Plant is designed to purify, condense, liquefy, and store raw carbon dioxide gas (CO₂) at the site. Production capacity is 15 tons/hour design, possible up to 16,5-17 tons/hour. Purity is 99.995%

Main process steps:

1. Washing of raw CO₂ gas
2. Compression of CO₂ gas(centrifugal compressor and screw compressor – 2 stages)
3. Purification and dehydration of CO₂ gas
4. Liquefaction of CO₂ gas(using a condenser operating with ammonia)
5. Distillation of liquid CO₂
6. Storage and loading stations

The crude oil plant is designed in such a way that it can process a wide range of crude oils into products that meet specifications according to the raw material and market situation.

Range of products of the plant

Product

Plant subsection

Head gas (distillation gas), raw gasoline

Crude oil column/debutaner

LPG (C3, C4)

Entbutaner

gas gasoline, light gasoline, light naphtha,

Naphtha Shards

Heavy naphtha, kerosene, medium oil, heavy medium oil, atm. Residue

• Crude oil column

Light Vacuum Gas Oil (LVGO), Medium Vacuum Gas Oil (MVGO), Heavy Vacuum Gas Oil (SVGO), Vacuum Residue

Vacuum column

The products obtained in the plant are pumped to the tank farm for intermediate and finished products or to other plants of the plant for further processing. The quantities produced depend on the composition of the crude oil and the operating conditions. In addition, excess medium-pressure steam (MD steam) is released into the plant network. MD steam is steam with a pressure of 20.0 bar.

The plant is supplied with crude oil. After preheating in several heat exchangers, desalination takes place. By adding water, the corrosive chloride-containing salt components of the crude oil are extracted with water in addition to the salts. In other heat exchangers and in the crude oil furnace, the crude oil receives the temperature of up to 360 °C required for distillative separation.

During the subsequent distillation in the crude oil column, the desired fractions are subtracted and fed into downstream columns and strippers for processing and further separation.

There, the extracted heavy naphtha, kerosene, medium oil and heavy medium oil are stripped to separate the more boiling components. The products heavy naphtha, kerosene, medium oil and heavy medium oil are fed into the tank farm for finished and intermediate products or into other plants of the plant for further processing. The medium oil is fed into the middle distillate thydation, Building 062. Here, the medium oil is hydrogenated together with light vacuum gas oil from the vacuum distillation column to reduce the sulphur content. After hydrogenation and stripping, the middle distillate (component of diesel fuel) is fed into the tank farm.

The head gas of the crude oil column is compressed in compressors and then cooled. Condensates produced in the process are fed into the debutaner. It distillatively separates the product used into a C3/C4 mixture (liquefied petroleum gas) and a swamp product. The latter is fed into the naphtha splinter for further separation into gasoline, light gasoline and light naphtha. Non-condensed gases are released as distillation gas for gas post-processing.

Atmospheric residue is removed from the sump of the crude oil column and, after cooling to approx. 320 °C, is conveyed through a heat exchanger into the vacuum furnace. Here, the energy required for separation in the vacuum column is supplied to the atmospheric residue. The two-phase flow from the vacuum furnace is fed into the vacuum column where it is distillatively separated.

The head gases from the vacuum column are sucked in in a three-stage vacuum generation system and the non-condensable parts are fed to the head gas compression of the crude oil column.

Light, medium and heavy vacuum gas oil (LVGO, MVGO and SVGO) are obtained from the vacuum column as side products; vacuum residue is withdrawn from the sump. MVGO and SVGO are further processed into other plants at the plant and LVGO is desulphurised as described with the medium oil from the atmospheric part according to specification.

In the Visbreaker, the residues from the VD‐500 are thermally cracked. In exceptional cases, the atmospheric residue of the D‐500 can also be used. The VBU consists of two strings, each capable of processing 80 t/h of vacuum residue.

In the VBU, long-chain hydrocarbons are broken up by the action of temperatures in the range of 400 °C to 500 °C. As a result, the residue of the VD‐500 mixing components is recovered in the boiling range below 400 °C. Since the splitting reaction that takes place results in a reduction in the viscosity of the residue used, the system is called a "visbreaker" or viscosity breaker.

The vacuum residue used is heated to a maximum of 450 °C in the L2‐A and L2‐B furnaces with the heating agent 8 bar heating gas (the ignition burner is operated with natural gas). At a pressure of 10 bar, the residue in the so-called soaker is exposed to the reaction conditions for a defined period of time.

