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Used Phosphoric Acid Plant, Pvc Plant

Posted at: Offers to Sell and Export | Posted on: Sat 27 Oct, 2007 5:22 am |
 
phosphoric acid plant pvc
Products Photos CatalogPhosphoric Acid Plant Photos Catalog



Used Phosphoric Acid Plant, Pvc Plant



Phosphoric Acid Plant

Capacity: 40 000 Tons H3po4/year

(75 %)

Technology: Combustion And Hydration In The Same Tower

Year Built: 1979

Year Shut: Currently Working

Product Info:

The Solid Yellow Phosphorous Arrives In Rail Tank Cars Or In Metal Drums, Under Water. The Yellow Phosphorous, Which Arrives In Rail Tank Car, Is Melted By Steam And Unloaded Into A Store Under The Earth. The Yellow Phosphorous Is Stored In Liquid Form Under Water. It Is Forwarded From The Store By Pumps Into The Intermediary Storage Tanks. The Phosphorous Gets With The Help Of Water Pressure To The Phosphorous Burners Laid On The Top Of The Phosphorous Burning And Absorption Tower. The Phosphorous Meets The Atomizer Air At The Outlet Of The Burner, It Flames Up Spontaneously, And It Burns Away While High Temperature Heat Is Generated. The Phosphorous Burning Takes Place While Air Surplus Is Assured. The Air Surplus Is Assured By The Secondary Air, Which Flows In Through The Small Gaps Around The Burners. The Air Inflow Is Resulted By The Suction Effect Of The Waste Gas Ventilator. The Arising Phosphorous-pentoxide Reacts With The Water Content Of The Phosphoric Acid, Which Gets Into The Tower, And Creates Phosphoric Acid. This Is The Final Product, Which Contains 75% And 85% Concentration Of H3po4. The Concentrated Phosphoric Acid Coming From The Tower Gets Into A Circulation Tank, Where It Is Diluted With Water To The Requested Concentration. The Phosphoric Acid Cools Down On Cooling Equipment With Pipes, And Gets Back To The Acid Atomiser And The Acid Film Forming. The Phosphoric Acid Product Goes To The Storage Tank Also From This Part. The Ventilator At The End Of The Production Line Results In Depression In The Absorption Tower, Assuring The Necessary Air Surplus. The Gas With Acid Drops Outgoing From The Tower Gets Into Venturi Scrubbers. When The Gas Has Lost The Most Of The Acid Drops, Finally It Is Cleaned By An Electrofilter. The Cleaned Gas Is Passed Through The Waste Gas Ventilator Into The Open Air. In1981 A Cleaning Line Was Connected To The Technology, Where The Arsenic Content Of The Acid Is Removed In The Form Of Arsenic-sulphide. The Arsenic-sulphide Is Removed In A Pressure-filter With The Help Of Filtering Subsidiary Material. Thus The Phosphoric Acid Is Suitable For Application In The Food Industry.

Major Equipment:

Phosphorus Store With Pumps 2x 370 M3 Transmission Phosphorus Tanks 3x10 M3 Hot Water Tanks With Pumps Air Compressor 2400 M3/h Phosphorus Burners Combustion And Hydration (absorption) Tower Venturi Scrubber Elektrostatic Precipitator Waste Gas Ventilator Acid Circulating/diluting Tank With Circulation Acid Pumps Acid Coolers Phosphoric Acid Storage 40-100-500 M3 Cooling Water Circulation Equipment With Pumps Reactors Niagara Pressure Leaf Filters Acid Pumps

Additional Info:

Typical Operating Requirements Per Metric Ton Of 75% H3po4 Phosphorus 0.24 Tons Process Water 0.53 Tons Electric Power 130 Kwh Steam 2.25 Gj Cooling Water 5.4 Tons

Pvc Plant

Capacity: 180,000 T/y Plant Is (3) Independent, Nearly Identical Trains With Capacity Of 60,000 T/y Each.

