncb Process: Mcb+nitric Acid= Pncb + Oncb + Mncb + H2o Mw 112.5 +63.0 157.5 Plant Capacity: Ncb: 120 M#/yr At The Low P/o-ncb Ratio. 1.33 156 M#/yr At The High P/o-ncb Ratio. 1.88 The Equipment Related To The Isomer Control Has A Much Higher Equivalent Ncb Capacity Than Either Of The Above. Strengths Of Technology: • Good Quality O Pncb Purity >99.3% O Oncb Purity >99.9% • Isomer Control Range From 1.3:1.0 To 1.8:1.0 P/o Ratio • Proven Technology • Reliable Operations Ncb Isomer Control Equipment: • Separator (acid Dehy Pot/tank - 701) O 825 Gal, Tantalum Clad O 58 Inch Diameter X 60 Inch O 58 Inch Diameter Teflon Demister • Reboiler (acid Dehy Reboiler - 703) O 16 Inch Diameter X 24 Feet Long O 54 Tantalum Tubes With Tantalum Clad Heads • Condenser (acid Dehy Condenser - 706) O 33 Inch Diameter X 12 Feet Long O 698 Tubes O Alloy 20 • Economizer (acid Dehy Interchanger - 720) – Tantalum Plate And Frame Throughput: The Isomer Control Equipment Could Easily Handle The Volumes Required For The Above Stated Capacity. Reduced Water From ~8.5% To <3.5%. All The Equipment Above Could Easily Be Relocated Installed: 9/76 Condenser In Service Since ~ 2000 Utilities: Nitrogen Is Used For Tank Blanking And Clearing Process Lines. Tower Water And / Or Chilled Water Is Required To Crystallize Pncb. Column Reboilers Used 200 And 600 Psig. Steam Is Also Required Throughout The Process To Pull Vacuum On Various Pieces Of Equipment And Heat Tanks Section I Synopsis Of The Process The Function Of The Dichlorobenzene Department 224 Is To Separate A Mixture Of Dichlorobenzene (dcb) Isomers Generated In The Mcb Department Into Refined Para-dichlorobenzene (pdcb), Ortho-dichlorobenzene (odcb) And Mixed Dcbs Containing Meta-dichlorobenzene (mdcb). All Three Of These Products Are Sold In The Merchant Market. The Dcb Refining Operations Can Be Divided Into Three Primary Areas: Continuous Crystallization, Batch Crystallization, And Batch Distillation. The Counter Current Continuous Crystallizer (4c) System Consists Of Two Jacketed Vertical Crystallizers And A Liquid/liquid Distillation Column. A Mixture Of The Crude Dcb From The Mcb Column In Department 233 And The Recycle Streams From The Batch Crystallizers And Odcb Column Areas Is Fed To The Primary Continuous Crystallizer. Chilled Water Is Pumped Through The Cooling Jacket And Used To Freeze Out The Pdcb On The Sidewalls Of Each Crystallizer. A Rotating Scraper Assembly Inside The Vessel Removes The Pdcb Crystals, Forming A Slurry At The Bottom Of Each Crystallizer. The Slurry From The #1 Crystallizer Is Pumped Through A Hydrocyclone Into The Purifier Column. In The Purifier, The Pdcb Crystals Gravity Settle To Form A Bed Of Crystal. Steam Is Used Melt The Crystals At The Bottom Of The Purifier, Forming A Liquid Reflux That Washes Back Up The Column Through The Crystal Bed. This Reflux Washes Any Remaining Odcb Impurities From The Crystals. Molten Pdcb Of 99.9+% Purity Is Pumped Out Of The Bottom Of The Purifier To Product Storage. The Molten Pdcb Is Loaded Into Tank Cars And Trucks To Be Shipped To Customers. The Liquid From The Primary Crystallizer Overflows Into The Secondary Crystallizer, Where Chilled Water Is Again Used To Freeze Out More Pdcb At A Lower Temperature. The Resulting Pdcb Rich Slurry Is Recycled Through Another Hydrocyclone Into The Primary Crystallizer. The Liquid Stream From The Secondary Crystallizer, Called Para Liquor, Overflows To An Intermediate Storage Tank, From Which The Material Is Pumped To The Batch Crystallization System. In The Batch Crystallization Process, Additional Pdcb Is Removed From