The reaction product is then expanded, cooled to below 400 °C and further processed to separate the hydrocarbons formed in atmospheric distillation N‐1 and vacuum distillation N‐2A. In the N‐1, the head product is a cracker gas is obtained, which is directed to the head gas of the D‐500. The upper side fraction is a crude cracker gasoline that is fed to the HDS (1200) kerosene desulphurization plant. A cracking gas oil (KGO) is produced as the lower side fraction, which is piped to the MDH. The swamp product of N‐1 is directed to N‐2A.

At a pressure of 10 mbar to 20 mbar, a cracking light distillate (KLD) is extracted from the N‐2A as a head product, which is fed to the T124 tank. A cracker vacuum distillate (KVD) is obtained as a side fraction, which is fed to tank T121 (additional component to HCU's application product) and/or as a flux agent for the cold residue to the input tank O‐38 for flux oil in the VBU.

The swamp product of N‐2A is formed, the so‐called visbreaker residue, which is cooled and used as an input product for oil gasification, as a sales product or as a mixed component for heavy heating oil. In the latter case, the Visbreaker residue is mixed with a flux agent KGO, KVD or a flux component from tank T55 or a mix of all of the above. This causes a further reduction in viscosity, so that the residue remains liquid even at temperatures below 100 °C.

The plant has a production capacity of 35 000 tons Phthalic Anhydride (PA) per year on a continuous seven days per week basis.

Raw material orthoxylene (o-Xylene, 1,2-dimethylbenzene) is mainly imported by ship to the tank storage at the jetty. Orthoxylene is pumped by pipeline to the site. The reaction is strongly exothermic and the reaction heat is recovered generating steam in an integrated WHB (Waste Heat Boiler). The tail gases from the processes are incinerated in a catalytic incinerator (Catox) where complete combustion takes place leaving only effluent CO2 and water.

The exothermic reaction develops substantial amounts of excess heat. Surplus heat is cooled off with a liquidized salt mix made up by potassium nitrate and sodium nitrate, which in turn is cooled with water and hence no thermal oils is present in the WHB. Reaction occurs in potentially explosive areas in all process steps.

The plant handles hydrocarbons at elevated temperatures and pressures and has the potential for pool fires, explosion and gas jet fires. There is however not sufficient quantity of light hydrocarbons to give rise to the inherent potential for a vapor cloud explosions. There is generally a good standard of remote isolation valves provided in the raw material supply as well as in process units.

Formaldehyde Plant (Reichhold Design using metal oxide catalyst).

Available for operation in-place (Allentown, PA USA) or relocation globally.

Process Description:

The Formaldehyde plant (P501) is designed to produce formaldehyde by the catalytic conversion of methanol and oxygen controlled recycle gas. Formaldehyde is produced by the direct oxidation of methanol from the Methanol Storage Tank and Piping (P502). Emissions from the methanol storage tank and piping, during truck unloading, are captured by the Methanol Vapor Recovery System (C502). Emissions not captured by the vapor recovery system are fugitive emissions (Z550). The catalytic conversion reaction is carried out with the aid of a catalyst, which consists of molybdenum and iron oxides. The process gas is passed through the catalyst, contained in a multiple tube unit called the converter. It both heats the air-methanol mixture to the reaction temperature in the upper part of the catalyst tube and removes the heat of the reaction in the lower part. The formalin gases, which leave the converter, are cooled in an after-cooler where low-pressure steam is produced. The cooled gases enter an absorber where the formaldehyde is absorbed into water to produce up to a 53.0% Formaldehyde solution. In order to reach desired production rates, it is necessary to operate the plant under recycle conditions. Part of the gas mixture leaving the absorber stack is returned to a recycle tank where it is mixed with fresh air, at a controlled rate, to maintain oxygen content of 10 — 10.5% by volume. The remaining unused gas mixture goes to the Natural Gas fired (FML541) Catalytic Oxidizer (C501) where it is preheated and oxidized, in the presence of a catalyst, to harmless byproducts. These byproducts are released to the atmosphere through the Formaldehyde Incinerator Stack (5501).

Notes: Shut down in 2024. Documentation is incomplete.

112 MW Combined cycle and Cogeneration

1 on 1 power train configuration

1 Gas turbine, 1 Steam turbine, 1 HRSG

2 x GSUT

1 x 115 kV / 23 kV transformer

1 x 115 kV/ 6.9 kV Aux transformer

2 x 6.9 kV/ 400V Aux transformer

Demin + RO water treatment

Power dispatch:

• 24 x 7 Baseload Operation
• 115 kV to EGAT and 4 Industrial Users
• 22 kV to 7 Industrial Users

Steam delivery: 20 ton/ hr, 1.3 barg superheated steam to an Industrial User

Gas Turbine (1 unit)

GE MS6001FA w/ DLN2.6 combustion NG fired OpFlex Auto Tune, speed 5,200 rpm, Output 64.0 MW