Technology: S-vinofley (basf) Suspension Polymerization

Year Built: 1970

Year Shut: 2005

Product Info:

In The S-vinoflex Plant Of Basf (ludwigshafen, Bldg.no.f410) Polyvinylchloride (pvc, Trade Mark: Solvin) Is Produced From Vinylchloride (vc) Which Is Produced In The Vinylchloride Plant (bldg.no.c410). The Pvc Process Is Based On Basf Technology Using Suspension Polymerization. Pvc Is Produced In Two Steps: A. Batch Wise Polymerization Including Discontinuous Degassing (sequence Controlled By Dcs). B. Continuous Processing Of The Suspension Of The Final Product. The Production Unit Consists Of 18 Polymerization Reactors (steel/glass Lined And Stainless Steel Elctropolished) Arranged In 3 Polymerization Lines. The Reactors Have Volumes Of 36 And 44 M. They Are Equipped With Top Driven Impellers (pole Changing, 55 And 110 Rpm) As Well As 2 Baffles. Each Poly Line Is Followed By A Processing Line. Thus It Is Possible To Produce 3 Different Grades In Parallel. The Poly Reactors Are Charged With Demineralised Water And, Depending On The Type, The Necessary Additives. The Starting Matter Required For Forming Radicals Is Added By Hand Through The Manhole. After Closing The Reactor And Evacuation/nitrogen Purging The Metered Quantity Of Vc Is Filled In. Polymerization Starts At An Agitator Speed Of 110 Rpm By Injecting Life Steam. The Temperature Is Chosen Between 35 80 Depending On The K-value Of The Product. The Polymersation Is An Extothermic Reaction (heat Of Polymerization 1695 Kj/kg) Thus Excess Heat Has To Be Removed During The Whole Poly Time. The Heat Removal Is Maintained Through The Reactor Walls (basic Amount) And The Condenser On Top Of The Reactors (peak Quantities). Depending On The Pressure The Nitrogene Flow To The Condensers Is Regulated And Thus The Active Heat Transfer Area In The Condensers Is Varied. In That Way A Constant Temperature Profile Is Maintained During The Polymerization. Corresponding To The Poly Temperature The Inside Pressure Of The Reactors Is Between 5 And 15 Bar. The Duration Of The Polymerization Is 4 6 Hrs. After The Polymerization Is Finished The Unconsumed Monomer Vc Is Recovered. This Vc Is Degassed In Two Separate Units. For Degassing Under Pressure A Set Of Compressors Is Run In Each Line. The Secondary Degassing Under Vacuum Is Done In A Common Unit For All Lines. The Recovered Vc Is Compressed And Condensed. It Is Available For Further Use. Samples Are Taken From The Suspension To Determine The Particle Size Distribution. Then The Suspension Is Transferred To The Holding Tanks. Up To Here The Production Is Batchwise. The Following Processing And Drying Is Continuous. Each Poly Line Is Followed By A Processing/drying Line Consisting Of 2 Centrifuges, 2 Vapor Strippers, 1 Pneumatic Conveyor Dryer, 2 Vibrated Screens, 1 Fluidized Bed, And 1 Blow Tank. In The First Step The Main Quantity Of Process Water Is Separated In The Centrifuges (sharpless Decanter). The Suspension Is Pumped From The Agitated And Vented Holding Tank To A Feed Tank. By Overflow The Two Centrifuges Are Fed. The Quantity Is Adjusted By Valve Operation Governed By The Amperage Of The Centrifuges. The Excess Volume Of The Suspension Is Fed Back To The Holding Tank. After Centrifuging The Suspension Has Still 20-30% Residual Humidity. The Removed Process Water Is Collected In A Tank, Passed Through The Effluent Centrifuge And Cooler And Finally Drained To The Effluent System (for Biological Treatment). The Temperature Of The Waste Water Which Should Not Exceed 40c Is Registered. After The Centrifuge The Pvc Is Fed By Means Of A Dosing Screw Into A Stripper. In A Counter Flow Operation With Steam (4 Bar) Resp. Steam/air Mixture The Residual Monomer Is Removed (set Point: <1 Ppm Vc). Via Discharge And Double Paddle Screw And Rotary Vane Feeder The Pvc Is Charged Into The Pneumatic Conveyor Dryer. The Conveying Air Is Filtered And Then Heated By Condensate And Steam (4 And 16 Bar). In The Dryer The Superficial As Well As The Internal Water Of The Product Is Reduced To 4 To 8% Moisture Content. In 4 Dry-stage Cyclones For Each Line The Product Is Separated From The Air. In 2 Parallel Vibrating Screens The Coarse Particles >400 Pm Are Separated Supported By Rubber Balls And Heated Air To Prevent Clogging Of The Sieve. This Airflow Too Is Vented By The Vent Fan Of The Dryer. The Coarse Product Is Collected And After Filling Into Big Bags Ready For Shipping. The Fines (standard Product <400 Pm) Are Conveyed Via Holding Bin And Star Feeder In The Fluidized Bed Dryer. The Air Flow In Maintained By A Rotary Blower (positive Displacement) And Heated By Steam (4 Bar). The Residual Humidity Predominantly From Inside The Pvc Particles Is Removed. The Product Is Separated From The Vent Air In A Cyclone. After A Certain Dwell Time The Dry Product (set Point <03% Residual Humidity) Is Conveyed Over A Baffle Plate Into A Bunker. Finally The Product Is Batch Wise Charged Into A Blow Tank And Pneumatically Conveyed Into The Silos. The Vent Air From Pneumatic Conveyor Dryers, Screens, And Fluidized Bed Dryers Is Treated In A Wet Scrubber To Remove Residual Fine Pvc Particles. After Filtration The Waste Water Is Drained. Power Supply Frequency-50hz Voltage-(230), 500, 6000 V Off Gas Treatment: No Incineration, But Absorption In Solvent. Emission To Air: Vcm 40 G/t Pvc Effluent Discharge To Biotreatment 4,9 M/t Vcm Cod Untreated 0,03 Kg/m Vcm In Effluent 0,1 Mg/kg Pvc Quality: Vcm Content 0,5 Mg/kg Pvc Bulk Density 500-600 G/l Moisture 0,2 Wt % 63u 90-96 Wt % 250u Pass 97-100 Wt% Av.ps 125 U Fish Eyes Film Grade K-value 57-68 (50-71)