The Para Liquor To Provide An Odcb-rich Feed Stream For The Odcb Column. The Para Liquor Is Fed To Three Batch Crystallizers - One Individual Crystallizer And Two Crystallizers That Operate In Parallel. Most Of The Remaining Pdcb Is Crystallized When The Liquor Is Cooled To 14°c Using A Chilled Ethylene Glycol Solution. The Chilled Liquid, Now Called P-still Feed, Is Drained From The Crystallizers And Pumped To The P-still Charge Tank For Odcb Purification At The P-still. The Remaining Crystals Are Melted Out And Pumped Back To The Crude Dcb Storage Tanks As Recycle. Another Type Of Batch, The Meta Batch, Is Run In An Individual Crystallizer. In This Batch, A Concentrated Meta-dichlorobenzene Stream From The Odcb Refining Column Is Charged Into The Crystallizer. The Material Is Cooled To 12°c And The Liquid Is Drained And Pumped To Storage To Be Sold As Mixed Dcb. The Remaining Solids Are Then Melted Out And Pumped Back To The Crude Dcb Storage Tanks As Recycle. The Odcb Column Or P-still Is Charged With The P-still Feed From The Batch Crystallizers. The P-still Feed Is Refined Using A Batch Vacuum Distillation Column Into Five Separate Streams Or Cuts. The First Cut Taken Off The Column Is The Mono Cut, Which Removes Any Trace Amounts Of Water And Mcb In The Feed. This Cut Is Recycled Back To The Benzene Drying Process In Department 233. The Second Cut Is The Meta Cut, Which Is Taken To Purge Metadichlorobenzene From The Process. This Stream Is Sent To The Static Crystallizers For Further Refining. The Third And Fourth Distillation Cuts Are Recycle Streams. The Third Cut, Intermediate Cut, Is Pumped Back To The Para Liquor Storage Tanks To Be Recycled Through The Static Crystallizers. The Fourth Cut, Tech Cut, Is Recycled Back To The P-still Charge Tank. The Fifth And Final Cut Taken Off The Distillation Batch Is The Product Cut. The Purity Requirement For Product Odcb Is 99.0% Odcb. Product Odcb Is Shipped Out In Tank Cars And Tank Trailers. Any High Boilers (primarily Trichlorobenzene And Catalyst From Mcb) Will Build Up In The P-still Pot Over Time. The Material Is Concentrated And Pumped Out To A Tank Truck Every Six Weeks To Be Incinerated As Residue Waste.
Co2 Plant
Capacity: 200 Tpd
Year Built: 1968
Year Shut: Completely Refurbished In 1997, Closed In 1998
Product Info:
Co2 Product Purity Is 99.2%, Inlet Feed From Blower Pipeline At 98% Co2 Purity. Major Equipment: Cooper Compressor, Stripper Skid, Dryer / Chiller Skid And A Heat Exchanger Skid: Ac/dc Ge Motor
Plant Is Missing 2 Separator Pots, Some Of The Exchanger And Ko Vessels Are Missing. Additionally;
C-2 High Stage Compressor Cylinder From Compressor (relocated To Tx.)
D-2 Knock Out Pot /moisture Trap
E-3 Heat Exchanger
F-1 Dryer Filter
Compressor, Circa 1959, Cooper Bessemer, Model Fm6, 5 Stage, Contains Both Co2 And 2 Nh3 Ammonia Cylinders
No 46779
Stoke 10 1/2"
450 Rpm
Type Fm6
1319 Hp
Westinghouse Synchronous Motor
Hr-6e2
Hp 1500
Hz 60
% Load 100 Hr/24
4160 V
450 Rpm
Amps 161
Sf 1.0
Cylinder Information:
Oper Press Suct 2.3 #ga
Oper Discharge Press
353 # Ga
Max Press 75 # Ga
S/n 36843 Normal Clearance 8.1
Size 29 3/4 X 10 1/2
Class Ckn-105 Max Relief Valve Setting
75 Oper Press Suct .3 #ga
Oper Discharge Press 51.3 # Ga
Max Press 250 # Ga S/n 36846
Normal Clearance 8.0 Size 23 X 10 1/2
Class Chb-105 Max Relief Valve Setting 250 Psi
Desalination Plant
Capacity: 27,000
Technology: Gea Niro Kestner Sa
Year Built: 1998
Year Shut: 2006
Raw Materials: Nacl Crystals
Overview / Process Details:
Desalination Plant, Designed And Built By Gea Niro Kestner Sa, 1998, Shutdown 2006, Material Of Construction Titanium. The Plant Was Designed To Remove Salt And Recover Product From The Waste Stream. Feed Rate To The Plant Is Approx 27,000 Litres/hr, Evaporator Consumes Approx 8600 Kgs/hr Of Steam. The Unit Comprises Of A Triple Effect Evaporative-crystallizer Unit Functioning Under Vacuum Including Forced Circulation Crystallizers Of The Msmpr Type; A Finisher In Order To Extend The Capacity Of The Crystallization Unit And Obtain A Significant Increase Of The Organic Concentration Contained In The Final Extracts Of The Mother Liquor; A Section Where The Feed Solution Undergoes A Pre-treatment, Comprising Of A Pre-heater And A Flash Tank; A Washing And Dewatering Section Of The Nacl Crystals; A Section For The Dissolution Of The Nacl Crystals
Edc-vcm Plant - 100,000 T/y
Capacity: 80,000 T/y Edc And 100,000 T/y Vcm
Technology: Inovyl & Stauffer
Year Built: 2001
Overview / Process Details:
Oxy Plant Oxygen Based Fixed Technology (3 Stages). Ethylene Absorption From Vent Gas By Cold Edc. 1 Terrace Wall Furnace On Cracking With External Stem Vaporization Of Edc. No Incinerator. Edc Distillation With Common Drying Column For Edc From Oxy And Import Edc. Heat Recovery From Cracking With Pump Around To Reboil Hci Column. Plant Balanced With Edc Import. Cooling Water Tower.
Edc-vcm Plant - 140,000 T/y
Capacity: 140,000 T/y Edc And160,000 T/y Vcm
Technology: Solvin
Year Built: Ethylene Cracking Furnaces - New 2001
Year Shut: 2005
Product Info:
Consumption Ratio And Figures: Ethylene 473 Kg/ton Of Vcm Chlorine 600 Kg/ton Of Vcm Power 180 Kwh/ton Of Vcm Water Demin 0.14 M³/ton Of Vcm Cooling Water 123 M³/ton Of Vcm Fuel Gas 2.7 Gj/ton Of Vcm Instrument Air 54 M³/ton Of Vcm Off Gas To Incineration 70 M³/t Vcm Emission To Air (incl. Fugitive): Vcm 1400 Kg/y Edc 2500 Kg/y Effluent Discharge To Biotreatment 1,1 M³/t Vcm Cod Untreated 1,4 Kg/m³ Vcm Quality: Purity 99.9 Wt% Moisture 20 Ppm Low Boiling 50 Ppm High Boiling 100 Ppm Iron 0.3 Ppm Note: The Following Sections Of The Plant Are Available: Edc Drying/distillation Oxichlorination Cracking Hci-separation/vcm-distillation Vcm-plant: Available Process Parts Edc-drying/distillation Raw Edc-feed To Drying K 11 40t/h (oxy-edc + Cracking – Edc) K11 D 2,5 M, H 33m Process Pressure 0,4 Bar-g Raw Edc-feed To Distillation K15 42t/h Giving 41 T/h Pure Edc K15 D 2,0 M; H 19m Process Pressure 2,0 Bar-g Feed To Heavy Ends Col. K13 1,2 T/h Giving 0,35 T/h Heavies K13 D 0,6m; H 17m Process Pressure 0,4 Bar Abs Oxy Chlorination Hci-feed To Oxi-reactor C24 12 T/h Giving 15,8 T/h Edc Ethylene-feed 4,9 T/h Exygen-feed 2,7 T/h C24 Solid Bed Catalyst 10 T, 2599 Pipes 10 M Long, Di27 Mm; Lc-ni99 Process Pressure 5 Bar-g, Max Temp 300°c Beam Generation 19 T/h 16-24 Bar V20 (hci) (recycle Gas) Turbo Atlas Copko (6kv) Carbon Heat Exchangers W242, 243, 245; Piping Carbon Steel With Ptfe Lining Waste Water Steam Stripping K42 Titanium, Feed 8 M³/h Edc-cracking Edc-feed To Furnace 19,3 T/h Giving 60 Kt/y With 8.400 H/y Cracking Ratio 60%; Process Pressure 7 Bar-g; Max Temp 500c Cracking Pipes Incoloy 800 Ht Hci-separation/vcm-distillation Crackages Feed To K34 55 T/h Giving 12 T/h Hci K34 D 1,3 M; H 34 M; Process Pressure 4,0 Bar-g Refrigeration Unit 2,2 Mw Feed To Vcm-distillation 43 T/h Giving 20 T/h Vcm For Polym. K35 D 1,3 M; H 20 M; Process Pressure 4,8 Bar-g Vcm Stripped K37 D 0,8 M; H 14 M; Process 4,8 Bar-g Edc Exchanger For The First Two Furnaces There Are (4) Robertverdampfer" 156 M2 And Installed In 1994, Normal Steel St 35. For The Third Furnace, There Are (2) "umlaufverdampfer" 173 M2 Built In 1988 And Composed Of Monel 400.