Generator (1 unit)

GE 7A6 Air cooled generator, Output 83.6 MVA, Armature volts 11.5 kV, 50 Hz, 2 Poles, 3 phase , Speed 3000 rpm

Major Upgrades & Changes

• Upgraded GTG combustion system from DLN2.0 to DLN2.6
• Upgraded GTG and STG GE control system from Mark V to Mark VIe
• Upgraded GT and ST GE generator exciter control system from EX2000 to EX2100e
• Replace GT rotor (new 6FA.01 compressor married with 6FA.01 refurbished turbine rotor)
• Upgraded GT DLN2.6 combustion system to OpFlex Auto Tune in order to operate with new fuel Wobbe Index range

NEW From Cancelled Project!

Design Capacity:

• Sodium Metabisulfite Food Grade 15,000 MT/year
• Magnesium sulfate heptahydrate (MgSO4•7H2O) ≥95% purity ~1800 MT/year by product

Production Process Description

Process Characteristics

Using “excess air + solid sulfur” incineration process, the obtained sulfur dioxide gas concentration is about 12%~15%. Control the reasonable sulfur incineration temperature to ensure complete combustion of sulfur.

Using our proprietary technology for solid sulfur feed system, so that the sulfur incinerator temperature is stable, the sublimation sulfur is less in the flue gas. The plant is designed with negative pressure air blowing system, which has good operating environment, and sulfur yield is high.

Using automatic continuous discharging centrifuge, which is a continuous automatic operation, is safe and reliable, saving manpower.

The low concentration sulfuric acid waste liquid is used for production of Magnesium Sulfate products, so the plant has no waste liquid effluent discharge.

Perfect design of exhaust gas treatment. In the waste gas, SO2 concentration is less than 50mg/Nm3（SO2≤50mg/Nm3）.

Process Description

Air Compression and purification section

The air is filtration by air filter, and then is feed into air compressor, the air is compressed by air compressor and is feed into sulfur incinerator, the air burning with solid sulfur and obtain sulfur dioxide gas (SO2).

Sulfur incineration section

The solid sulfur is fed into sulfur incinerator by solid sulfur feeder, the solid sulfur is mixed with air and burning in the sulfur incinerator, and obtain sulfur dioxide gas (SO2), and release a lot of heat at the same time.

S + O2 = SO2 + Q

A part of sulfur dioxide reaction with oxygen and get sulfur trioxide.

2SO2 + O2 = 2SO3 -Q

Sulfur dioxide gas purification section

After burning, the hot flue gas is enter the flue gas buffer tank, and then is enter the cooling pipe, using circulating water to cooling the flue gas, the flue gas is cooling to 50~60℃ and then is feed into flue gas scrubber, through bubble washing to remove SO3 of flue gas. After the flue gas scrubber, using stage of separator to separation and removal of entrained droplets of flue gas. The scrubbing obtained dilute sulfuric acid is collected and used to produce Magnesium Sulfate by-product. The purified sulfur dioxide gas is sent (through pipeline) to sodium Metabisulfite synthesis section.

SO3 + H2O = H2SO4 

Soda ash solution batching and sodium Metabisulfite synthesis section

Put solid soda ash (Na2CO3) into the soda ash batching kettle of sodium Metabisulfite synthesis section, add water and mother liquor (the filter liquor) of sodium Metabisulfite centrifuge and mixed into suspension, and then pumping the suspension into sodium Metabisulfite synthesis reactors, and feeds clean sulfur dioxide gas successively into the first stage, second stage and third stage synthesis reactors, after synthesis reaction, get sodium Metabisulfite suspension in the first stage synthesis reactor. The reaction tail gas is discharged from the third stage synthesis reactor, and is lead into the scrubbing tower for treatment.

Na2CO3 + 2SO2 = Na2S2O5 + CO2 

Centrifuge & drying process

The Sodium Metabisulfite suspension is discharged from the first stage synthesis reactor and stored into slurry tank, and then from the slurry tank feed into centrifugal, through centrifugal separation and get wet solid Sodium Metabisulfite, which is content 3~5% water, feed the wet Sodium Metabisulfite into hot air dryer (airflow drier), and through cyclone separators, get Sodium Metabisulfite products. The filtrate is collected into the acid mother liquor tank, reused for soda ash solution batching kettle. The drying use hot air comes from the waste heat recovery jacket of sulfur incinerator. After drying, the tail gas is send into tail gas absorption column.

Tail gas treatment section

The tail gas countercurrent contact with soda ash solution, the sulfur dioxide gas in the tail gas was absorbed by soda ash solution, the tail gas was cleaned and emptying **(SO2≤50mg/Nm3)**. The absorption solution reused for soda ash solution batching.