Major Equipment:

Reactors/autoclaves: 12 X 44 M Reflux Condenser: On Each Reactor/autoclave, With Cooling Water (no Chilled Water)

Additional Info:

Consumption Ratio: Vcm 1003 Kg/ton Of Pvc Steam 1000 Kg/ton Of Pvc Power 145 Kwh/ton Of Pvc Water Demin 1.8 M/ton Of Pvc Cooling Water 65 10m/ton Of Pvc Off Gas Treatment: No Incineration, But Absorption In Solvent. Emission To Air: Vcm 40 G/t Pvc Effluent Discharge To Biotreatment 4,9 M/t Vcm Cod Untreated 0,03 Kg/m Vcm In Effluent 0,1 Mg/kg Pvc Quality: Vcm Content 0,5 Mg/kg Pvc Bulk Density 500-600 G/l Moisture 0,2 Wt % 63u 90-96 Wt % 250u Pass 97-100 Wt% Av.ps 125 U Fish Eyes Film Grade K-value 57-68 (50-71)

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)



Company Contact:

No member photo
Contact Name: Sidra (Miss)
Company Name: Sidra Commercial Trading Company
Email: Email
Tel: 92-0300-4705383
Fax: 92-42-6558083
Street Address: P.O.BOX 2504,
G.P.O., Lahore - 54000, Pakistan
Member name: Sidracommercialtradingcom
Country: Pakistan-PK Pakistan
Member Since: 26 October 2007
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