RM TECHNICAL DATASHEET. Ballast tray section properties. 1 of the 2010 Aluminum Design Manual Clip Load Direction Y + Y - X.

Glitsch Nye tray This is the author s correlation of a nomograph in the Glitsch Manual. It gives results within 5% of the nomograph for diameters 4 feet or greater and within 15% for smaller diameters. This is adequate for this first approximation of tower diameter. It applies for Bottoms Level. Trays are particularly vulnerable to damage during shutdown and startup operations. Inc., (Reference 14) provides several good tips to minimize the possibility of tray damage during such periods.

Glitsch Ballast Tray Design Manual, 5th Ed., Bulletin No. Copyright 1974, Printing 1989, Glitsch, Inc. A straight reduced asphalt is the residual product after removing the most volatile or lower boiling components (usually lower than 1,000 °F normal boiling point) from crude oil. Crude oils vary in their content of asphalt residuum, and may eontain as little as 1 LV% or as much as over 60 LV%.

From a given crude oil the asphalt yield will vary with the consistency (i.e, penetration) of the residuum, which in turn is dependent upon the extent of removal of the lower boiling components. Thus, the lower the penetration of the asphalt residuum, the lower is its yield on erude. There are three general methods by which asphalts of this type ean be manufaetured. These methods are vaeuum distillation, blending and solvent separation.

Among these methods vacuum distillation has historically been the most popular method for the manufaeture of straight redueed asphalts. After distillation of the erude oil in an atmospheric pipestill, the redueed crude is partially vaporized in a furnaee and eontinuously flashed in a vaeuum pipestill (VPS). Straight redueed asphalt is obtained as bottoms from the VPS, whereas a 'broad cut' vacuum gas oil (VGO) is obtained as overhead from the VPS. Penetration of the vaeuum residuum will be determined primarily by the temperature and pressure at which the reduced crude is flashed in the VPS. Vaeuum redueed asphalts typically have initial boiling points of about 1,000 °F (atmospherie equivalent boiling point), although this depends on the inherent eomposition of the crude oil. The VGO can be used for 'fluxing' (i.e., softening) eertain straight reduced asphalt grades for specifie applieations or as craeking feed stock. Straight reduced asphalt may also be obtained as bottoms from a VPS in which lubricating oil fractions are being separated.

A VPS for the manufaeture of asphalts looks very mueh like the bottom section of a lube VPS. It eonsists of a tower operated under vacuum in which the reduced crude is flashed. The seetion below the flash zone of an asphalt VPS is fitted with about six trays to strip with steam the liquid product from the flash zone.

This stripping removes lower boiling components present in the liquid, thereby permitting a lower flash zone temperature for the desired cut point. The section above the VPS flash zone is generally fitted with a Glitsch grid. In this section vapors from the flash zone (i.e., VGO product) are eondensed by direct heat exchange with a cold VGO liquid pumparound. Liquid from the Glitsch grid is removed from the tower using a total drawoff tray. No fractionation of the vapors from the flash zone is required sinee there are usually no specifications on the VGO Another variation in fuel vacuum pipe still designs is to use contacting devices that give lower pressure drop than distillation trays.

These permit a lower flash zone operating pressure and thereby allow higher yields of heavy gas oil. The plates in the wash section are replaced with Glitsch grids. These grids are highly efficient de-entrainment devices and give a reasonable fractionation contacting efficiency. The plates in the pumparound sections are replaced with Pall ring packing. El Jardin De Al Lado Pdf.

This packing competes well with plates in providing the required heat transfer area in the minimum practical tower height. Ballast, Valve V-Series V-1 thru V-5 valves Figure 8-74 and 8-77 Glitsch Higher than Sieve High/High Medium Similar to Sieve Good Figure 8-64.

Bubble cap tray In large column. Used by permission, Glitsch, Inc. Figure 8-67B. For sieve tray layout arrangements typical one-, two-, and four-pass tray flow patterns with clarifying flow markings by this author. Used by permission, Glitsch, Inc., Bui. Glitsch Nye Tray action to improve conventional sieve and valve tray performance by 10-20%. Used by permission, Glitsch, Inc., Bui.

Klein [201] has evaluated from the literature including manufacturer s, i.e., Glitsch [202], Koch [203], and Nutter [204], design procedures for their respective valve type tray Glitsch, Inc. Ballast Tray Design Manual, Bui. 4900, 5th Ed. Glitsch, Inc. (1974, 1989), Dallas, Texas.

Glitsch performance data for their Cascade Mini-Ring are shown in Figures 9-34A, B, and C for HETP with other published data and pressure drop for comparison with Pall rings and sieve trays. Note the abbreviation CMR stands for Cascade Mini-Rings. The performance and design information in Glitsch reference [104], as for all the other manufacturers with respect to their data and charts, is proprietary, but not necessarily warranted to be suitable for the designer s service/applications unless verified by the manufacturer s representatives.