Liquid waste treatment section

In the flue gas scrubber of sulfite dioxide purification section, the sulfite trioxide is absorbed by water and get concentration of 50~60% dilute sulfuric acid liquid waste, which is used to produce Magnesium sulfate heptahydrate by-products.

MgO + H2SO4 + 6H2O = MgSO4·7H2O

Solid Separations:

Saccharified mash is then sent to the sugar clarification system. Paddle screens and centrifuges are used to filter out spent grain solids and wash sugar from the spent grains in a 3-stage counter current wash. Liquid sugar is pumped to 121,000-gallon SS storage tanks and solids are sent to rotary drum dyer for final drying.

Fermentation begins with bacterial propagation through a sanitary seed train consisting of two 44 gallon seed tanks, two 2000 gallon seed tanks and finally a 28,500 gallon seed tank before being mixed with liquid sugar in four 285,000 gallon fermenters. During fermentation broth is continuously stripped from the fermenters and passed through an Alfa Laval ultra filtration skid separating the biologics from the fermentation broth which are sent back to fermenter. Filtrate is pumped to the distillation unit where Butanol and Acetone are distilled off through a series of distillation columns and passed through a 3-effect evaporation system before heading to final product storage

Other notable features include an on-site wastewater treatment facility rated for 157,000 gallons per day and full product testing and microbiological laboratory.

Other potential uses included: high protein feed products, renewable biochemicals, single cell proteins, sustainable aviation fuel, food grade organic acids and industrial/GNS alcohols.

Combined heat and power cogeneration system, it was built in 2000 and started up in 2001, it was shutdown in early 2016, the engines have operated for 36,300 hours and 34,000 hours

6.72 Megawatt gas fired combined heat and power cogeneration system, system includes:

5000 kg/hr Cochran single pass waste heat recovery boiler, inlet temperature 160 degrees C, outlet 186 degrees C (saturated steam @ 10.5 barg), heat transfer duty 2934 +- 15%, specific gravity/density 0.95 kg/m3, specific heat 1.00 kCal/kg.C, with economiser

2 x 3360.8 Kw (4201 kVA) gas engine driven electrical generator, engine manufactured by Waukesha (Dresser), model #16VAT27GL, serial #C-80859/1 & C-80859/2, SAA #2000-168, natural gas fired, continuous, comp ratio 9/1, min.WKI 91, ignition timing (BTDC) 11-02, service 4650 HP (3469 Kw), altitude limit 500 feet (152 meter), governed speed 1000 rpm, 0.80mm valve intake & exhaust clearance, firing order 1R-1L-4R-4L-7R-7L-6R-6L-8R-8L-5R-5L-2R-2L-3R-3L, AC generator (alternator) manufactured by Leroy Somer, type LSA-56-BM65-6P, serial #167056-2, IP 23, 3360.8 Kw, 4201 kVA power rating, 11000 volt, 220.5 Amp, 3 phase, 50 Hz, 1000 rpm, excitation AREP, all mounted on a carbon steel skid

oil lubrication, cooling water system, MCC control panels, some ductwork,

• Products Produced:  Heavy Multi Layered Stock – High Quality Specialty Grades, Whites and Colors

• Capacity:  Capable of running 900 ft. per min.

• 100 lbs per cylinder (3,000 sq.ft.)

• 100 tpd of heavyweight multi layered board

• Max Speed:  300 FPM

• Cylinders: (5) Vacuum Cylinders - 42” O.D. Cylinders w/20” O.D. Couch Rolls (2) Spare Cylinders

• Presses: (3) Wet Presses (2400 PLI) total • (1) LG Industries Suction Press with 24” O.D. Rolls • (2) Plain Presses with Blind Drilled Roll

• Dryers: (54) 48” X 120” Face Rice Barton Dryer Section (non-code) • Majority of Dryers are Stacked in a Vertical 4 Roll Stack • 65 Cans in a Stack Section • Conventional Dryer - nest-felted

• Misc.:   (2) Multi-Roll Farrel Calendar Stacks- Wet and Dry including Water Boxes

• Wesport Tension System

• Inclined Size Press

• Accuray Color and Thickness Scanner

• A&F Horizontal Track Reel for 60” O.D. Rolls with Extra Spools

• Cameron Two Drum Slitter Rewinder for 60” O.D. Rolls

• Process Computer- measuring machine direction/ cross direction variables

PET Cutter System consisting of:

(4) Rieter (Maag) Underwater strand pelletizers ( M-USG 900 V)

• vertical design (providing space savings and easy access to the cutter head)
• 316 SS contact

Each System is Designed to Process the following PET (bottle grade):

• Viscosity: 200-500 Pas viscosity.

