阅读说明：本技术 具有以45度取向的降液管的分馏塔盘 (Fractionation tray with downcomers oriented at 45 degrees ) 是由 凯文·J·理查德森 布莱恩·J·诺瓦克 迈克尔·J·贝姆 大卫·M·沃拉伯 山达·G·弗赖伊 于 2019-08-22 设计创作，主要内容包括：本发明提供了一种降液管布置结构,该降液管布置结构以与支撑件成45度角取向,该支撑件是分隔壁塔内的壁或允许蒸馏塔内的塔盘之间具有0.3m至0.76m间距的减小间距的支撑梁。优点包括使用单个支撑梁来支撑两个塔盘以及更有效的操作,并且允许塔具有0.9米至15.2米的直径。(The present invention provides a downcomer arrangement that is oriented at a 45 degree angle to a support that is either a wall within a dividing wall column or a support beam that allows a reduced spacing of 0.3m to 0.76m spacing between trays within a distillation column. Advantages include the use of a single support beam to support both trays and more efficient operation, and allowing the column to have a diameter of 0.9 to 15.2 meters.)

1. A tray assembly for a distillation column, the tray assembly comprising a support beam or wall, a plurality of downcomers contacting the support beam or wall and extending from the support beam or wall at a 45 degree angle.

2. The tray assembly of claim 1, further comprising a plate having a plurality of openings above the downcomer.

3. The tray assembly of claim 1, wherein the tray assembly comprises a support beam having upper and lower flanges extending along the entire length of the support beam.

4. The tray assembly of claim 1, wherein the support beams are I-beams.

5. The tray assembly of claim 1, comprising an upper downcomer and a lower downcomer.

6. The tray assembly of claim 5, wherein the upper layer of downcomers is perpendicular to the lower layer of downcomers.

7. The tray assembly of claim 1, having a diameter of 0.9 to 15.2 m.

8. The tray assembly of claim 1, having a maximum diameter of 9.1 m.

9. The tray assembly of claim 1, wherein each of said layers is spaced apart by a minimum of 0.3m to 0.76 m.

10. The tray assembly of claim 1, wherein each of said layers is spaced apart by a minimum of 0.3 m.

Background

The present invention relates to an arrangement of fractionation trays for use in a distillation column for separating volatile compounds via fractional distillation. More particularly, the present invention relates to a fractionation tray having downcomers oriented at 45 degrees to a support beam across the diameter of the distillation column, or in the case of a dividing wall column, at 45 degrees to the dividing wall.

Fractionation trays are widely used in the petrochemical and petroleum refining industries to facilitate multi-stage vapor-liquid contacting in fractionation columns. A normal configuration for a fractionation column includes 10 to 120 individual trays. Typically, the configuration of each tray in the column is the same. The trays are installed horizontally, at a uniform vertical distance called the tray spacing of the column. This distance may vary in different parts of the tower but is generally considered constant. The trays are typically supported by rings welded or bolted to the inner surface of the column.

Fractionation trays prior to the present invention have employed a cell design due to the 90 degree rotation between trays, which is ideal for use in divided wall columns. However, if the walls are oriented parallel or perpendicular to the downcomer, the walls make it impossible to have the same hydraulic tray design for an odd number of trays and an even number of trays. This is the typical orientation one desires. If the dividing wall is slightly off-center, the difference between the odd and even number of trays becomes even greater. Thus, the performance of the odd and even number of trays may be different and may be the cause of hydraulic bottlenecks.

In addition to the difficulties found in conventional designs of fractionation trays having downcomers in a divided wall column, there are also difficulties in conventional columns that do not include a divided wall. Trays require mechanical support, which is typically achieved by using downcomers as the primary support structure. The problem is that as the column diameter becomes larger, the downcomer height must be increased in order to meet the tray deflection conditions. This in turn leads to an increase in the design tray spacing to accommodate deeper downcomers. Thus, tray spacing is determined or limited by mechanical constraints rather than process/hydraulic constraints. A significant advantage of this tray over competitor technology is that a relatively low tray spacing of 12 inches (30.48cm) can be achieved. At large diameters, this advantage diminishes as tray spacing needs to be increased in order to meet mechanical design criteria. The low tray spacing allows a large number of MD/ECMD trays to be housed in a single shell or possibly reduce the column height to meet customer constraints, thereby providing technical advantages in the marketplace. Although I-beams can be used for very large diameter columns greater than 9.7m (> 32 feet), a relatively high tray spacing is still required. The problem is that in the prior art configuration, the I-beams are perpendicular to the downcomer they support and parallel to the downcomer of the tray below. Thus, the beams are located directly above the movable tray deck below and have the potential to interfere with the vapor flow through that particular deck section below. Another problem is that if the width of the beams is greater than 15cm (6 inches), it is difficult to obtain liquid under the I-beams to feed to the underlying movable tray deck. Both of these problems can lead to maldistribution and poor tower performance. To reasonably prevent these problems, the height of the I-beam is limited so that the I-beam can only extend slightly below the bottom of the downcomer, thereby limiting its strength.