Ethyl Acetate Plant
Capacity: 10,000 Mt/y
Technology: Tischtshenko – Gemany
Year Built: 1987
Year Shut: 2004
Overview / Process Details:
Tischtshenko Reaction Using Acetaldehyde As Raw Material And Aluminum Ethylate As Catalyst. Reaction Is Exothermic.
Major Equipment:
(1) Titanium Column (1) 316ss Column (2) 304ss Columns (2) Carbon Steel Colums (2) Luwa Thin Film Evaporators (extract Caralyst From Liquid)
Additional Info:
From Same Site Also Available Are The Following Plants: Acetic Acid Plant, Anhydride Acetic Plant, Acetyl Salicylic Acid Plant, And Acetaminophen Plant
Ethylene Oxide Plant
Capacity: 100,000,000 Lbs/yr.
Technology: Shell – Direct Oxidation Process
Year Built: 1988
Year Shut: 2000
Product Info:
Fat Absorbent From The A-4 Ethylene Oxide Absorber Tower Serves As Feed To The Eo Purification Section. Fat Absorbent Exits The Bottom Of The Absorber Section Of A-4 At 90-140 Of And Is Joined By The Bottoms Stream From The A-56 Residual Gas Absorber (recovered Eo From Residual Gas). Fat Absorbent Contains 1.5-2.5% Eo. The Fat Absorbent Stream Is Preheated First By The T-12 Fat Absorbent Preheater By Heat Exchange With Lean Absorbent From The T-51 Feed Product Exchanger, Next By The T-10 Secondary Product Cooler By Exchange With Reactor Exit Gas From The M-13 Reactor Knockout, And Finally By The T-51 Feed Product Exchanger By Exchange With Lean Absorbent From The Bottoms Of The A-51 Eo Stripper Tower. Fat Absorbent Exits T-51 And Enters The A-51 Tower At 180-200 Of. The A-51 Eo Stripper Tower Separates Eo From The Fat Absorbent Stream. A-51 Overheads Provide Feed To The Rest Of The Ethylene Oxide Purification Section. In Addition To Fat Absorbent, A-51 Also Receives Recycle Feed Streams From The A-52 Quench Bleed Stripper Overheads (recovered Eo From The A-4 Bottoms Quench Bleed) And From The A-54 Eo Purification Column Bottoms. Heat Is Supplied To A-51 By Return Steam From The T-56 Glycol Bleed Reboiler And By Condensate Addition From The P-11a/b Condensate Pumps Based On A-51 Level Control. Heating Can Also Be Provided By Open 50# Steam Addition, But This Creates An Excessive Water Load Which Must Be Relieved By Dumping Lean Absorbent To The Sewer. The A-51 Tower Is Operated At A Low Pressure Of 1-4 Psig (enabled By The Upstream C-51a/b/c/d Eo Compressors). This Low Operating Pressure Reduces The Amount Of Ethylene Oxide That Is Hydrolyzed At Elevated Temperatures To Ethylene Glycol (predominantly Mono Ethylene Glycol). Ethylene Glycol Must Be Removed From The A-51 Bottoms Lean Absorbent Stream Through The Glycol Bleed Stream. Lean Absorbent Exits The Bottom Of The A-51 Tower At 200-250 Of By Means Of The P-51a/b Eo Stripper Bottoms Pumps. Lean Absorbent Contains 1.5–2.0 % Eg And < 0.10 % Eo. A Sidestream From The Discharge Of P-51a/b Supplies The T-56 Glycol Bleed Reboiler Based On Level Control. T-56 Serves As Both A Reboiler To Supply Heat To The A-51 Tower As Well As A Glycol Concentrator To Remove Glycols From The System. Heat Is Supplied To The T-56 Tube Side By 50# Steam. Steam Generated In The T-56 Shell Side Returns To The Bottom Section Of A-51. The Glycol Bleed Stream Is Pumped Out Of The T-56 Shell Side By The P-52 Glycol Bleed Pump. The Glycol Bleed Stream Contains 0-35% Eg And Feeds The A-302a Glycol Flash Tank (see “glycol Recovery Section”). Excluding The Sidestream To T-56, Lean Absorbent Is Pumped By P-51a/b To The T-51 Feed Product Exchanger And Then The T-12 Fat Absorbent Preheater, Both Of Which