• Pellet dimension of (2.1x2.8)mm x 2.8 mm lg. +/- 10%

• No. of Strands: 90

• Capacity:

  Minimum: 3200 kg/h

  Nominal: 5000 kg/h

  Maximum: 6900 kg/h

• Melt density 1.18 g/cm3,

• Solid density 1.34 g/cm3.

• Melt temperature 285-290°C.

• Cooling length before cut: 1.5m

• Max strand speed of 220 m/min (minimum speed 100 m/min)

Each System is Equipped with:

• Die plate design (pn# 10295462) 5.5 mm hole diameter.
• Quick change cutting head with a diameter of 162.5 mm, 30 teeth, with a 2° helix angle and # 2 tooth profile.
• Cutter main drive system is direct drive, with a three phase AC motor, rated for 37 kW.
• Feed rolls -timed, with a belt drive, driven by a three phase AC motor, rated for 5.5 kW.
• The machine is supplied with an operator control panel.

Utilities Required (for each system):

• Compressed air-4-6 bar. (dry and oil free)
• Electrical-400 volt 3 phase.

The polymerization plant (PPU) has a capacity of 225,000 tons per year and is a Unipol technology plant, with two gas phase reactors, so can produce homopolymers, random copolymers and impact copolymers.

The extruder is a Coperion ZSK300, with a 5.5MW Loher main motor and associated transformer. The extruder also has a Maag polymer pump, Gottfert on-line rheometer, and electric hot oil systems for the die plate and barrel.

There are six, 280t capacity pellet silos downstream of the extruder, three with air spinner container loading spouts.

There are also another 280t silo, one 140t silo and three 70t silos.

There are also six air blowers for the dilute phase conveying of the pellets from the extruder to the silos or between silos.

There are also two Atlas Copco GA132 compressors to drive the air spinners and silo purging.

There is also a Refinery Grade Propylene (RGP) purification system which includes a Propylene Treatment Plant (PTP) which contains alumina bed driers, a de-ethaniser column, and a de-butaniser column. The PTP supplies treated RGP to a propane-propylene splitter (PPS). The PPS is a heat pump design for minimum utilities demand.

The PTP has a RGP feed capacity of 26 t/hr, whilst the PPS has an RGP feed capacity of 16 t/hr at 70% propylene to produce 11 t/hr polymer grade propylene (PGP) at 98% recovery and 99.0% purity.

The PPU, extruder and PPS were commissioned in September 1991.

The PTP was commissioned in April 1995.

There is a fibre glass cooling water tower comprised of four 15MW cells and three 450kW water circulation pumps. This was commissioned in October 2010.

Plant Capacity: 150,000 MTPY

Commissioned: February 2001

Shut Down: January 2013

Associated with the 4000,000 MTPY VCM Plant -IPP Stock #600847

This 150 kmta PVC Plant uses licensed technology from Ineos Vinyl.  The process employs “closed-lid” and VCM stripping technology.  The reactors are designed to remain closed in between batches and unreacted VCM is removed with a stripping column for recycle.

Engineering was by Technip and the plant started up in 2001.  The last major turnaround was in September, 2012 and the plant was shut down in December, 2012.

The plant produces K57, K66-R-G-F, and K70 grades

Complete EDC/VCM plant available as well.

All field instrumentation is electronic.  Redundant Micromotion flow meters are used for critical fluid measurements, even on lines up to 6” diameter.

Utility systems include instrument air compressors (3), nitrogen booster compressor, major electrical transformers (11), thermal oxidizers (2), waste water treatment facility, and fire water pumps (3).

70 TPD PET - SSP Plant It is a facility that manufactures high-IV PET chips suitable for various bottle production by reacting low-IV PET chips produced in a melt polymerization process in a solid state to have high crystallinity and removing moisture and acetaldehyde.

3.2 MW Gas Fired Co-Generation combined heat and power plant.  With (4) 800 KW Caterpillar natural gas-fired, after-cooled, lean burn 3516 90 LE reciprocating engine generator sets each rated at 820kWe output at 480V at the generator terminals.

This chp plant is in excellent condition. All four generators operate at a base load of 700KW, though are capable and have run at their 800KW nameplate. All units are operated on a 24/7 basis with very little downtime for anything other than scheduled maintenance.

