This 321 stainless steel, high-pressure stripper column system was designed by ICI and built by Robert Jenkins, LTD. The column is rated for 250 psig at 220oC. The system used live steam to strip light components from crude methyl amine product (932 kg/m3 density).
The 321 stainless steel (10.5% Ni) column is 3.0' diameter by 54' straight side. It has a design pressure of 250 psig @ 220oC. The column has 28 single-pass valve trays also constructed of 321 stainless steel. The column has an internal overhead condenser mounted in the top head. It also has an overhead stream cooler as well as a bottoms cooler. There are two feed interchangers for heating the feed with the column bottoms stream.
Feed to the column is heated by cross-exchanging with the column bottoms flow using two feed interchangers. The interchangers are constructed of 321 stainless steel on both the shell and tube sides. The feed enters the column around the tray #8 area, but there are other optional feed entry points.
An internal condenser is used in the top of this column to condense heavier compounds in the overhead stream. The condensed compounds are collected and further cooled in the overheads cooler before being sent to storage.
The hot bottoms stream from the column is cross-exchanged with the incoming feed using two interchangers in series. The bottoms stream is further cooled in the bottoms cooler exchanger.
Intermediate pressure steam is injected into the column bottoms through a 2” nozzle to provide the stripping momentum.
This high-pressure stripper column system includes the following major components:
Stripper Column: The 321 stainless steel (10.5% Ni) column is 3.0' diameter by 54' on the straight side. It was manufactured by Robert Jenkins, LTD with a design pressure of 250 psig/FV @ 220°C. The column has 28 single-pass valve trays also constructed of 321 stainless steel. The column has an internally mounted condenser in the top section.
Feed Interchangers (2): 425 sq. ft. (each) horizontal heat exchangers. 321 stainless steel tubes, shell, and heads. Design pressure on the tube side is 250 psig/FV @ 220°C and on the shell side is 250 psig/FV @ 220°C. There are 80 tubes - ¾” diameter by 14 SWG by 13’-5” straight tube length.
Overhead Condenser: Internal to the stripper column; 596 sq. ft. vertical condenser. 321 stainless steel ‘U’ tubes with carbon steel head. Design pressure on the tube side is 100 psig/FV @ 5/70°C. There are 251 “U” tubes - ¾” diameter x 12.25’ straight tube length.
Overheads Cooler: Hairpin “U” fin tube carbon steel exchanger; 187 sq. ft. of surface area. Design pressure on the tube side is 100 psig @ 50°C and on the shell side is 250 psig @ 220°C. Tubes are ¾” diameter by 15’ long with a 4” diameter shell.
All instrumentation and control valves are provided with this system.
Typical industrial distillation towers; Continuous distillation
and desired products. Given a simple, binary component feed, analytical methods such as the McCabe–Thiele method or the Fenske equation can be used. For a multi-component feed, simulation models are used both for design and operation. Moreover, the efficiencies of the vapor–liquid contact devices (referred to as "plates" or "trays") used in distillation towers are typically lower than that of a theoretical 100% efficient equilibrium stage. Hence, a distillation tower needs more trays than the number of theoretical vapor–liquid equilibrium stages. A variety of models have been postulated to estimate tray efficiencies.
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