Cool The Lean Absorbent Stream By Exchange With The Fat Absorbent Feed To A-51. At The Exit Of T-12, A Portion Of The Lean Absorbent Stream Can Be Diverted To The Sewer Based On A-51 Level Control. Lean Absorbent Flow Proceeds To The T-69a, T-69, T-138, And T-139 Lean Absorbent Coolers, Where It Is Cooled By Exchange With Cooling Water. T-69a Is A Shell And Tube Exchanger; T-69, T-138, And T-139 Are Plate-and-frame Exchangers. From These Coolers, The P-10a/b Lean Absorbent Pumps Feed Lean Absorbent To The A-4 Ethylene Oxide Absorber Tower. A Sidestream Of Lean Absorbent Also Supplies Feed To The A-56 Residual Gas Absorber. The Lean Absorbent Coolers Are Placed In Service In Series With Each Other As Needed To Maintain Lean Absorbent Feed Temperature To A-4 At 50-80 Of And A-4 Overheads Temperature At 50-90 Of. The A-51 Overheads Stream Exits The Tower At 200-210 Of And Contains Ethylene Oxide Stripped Out Of Fat Absorbent As Well As Water And Non-condensable Impurities. A-51 Overheads Is Cooled In The T-53 Eo Stripper Overhead Condenser And Then Enters The M-51 Condensate Tank. The Bottoms From M-51 Are High In Water Content And Are Pumped By The P-53a/b Condensate Pumps To The Mix Nozzle On Top Of The T-54 Residual Eo Condenser. The Overheads From M-51 Are High In Eo Content And Are Compressed By The C-51a/b/c/d Eo Compressors From 1-4 Psig And 65-115 Of To 38-48 Psig And 200-245 Of. The Discharge Of The C-51 Compressors Combines With Co2, Non-condensable Gases, And Uncondensed Eo From The Overhead Stream Of The A-53 Light Ends Column And Is Then Cooled In The T-60 Eo Compressor Vapor Cooler. M-51 Overheads And Bottoms Are Then Combined In The T-54 Mix Nozzle And Cooled In T-54. Co2, Non-condensable Gases, And Uncondensed Eo Exit The Top Of The T-54 Shell To The A-56 Residual Gas Absorber. Condensed Liquid From The Bottom Of The T-54 Shell Flows Into The M-52 Stripper Tops Surge Tank. M-52 Is Vented To A-56 As Well. Liquid Bottoms From M-52 Is Composed Of Roughly 50% Eo And 50% H2o With Less Than 1% Co2. M-52 Bottoms Are Pumped By The P-54 Feed Pump Or The P-53b Condensate Pump To The T-55 Light Ends Column Preheater And Then The A-53 Light Ends Column. The Density Of The A-53 Feed Stream Is Measured At P-54/p-53b By A Process Analyzer Which Coverts The Measured Density To A Readout As %eo. The Eo Content Of A-53 Feed Is Maintained At Or Near 50% By Adjusting The Flow Of 50# Steam To The Tube Side Of The T-56 Glycol Bleed Reboiler, Thus Varying The Amount Of Reboiler Steam Returned To The A-51 Tower. Dow Antifoam B From The M-60a Antifoam Transfer Tank Is Added To A-53 Feed Just Upstream From T-55. A-53 Is A Packed Column That Removes Co2 And Non-condensables Dissolved In The Crude Eo Stream. A-53 Feed Enters The Column At 100-130 Of. In Addition To T-55, A-53 Is Heated By Direct Addition Of 200# Steam. Non-condensables In A-53 Overheads (mostly Co2 Plus Eo And H2o) Exit The Tower At 125-145 Of And 42-60 Psig Based On Pressure Control. The A-53 Overhead Stream Joins The Discharge Of The C-51 Eo Compressors To T-60. The A-53 Bottoms Stream Exits The Tower At 142-155 Of On Level Control. The A-53 Bottoms Stream Contains Roughly 50% Eo And 50% H2o And Supplies Feed To The A-54 Eo Purification Column. The A-54 Column Performs The Final Strip To Remove Water From The Eo Purification Stream. Heat Is Supplied To A-54 By The T-64 Product Feed Reboiler. T-64 Is A Thermal Siphon Reboiler And Is Supplied With 200# Steam Based On Tower