(3) Plastic Recycle Systems Available

• Materials: PET, PS, LDPE, LLDPE, HDPE, PP, Other Polymers

• Feedstock Forms: Flake, Regrind, Shredded Film, Densified Forms

• Process:

• Shredding

• Grinding

• Washing

• Drying

• Extrusion

• Pelletization

• Power Supply:

• 380 VAC/3PH/50Hz

• 480 VAC/3PH/60Hz

  (2) 8" lines consisting of:

• 8” Single Screw Extruder

• 10 Inch Slide Plate Screen Changer,

• Two (2) High Force Compactor Densifier Extruders,

• Underwater Pelletizer And

• Recycle, Cleaning , Washing & Drying System

  Estimated Rate for the (2) Lines: 1,000 - 5,000 lbs/hour (material Dependant)

  (1) 10" line consisting of:

• 10” Single Screw Extruder1 2 Inch Slide Plate Screen Changer,

• Two (2) High Force Compactor Densifier Extruder,

• Underwater Pelletizer and

• Recycle, Cleaning, Washing & Drying System

  Estimated Rate for the line: 1,000 - 7,000 lbs/hour (material Dependant)

  (1) 160mm Compounding Line Also Available

• Estimated rate: 1,000-5,000 kgs/hr

• All Necessary Feedstock Forms

• Materials: PA, PS, PE, PP, PET and other materials

• Process: Extrustion - Devolitilizing - Pelletizing

• Available Power Supply: 480 VAC/3PH/60Hz

• 160mm Twin Screw

• High Capacity Devolatilizing Extruder

• Three Zone Vacuum Relief Sections

• 44:1 L/D With 2000 HP AC Drive

• 450MM Dual Bolt Screen Changer

• Underwater Pelletizer

5,250 KW, 50 Cycle, Escher Wyss steam turbine generator set, with extraction.

Turbine:

• Escher Wyss

• Type REA 1600

• Designed for 5,240 KW

• Rpm: 6,600

• Inlet Pressure: 36 Kp/SqCm @ 410 degrees C

• Extraction 1 - non controlled 2800 Kg/H

• Extraction 2 - controlled 27,000 Kg/H, pressure 11-14 Kp/SqCm

Generator:

• Type 14S250

• 6600 KVA

• COS Phi 0.8

• Voltage: 11 KV, 50 Hz

"Green Energy" CHP Steam Power Plant Uses Alternative Methane-based Natural Gas Biofuels Like Biogas & Landfill Gas Also Burns Natural Gas Gas Fired Power Generation of 10 Megawatts (MW)

This biogas cogen plant is the largest of the smaller scale combined heat and power systems IPP has available for sale.  This 10 megawatt (10,200 kw) thermal power station uses Rankine cycle process to produce energy that could supply electricity to ~2,000 - 6,000 residential customers* and includes:

• Deltak gas fired boiler - burns landfill, bio-gas, methane & natural gas

• steam powered turbine

• 10 MW electric power generator by Ideal Electric Co.

• Complete control room

• Complete documentation available including manuals, drawings, inspection and operational data reports

• Estimate based on average annual electricity consumption figures published by the US Energy Information Administration with a peak load factor of 2.0.

Built in 1996-1998, this steam power plant started operating in 1998. The previous use was for combined heat and power generation from biogas feed sourced from a landfill.  The prior owner shut this chp plant down when its bio gas supply increased dramatically and it decided to replace the gas based power plant with a larger capacity landfill gas power plant. Contact IPP for operational data, documentation, complete equipment list

Click Here to View this Video on Youtube

3100 Gallon (12 M3), 25 bar Buss Loop Hydrogenation Reactor System

12 m³ 1.4439 SS Hydrogenation Reactor system, BUSS LOOP reactor, -1/25 bar@ 200 ° C, max operating pressure 16 bar@ 105°C . Gebr. Quast/Gothe KG, SN # 2603 total volume 13.143 l. System includes a 114 m² 1.4439 SS heat exchanger , -1/25 bar internal, jkt -1/6 bar @ 200°C, manuf. Gessner Apparatebau GmbH /Germany, volume 870 l pipes, 1.139 l shell, dia 700 mm, 5 m length , connected to AW 413 double jacket pipe, 1.4571 SS 10 bar@ 120°C, 5 l both sides; a 30,6 m² 1.4571 SS Vicarb plate heat exchanger , 8 bar@110°C, 70 l each side, SN # D 3660; and a 995 l 1.4571 SS pressure tank -1/26 bar @ 200°C, used as Hydrogen buffer tank, manufactured By Weisstaler, SN 38644.

Process Description

The natural gas feedstock is first preheated and de‐sulphurized (382°C/25bar), absorption is carried out over Zinc oxide granules, and then reacted with steam to produce a reformed gas/steam mixture at 860°C temperature and 21 bar pressure.