GUtsch Ballast Tray Design Manual, 5th Ed. 4900, Copyright 1974, Glitsch Inc. The vapors from the flash zone are cleaned from bottoms components in the VPS 'wash zone,' which is located immediately above the flash zone. The VPS wash zone consists simply of an entrainment removal device called a Glitsch grid which works on the same principle as a crinkled wire mesh screen.

This device provides a large amount of surface area on which entrained bottoms components can coalesce. The coalesced liquid is then washed from the grid by clean wash oil distributed uniformly over the grid by means of spray nozzles. Coalesced liquid and wash oil from the wash zone are removed using a total drawoff tray. Vapors passing overhead from the VPS wash zone are fractionated and condensed in the upper section of the VPS.

Liquid reflux is necessary in this section of the tower to obtain the desired degree of fractionation. Another alternative might be to make sure that dust suppression, such as water or foam, or other controls are instituted so that the wind will not transport hazardous materials to the support zone. This is easier said than done.

Although dust suppression techniques have been used with success, if there is a glitch in the dust suppression system, workers in the support zone may be exposed. It appears that this situation might be more difficult to resolve than initially thought. This theoretical problem has existed on many hazardous waste sites.

We believe that this situation could have best been resolved during the planning stages. Type A-1 Ballast Tray. Used by permission, Glitsch, Figure 8-77. Type V-1 Ballast Tray. Used by permission, Glltsch, Inc. The design engineer cannot adequately design a valve tray that includes the operating valves and expect to have reliable performance. The proper approach is to assemble all of the required system/column operating performance requirements and then turn the problem over to a manufacturer who has tested its own valve designs and is capable of predicting reliable performance.

The manufacturer can then provide a hydraulic design for the tray, as well as the expected performance of the entire column/tray system. The major manufacturer/designs are Nutter Engineering, Harsco Corporation, [204] Koch Engineering Co., Inc. [203] Glitsch, Inc. [202], and Norton Chemical Process Products Corporation [233].

Figure 8-158. Composite tower-tray assembiy iliustrating speciai trays with corresponding nozzles. Used by permission, Glitsch, Inc. Figure 9-6CC. York-TwisP structured tower packing. Note insert showing weave and sections fabricated to fit through manway for larger towers.

Used by permission of Otto H. York Co., Inc., a division of Glitsch, Inc. Example 9-8 Heavy Gas-Oil Fractionation of a Crude Tower Usu Glitsch s Gempak (used by permission of Glitsch, Inc.

Last Updated on Mon, 03 Jun 2013 (2) CIRCULATION RATE LC3 = QC3/(c)(t(n-2)-tC32) (3) CONDENSER DUTY-ENVELOPE ZT Qcoh= Qvn-(qnv+QNl + QH2o) Figure 4.7. Heat and equations-top tray and condenser. Presence in the vapor of the overhead distillate liquid and considering the overhead distillate vapor and steam as inerts. Convert the of the unstripped hydrocarbon liquid on the draw tray to this partial pressure and check the assumed temperature. Set the temperature drop across the at 30 degrees F and calculate the heat content of the product leaving the system.

Calculate and tabulate the external heat quantities to the base of Tray (B + 1). Calculate and tabulate the vapor and liquid quantities above Tray B. Top Tray Calculations and Overhead Condenser Duty The heat and material balance relationships at this section of the tower are determined by making balances around Envelopes V and VI as shown on Figure 4.4. An expanded view of this section together with the equations to be used in the computations is given by Figure 4.7.

Calculations of Top Pumparound Heat Removal-Envelope V a. In Step D, the temperature of the overhead product vapor was calculated on the basis that there would be zero to the tower from the condenser. At this temperature, calculate the heat content of the vapor leaving the tower. Note tlVat this stream consists only of product materials and stripping steam. The top pumparound heat removal is now calculated as that amount required to balance the toWer. In practice it may not be feasible to set the temperature of the cool pumparound liquid 150 degrees F lower than the overhead vapor temperature, In this case, take a reasonable approach to the temperature of the available cooling medium and calculate the top pumparound circulation rate.

Calculation of Overhead Condenser Duty—Envelope VI The overhead condenser duty is calculated as the enthalpy difference between the overhead vapor and the products from the overhead accumulator. Fractionation Calculations 1. Calculation of Internal Reflux to Key Trays By making heat balances, calculate the internal reflux at the following points in the tower. Liquid to the top tray in the bottom pumparound section, Tray (A — 1).

Liquid from the bottom tray in the midpumpa-round section, Tray (B - 3). Liquid from the bottom tray in the top pumparound section, Tray (N — 2). Lg _ 3 and Ljsj _ 2 are the liquid rates which are used in the fractionation analysis. Fractionation Calculations Using Figures 4.2 and 4.3, determine the degree of separation possible for the system as calculated.