Temperature Control With A Latching Relay Override For High Tower Pressure. A-54 Operates At 37-45 Psig. Bottoms Exit A-54 At 285-295 Of And Contains 0.0-0.5% Eo And 0.0-4.0% Eg. A-54 Bottoms Are Fed To The A-51 Ethylene Oxide Stripper To Recover The Ethylene Oxide In This Stream. A Side Draw From Trays 6, 8, And 10 Of A-54 Is Pumped By The P-56a/b Feed Pumps To The A-55 Acetaldehyde Column. A-55 Is A Packed Column That Removes Acetaldehyde From The Eo Purification Stream. Heat Is Supplied To A-55 By The T-57 Acetaldehyde Column Reboiler. T-57 Is A Thermal Siphon Reboiler And Is Supplied With 50# Steam Based On Tower Level Control. Bottoms Exit A-55 At 135-155 Of And Are Pumped To The R-6 Eo Reactor By The P-305 Acetaldehyde Metering Pump (see “glycol Recovery Section”). A-55 Overheads Exit The Column At 125-140 Of And Return To A-54. Cooled Condensate Is Fed To The Upper Section Of The A-54 Tower To Prevent Formaldehyde From Escaping In The Tower Overheads. Overheads Exit A-54 At 115-123 Of, Are Condensed In The T-59a/b Eo Condensers, Subcooled In The T-59c Eo Condenser Sub-cooler, And Then Flow To The M-53 Eo Reflux Drum. M-53 Is Vented To The A-56 Residual Gas Absorber. Ethylene Oxide Product Is Pumped From M-53 By The P-58a/b Eo Purification Column Reflux Pumps. P-58a/b Supplies Reflux To A-54 And Eo Product To Storage. The A-56 Residual Gas Absorber Recovers Ethylene Oxide From The Eo Purification Vents (t-54 Residual Eo Condenser, M-52 Stripper Tops Surge Tank, And M-53 Eo Reflux Drum). A-56 Is A Packed Column And Operates Under 35-42 Psig Of Pressure. Lean Absorbent Fed To A-56 Serves As The Eo-absorbing Media. Recovered Eo In The A-56 Bottoms Stream Is Pumped By The P-59a/b Bottoms Pumps To The Fat Absorbent Stream From A-4 At The Inlet Of The T-12 Fat Absorbent Preheater. The Eo Rerun Line From Eo Storage, Which Is Used To Rework High-water Eo Product Through The Purification Section, Ties Into The A-56 Bottoms Line Near T-12. The Overhead Line From The A-6a Carbonate Flash Tank Column (high Ethylene Content) Ties Into The A-56 Overheads Line Downstream From The A-56 Overhead Pressure Control Valve. Co2 And Non-condensable Gases In A-56 Overheads Flow To The M-54 Residual Gas Knockout. The C-52/52a Residual Gas Compressors Take Suction From M-54 And Return The Residual Gas To The Recycle Gas Stream At The Inlet Of The T-10 Secondary Product Cooler.
Additional Info:
Many Spare Parts Available. Complete Documentation. Complete Ethylene And Oxygen Plant From Site As Well
Price Upon Request
Pictures Upon Request
Subject To Prior Sale
The Above Information Is Correct To The Best Of Our Knowledge,
But We Cannot Be Held Responsible For Any Errors Or Ommissions.
For Further Information I Am Gladly At Your Disposal.
Regards,
Sidra (miss)
Sidra Commercial Trading Company,
P.o.box 2504, (gpo).,
Lahore- 54000
Islamic Republic Of Pakistan
Voice: 92-0300-4705383
_________________
Contact Name: Sidra Commercial Trading Company
Company Name: SIDRA (MISS)
Email: sidraco@gmail.com
Tel: 92-300-4705383
Fax: 92-42-6558083
Street Address: P.O.BOX 2504,
G.P.O., Lahore - 54000, Pakistan
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Posted By Sidracommercialtradingcom
Country:  Pakistan
Member Since: 26 October 2007
Total Leads: 419
Business focus: Portland Cement, Sugar, Urea, Scrap, Used Power Plants, Used Generators, Used Machine Tools, Used Processing Plants, Used Plastic Machinery
 
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