The reforming reaction is basically the reaction between a hydrocarbon and steam to produce carbon  monoxide and hydrogen. In the presence of excess steam these basic products are modified to produce quantities of carbon dioxide and methane, giving a reformed gas consisting of methane, carbon  dioxide, carbon monoxide and hydrogen.

The reformed gas/steam mixture is then cooled, separated from process condensate and passed into the make‐up gas compressor where the gas is compressed (36°C /17bar) to a high pressure (113°C/49bar)  to be injected into the methanol synthesis loop.

With Carbon Dioxide Additions, the external supply of carbon dioxide is mixed with the high pressure gases from the make‐up gas compressor before injection into the synthesis loop.

Synthesis gases are circulated at high flow rates through a methanol synthesis catalyst held at moderate temperatures (135°C/52bar) where hydrogen reacts with carbon monoxide and carbon dioxide to produce gaseous methanol.

Cooling of the circulated gas condenses crude liquid methanol which is bled from the system and sent to crude storage. The remaining gases are then replenished with make‐up gas before entering the synthesis gas circulator to pass round the loop again.

Inert gases (methane) present in the reformed gas accumulate in the loop and are bled from the system to be burnt as fuel.

The crude methanol contains small concentrations of other organic chemicals synthesized in the methanol converter.

The crude product is then taken from storage, fractionated in two distillation columns and the pure methanol passed to purified product storage tanks.

This all stainless steel, dual-column distillation system was designed by Sabic to separate and purify up to 18 mt/hr of toluene from a complex mixture including isomers, Bisphenol-A, and water.  The system consists of a feed tank, vaporizer, pre-flash vessel, upper column, lower column, two column reboilers, and two overhead condensers with vacuum jets.

Subsystem from Complete Bisphenol A (BPA) Plant, IPP Stock #600363

190 Acre API Manufacturing Plant Complex Grimsby, England, UK

This world-class, fully integrated API manufacturing site, formerly operated by Novartis, includes over 1,200m3 of total reactor vessel capacity across three distinct production buildings, available for sale or lease as a whole site or individual buildings for operation in-place. The facility could be utilized for pharmaceutical and animal health API manufacturing or repurposed for specialty/fine chemical manufacturing, flavors and fragrances, or agrochemicals.

VIDEO: https://www.youtube.com/watch?v=AUWUHnAyWos&list=PLRlhdb05DXKR4eyHsLOkB6NzTyh2R4YCE

The site is located adjacent to the river Humber and between the Immingham and Grimsby port facilities, less than 5 minutes from downtown Grimsby, 25 minutes from Humberside Airport, 2.5 hours from Manchester Airport, 3.5 hours from London Heathrow.

Inside the fenceline is approximately 100 acres, with significant development land and infrastructure available inside the fence. There is an additional approximately 90 acres of agricultural land outside the fenceline.

Facility has the capabilities to perform various chemical synthesis, including hydrogenation, Grignard/Friedel-Crafts Reactions, Azide, and Tin Chemistries.

Building 110: Multi-product, Multi-purpose facility (ca. 1993)

• Total Reactor Capacity: 140m3
• Hydrogenation, Crystallization, Centrifugation, Nutsche Filters, Short-Path Distillation, Milling/Blending, Solvent Recovery
• Overhead manifolds and flex piping for production flexibility
• Glass Lined, Hastelloy, and Stainless Steel Equipment

Building 120: Mixed High Volume, Multi-Purpose Facility (ca. 1994/2007)

• Total Reactor Capacity: ~450m3
• 3 dedicated, 3 multi-purpose lines -Hydrogenation, Crystallization, Sublimation, Nutsche Filters, Paddle Dryers, Milling/Blending, Solvent Recovery
• Glass Lined, Hastelloy, and Stainless Steel Equipment

Building 150: High Volume, Multi-Product Facility (ca. 2004/2007)

• 4 Dedicated Process Trains
• Total Reactor Capacity: ~550m3
• Hydrogenation, Crystallization, Centrifugation, Drying, Milling/Blending, Solvent Recovery
• Glass Lined, Hastelloy, and Stainless Steel Equipment

Each building has its own dedicated solvent storage and recovery, in-process lab spaces, workshops, and offices.

Site Utilities:

• 2400m3/day Wastewater (Effluent) Treatment Facility
• 2x4.2MVA grid electricity
• 8000m3/h compressed air
• 3000m3/h nitrogen (by pipeline)
• 4x8MW cooling water capacity
• Towns Water potable supply & 400m3/day borehole (well) water for process cooling
• Previously, there was a CHP plant which has been removed and steam boilers will need to be added to support operations.

