Perspectives: Plant InSites

Distillation Columns: Get Some Inside Information

A gravity-flow loop can enable measuring internal liquid flow in a column

By Andrew Sloley

Throughput or fractionation performance in specific systems may vary dramatically depending upon how precisely the internal liquid rate can be controlled close to its limit. Four basic methods can determine the liquid rate within a column:

• calculating heat and material balances using heat input, heat output and external stream rates and properties;
• taking a total draw and then returning liquid through a metered pumped-flow loop;
• taking a total draw and then returning liquid through a metered gravity-flow loop; and
• measuring a column liquid level to infer flow.

Each of these has pros and cons; several or all four might work for a given system. Physical layout and data precision impose particular requirements for each option. Specific systems tend to favor one option or another. Getting the details right counts.

Here, let’s specifically look at taking a total draw and then returning the liquid through a metered gravity-flow loop.

Figure 1 is a partial elevation sketch of a 42-in.-diameter distillation tower. Feed enters the tower between Bed 2 and Bed 3. Beneath Bed 2, a collector tray takes liquid out as a total draw. A gravity-fed loop is used to measure the flow rate of liquid from that collector tray.

I first applied this configuration nearly 25 years ago in a specialty lubricants distillation unit as part of a larger revamp. Discussing that job after the fact, another senior engineer emphatically stated that this type of flow measurement system never could work. He had seen many attempts but none had succeeded. This surprised me because the client was very pleased with its performance. So, we sat down together to review what was built.

Figure 1 highlights seven key features:

1. Collector tray. This serves to gather the liquid. For a packed tower, it’s a default choice. Most applications of this configuration will have a low liquid rate. (A future column will cover the “why.”) Therefore, the tray must be fully welded. A collector tray is a good idea even in a tower with trays. However, with the correct modifications, a special tray configuration may suffice.

2. Nozzle sized for self-vented flow. Vapor bubbles entrained in the liquid reduce system capacity and give incorrect flow-meter readings. Self-vented nozzles have a low enough liquid velocity that vapor can escape and return to the tower. (See: “Assess the Gravity of the Situation.")

3. Sufficient static head. H1 is the minimum distance required to generate enough static head for pressure drop to drive flow through the system. This sets the minimum distance between the draw nozzle and return nozzle elevations. Pipe diameter often is reduced downstream of the self-venting nozzle to cut costs. In that case, H1 must be based on the elevation of the pipe diameter reduction, as shown in Figure 1. In an effort to minimize this height, high-β-value orifice plates often are used to decrease pressure drop.

4. Adequate upstream pipe run. H2 is the minimum upstream pipe run to get well-conditioned flow needed for accurate metering. With orifice flow meters, the higher the β value, the longer the pipe run required. (See: “Think Straight about Orifice Plates.”)

5. Flow instrument in liquid-filled location. The meter can be installed in either a vertical (as shown) or horizontal position. In all cases, the piping configuration must ensure the line is filled with liquid.

6. Long-enough downstream pipe run. H3 is the minimum downstream pipe run necessary for well-conditioned flow for meter accuracy.

7. Suitable distance between the return and lowest-pressure points. H4 is the minimum interval from the return elevation to the lowest-pressure point (vena contracta) to prevent vaporization downstream of the orifice plate. The vena contracta occurs some distance after the orifice plate. Most times, it’s close enough that the orifice plate location can be used to set elevations. Nevertheless, engineers with a good grasp of fundamentals never forget the difference. Avoiding vaporization is important to getting accurate flow measurements. Either H3 or H4 may set the minimum distance from the flow meter to the return nozzle.

One extra point not shown — insulation — is important. In hot systems, a little heat loss makes H4 less likely to set the system. In cold systems, heat gain easily may make H4 dominant. More insulation helps. Vaporization in the system also dramatically may boost pressure drop, increasing H1 as well.

These points apply equally to both packed and trayed towers.

Going back to the discussion with my colleague: After reviewing the system, he asked: “Just how tall was this loop?” The final system with its vertically mounted meter was nearly 30-ft high. Gravity-feed flow-measurement systems require ample height. A horizontal mounting may make H2 and H3 unimportant but H1 and H4 never go away.


ANDREW SLOLEY is a Chemical Processing contributing editor. You can email him at ASloley@putman.net

More from this perspective...

Title

Consider More Than Static Mixers

A number of technologies can handle pipeline mixing.

01/31/2011

Properly Assess Energy Recovery Projects

Impact on other operations and transfer prices may alter the economics.

03/09/2011

Find the Real Maximum Pressure Of Vessels

Always consider static head when assessing pressure vessels.

04/21/2011

Don't Calculate Pressure Drops in a Vacuum

Consider flow regime boundaries and the limitations of methods.

06/08/2011

Pick the Proper Centrifugal Pump

Consider the impact of startup conditions and prospective operating points.

07/11/2011

Take a Different Look at Centrifugal Pumps

An unconventional assessment can provide insights for effective control.

07/25/2011

Distill Your Internals Choice

Some general guidelines can ease the selection process.

09/01/2011

Watch Out For Dead-Legs

Lack of flow doesn't mean lack of problems.

09/27/2011

Tackle Tray Trade-Offs

Find the right compromise between process and mechanical requirements.

10/26/2011

Let the Buyer Beware

Understand common dangers when developing specifications and evaluating bids.

11/21/2011

Do Liquid Injection Right

A variety of factors influence performance.

01/05/2012

More Exchanger Area Can Pose Pitfalls

This "obvious solution" for heat-transfer problems may not work.

02/01/2012

Vacuum System Fix Fizzles

Use of scavenged equipment leads to problems.

03/07/2012

Old Doesn't Mean Outdated

Some equations have stood the test of time.

04/04/2012

Get Your Head Around Velocity Head

Confusion about what the term means can spell trouble.

05/02/2012

Select the Right Reboiler

Understand the strengths and weaknesses of various options.

06/04/2012

Consider Compact Reboilers

Several types of heat exchangers can save space

07/24/2012

Piping Geometry: Grasp Line Layout

Draining, venting, fouling and other considerations affect piping geometry.

09/06/2012

Properly Position Interlock Valves

The obvious location may not be the most cost effective

10/16/2012

Backflush Away Fouling

Flow reversal can remove fiber buildup in heat exchangers.

11/06/2012