If the fractionation criteria have not been satisifed, additional trays or reduced heat removal may be employed to achieve the desired separation. Vapor-Liquid Traffic Tabulate and plot the vapor and liquid traffic at key points in the tower. This plot will usually identify the points of maximum load in the tower and will be of great assistance in tower sizing and tray design calculations.

Process Design Considerations Assuming that the heat and material balance calculations have been finished and that the design appears feasible, the remaining tasks are to ensure that the assumed pumparound configuration can indeed remove the required amount of heat from the tower. Neeld and O'Bara (7) and Fair (8) have published procedures for calculating the heat transfer capabilities of 'jet trays' and side-to-side trays, respectively. Jet trays are similar to conventional trays, e.g., bubble-cap or valve trays, which would normally be specified for this service, and, thus, Neeld and O'Bara's correlations may be used as checks. Since tower diameters are used in the heat transfer calculations, tray sizing calculations may be made using procedures from Glitsch (9) or Koch (10) or any other method which the reader might prefer. If an insufficient number of heat transfer trays were provided in the original design assumptions, they can be added as required with only minor modifications to the calculations. References 1.

'1970 Refining Processes Handbook,' Hydrocarbon Processing (September, 1970), pp. Edmister, Applied Hydrocarbon Thermodynamics (Houston: Gulf Publishing Company, 1961). Maxwell, Data Book on Hydrocarbons (Princeton. Van Nostrand Co., 1965). Technical Data Book-Petroleum Refining (Washington, D.C.: American Pelroleum Institute, 1966). Houghland, E.J.

Lemieux, and W.C. Schreiner, L'The Performance of Catalytic Cracking Unit Fractionating Towers,' 19th Midyear Meeting, API Division of Refining, (May 13, 1954). Packie, 'Distillation Equipment in the Oil Refining Industry,' AIChE Transactions 37 (1941), pp. Neeld and J.T. O'Bara, 'Jet Trays in Heat Transfer Service,' CEP 66, no 7 (July, 1970) pp. Fair, 'Design of Direct-Contact Gas Coolers,' PetroJChemical Engineer (August, 196 1).

'Ballast Tray Design Manual,' Bulletin No. 4900, Fritz W. Glitsch & Sons Inc., Dallas, Texas.

'Koch Flexitray Design Manual,' Koch Engineering Co., Inc., Wichita, Kansas. Fracti fracti Up to this point, this work has considered gross or rough separations. In the case of the atmospheric crude tower, petroleum was separated into relatively narrow fractions while, in the case of the FCCU main fractionator, the tower produced fewer fractions having wider boiling ranges. In both cases, the lightest (overhead) fraction was a full-range naphtha, i.e., everything in the tower feed up to a certain predetermined end point.

This section will concern itself with the distillation processes required to separate light hydrocarbon components from the heavier continu-ous-boiling fractions, to fractionate the discrete light ends components and to separate the heavier continuous boiling materials into two or more fractions. In the refinery, the term 'light ends' generally means any discrete component lighter than heptane which can be identified by a name. This includes everything from hydrogen through the hexanes. A more narrow definition might consider only C3 and C4 liquids as light ends since, in many refineries, ethane and lighter is used as fuel gas and the pentanes and hexanes are blended dircctly into gasoline. As will be seen in the development of this section, there are many reasons for recovering light ends, each being dictated by the process configuration and economics of the refinery in question. For a moment, let us explore the historical development of light ends recovery plants within the context of the total refinery. In the early days of the industry, kerosene, stove oil and lubricants were the principal products.

With the advent of the automobile, gasoline became valuable and was produced. Ac Dc Best Hits Download on this page. In most cases, the raw naphtha distillate was stored in open tankage where the light components vaporized and the gasoline became self-stabilized.

Besides being wasteful, this practice was dangerous. As the automobile engine developed, gasoline specifications became more stringent, and a need developed for better control of vapor pressure which radically affects carburetion and ignition.

The refiner accomplished this by installing a naphtha stabilizer with which he could closely control gasoline vapor pressure. A secondary benefit was that the vapor distillate from this tower—essentially butanes and lighter—could be used as fuel gas within the refinery. Figure 5.1 shows a typical whole naphtha stabilizer producing a vapor distillate to the refinery fuel gas system.

In time, some enterprising person invented a stove utilizing as fuel either propane or butane, which the refinery could easily produce. It required that the naphtha stabilizer be redesigned at a higher pressure level in order to yield a liquid distillate which, in turn, could be fractionated into propane and butane as liquefied petroleum gas (LPG).

Figure 5.2 shows a typical scheme for processing the whole naphtha stabilizer liquid distillate into propane and butane while still yielding fuel gas consisting of ethane and lighter. As time, passes and the petroleum industry and society develops, the demand for refinery products skyrockets, and product specifications continually tighten. New processes are developed to improve gasoline octane.

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