The production buildings are supported by the following non-production infrastructure:

• Security Facility
• Administrative Office Building
• 4600m2 (50,000ft2) Engineering Workshop and Offices to support major projects, MRO stores, fabrication, equipment and instrument maintenance, etc.
• 3700m2 (40,000ft2) Lab/R&D Space with sample retain storage facility
• Restaurant/Canteen Building
• Medical Facility/Employee Welfare
• Sports Club and Fields
• Capital Good Stores
• Changeover Warehouses

Warehousing:

• Raw Materials & Intermediate Storage: 3000 pallets
• Solvent (flammable & hazardous) Warehouse: 1930 pallets
• Packaging Storage: 500 pallets
• Finished Goods Storage: 750 pallets
• Cold Storage (-8 deg. C): 320 pallets
• Classified area for sampling / repacking of raw materials: 40 pallets
• Waste Storage: 1200 pallets

The facility was not used in production of of plant/animal extracts, fermentation, penicilin, beta-lactams, steroids, hormonals, or cytoxic compounds.

UNUSED state-of-the-art highly flexible small molecule manufacturing facility constructed in 2011The facility is capable of producing around 400kg of API per year, allowing for the production of batches from lead to candidate through to Phase III and commercial launch quantities. This is the potential capacity, in a configuration of people working in 2x7h on 5 days, but this tool could be operated on a 24x7 basis if needed, in which case higher levels of output could be achieved. Production capacity remains dependent on the type and number of synthesis steps.

PILOT PLANT

• Designed to produce GMP active ingredient batches
• 15 reactors (from 100 to 1600 liters) and 5 finishing units (from 10 to 100 kg)

1,170 barrel-per-day Fischer-Tropes GTL Facility targeting the production of higher-value wax products.

The facility consists of the following sections:

• Steam-Methane Reformer: 46.5 MMSCFD Linde-designed Steam-Methane Reformer (SMR) facility including feed preparation, reformer, syngas cooling, steam generation, hydrogen separation, carbon dioxide removal section (amine section), and carbon dioxide compression for recycle. The facility has only 10 years of operation as a HyCO Plant (hydrogen and carbon monoxide production). The SMR was redesigned and upgraded by Linde in 2015 to supply the new GTL facility
• Fischer-Tropes Reaction Section: Two Fischer-Tropes reactors, each with78,000 sq ft shell and tube exchangers with FT catalyst packed inside the tubes. The reactors are 11’ diameter with 32’ long tubes which are rated for 500 psig at 500°F. All of the steam-generation equipment is included for capturing the FT reaction exotherm. All of the equipment was constructed in 2015 and most of the downstream process-contact material of construction is 304L stainless steel.
• Product Fractionation Section: The Fractionation Column is 3’ diameter by 90’ tall and is constructed of 304 stainless steel. It is rated for 50 psig/full vacuum at 650°F. It has four packed sections with four product “take-offs” (overheads, two side-draws, and bottoms). All associated equipment is included such as the feed heater, condenser, two accumulators, and four overheads product/reflux pumps included. This system was manufactured in 2015 and is almost entirely 304 stainless steel construction.
• Wax Upgrade Section: Two 4,000 gallon batch hydrogenation reactor systems; each with 100 gpm feed capabilities. The reactors are rated for 327 psig at 455°F. Two 218 sq ft Short-Path Distillation Units (SPDU) rated for 22 psig/FV @ 572°F. One 82 sq ft Wiped-Film Evaporator (WFE) rated for 22 psig/FV @ 572°F. All of these systems were manufactured in 2015 in modular construction units and are ready to ship. Virtually all of the process contact material of construction is 304 stainless steel or better. The facility was designed and delivered in modules, but was never constructed or operated.

More Details

• The Fischer-Tropes Reaction Section, the Product Fractionation Section, and the Wax Upgrade Section were all manufactured in 2015 and have never been operated. All of the equipment downstream of the FT Reactors is constructed of 304L stainless steel or better alloys.
• The process is being kept under a nitrogen blanket. All electric motors are being “bumped” weekly or they have been removed and are in climate- controlled storage.
• The DCS is by Yokagawa and it is completely programmed and ready to install. The hardware is still at Yokagawa.
• There is no asbestos in this facility.
• Many spare parts are available.
• This system is located on a major deep-water port with international shipping routes.

This higher-alloy and graphite constructed hydrochloric acid (HCl) recovery system was designed by Sabic.  It can handle up to 24 m3/hr of liquid feed and separate out the organics, water, and HCl in aqueous form.  The system includes a main distillation column for HCl removal, four HCl absorbers, an HCl regeneration column, and an HCl water removal column.

The previous service was for the recovery of 3% HCl in a wet phenol stream.

Subsystem from a Complete Bisphenol-A (BPA) Plant Stock #600363