Disclosure of Invention

The present invention provides a tray assembly for a distillation column comprising a support beam or wall, a plurality of downcomers contacting the support beam or wall and extending from the support beam or wall at 45 degrees. The tray assembly also includes a plate having a plurality of openings above the downcomer.

The tray support beam may have an upper flange and a lower flange extending along the entire length of the support beam, which may be configured as an I-beam. The support beams of the tray assembly provide support for both the upper and lower downcomers, which allows the layers to be spaced closer together than prior art mounting devices. In a preferred embodiment of the invention, the upper downcomer is perpendicular to the lower downcomer. The present invention allows the tray assembly to have a maximum diameter of 0.9 to 15.2m (3 to 50 feet) and typically 9.1m (30 feet). The tray assembly allows for the layers to have a minimum spacing of 0.3 to 0.76m (11 to 30 inches) and typically 12 inches (0.3 m). The tray assembly may include at least one of: a sensor for sensing at least one parameter and capable of generating a signal from the sensing; a component capable of generating and transmitting a signal; or components capable of generating and transmitting data regarding the operation of the tray assembly.

Drawings

Fig. 1 shows a set of downcomers of a fractionation tray oriented at 45 degrees relative to a support beam.

Figure 2 shows a side view of a group of downcomers connected to a support beam.

Figure 3 shows a top view of a group of downcomers connected to a support beam.

Figure 4 shows a portion of a platform layer having circular openings and slots.

Fig. 5 shows a column with a dividing wall and a plurality of trays.

Detailed Description

In the petroleum refining, petrochemical and chemical industries, fractionation columns are used for the separation of various compounds. They are used, for example, in the separation of various paraffinic hydrocarbons, such as the separation of butanes and pentanes, in the removal of contaminants including water from hydrocarbon streams, and in the separation of various alkylaromatic hydrocarbons, such as the separation of toluene from xylenes. Fractionation trays are also used for separating oxygenates such as ethers or alcohols from hydrocarbons, for separating inorganics such as halogenated compounds, fluorocarbons and elemental gases, and various other separations. Fractionation columns and trays therefore have great utility in many industries.

During the fractionation process, the vapor produced at the bottom of the column rises through a large number of small perforations spread over the area of the tray deck, which supports a quantity of liquid. The passage of the vapor through the liquid creates a layer of bubbles called froth. The large surface area of the foam helps to quickly establish a compositional equilibrium between the gas and liquid phases on the tray. The vapor loses less volatile material to the liquid and thus becomes slightly more volatile as it passes upwardly through each tray. As the liquid moves downward from tray to tray, the concentration of lower volatility compounds in the liquid increases. The liquid separates from the froth and travels down to the next lower tray. This foam formation and separation is performed on each tray. Thus, the tray performs the following two functions: the rising vapor is brought into contact with the liquid, and the two phases are then separated and flow in different directions. When these steps are performed an appropriate number of times, the process can result in highly efficient separation of the compounds based on their relative volatility.

The present invention is readily applicable to multiple downcomer trays. Multiple downcomer trays have several distinct physical characteristics. For example, multiple downcomer trays do not have "receiving pans". This is a generally imperforate segment located below the outlet downcomer opening. This is the imperforate area of the tray on which liquid descending through the downcomer impinges before passing horizontally to the deck of the tray. The receiving pans are typically located directly below the downcomers leading from the next upper conventional fractionation tray. The horizontal deck surface area of the preferred embodiment of the multi-downcomer fractionation tray is divided into a recessed area that serves as a downcomer and a flat vapor-liquid contacting area commonly referred to as a deck. No non-porous area is allocated to receive descending liquid from the tray directly above.

Another significant feature of typical multi-downcomer type fractionation trays is the provision of a relatively large number of parallel downcomers evenly spaced across the tray. From one to fifteen or more downcomers may be employed per tray. These downcomers are spaced relatively close together, as compared to the downcomers of a cross-flow fractionation tray, because they spread over the surface of the tray rather than just at the periphery of the tray. The distance between adjacent downcomers of a multi-downcomer tray (measured between its side walls) will be between 0.2 and 2.0 meters, and preferably less than 0.5 meters.

The land portion between any downcomers on the tray is preferably substantially planar, i.e., flat, and oriented in a horizontal plane. These deck sections preferably have evenly distributed openings with sufficient total cross-sectional opening area to allow the desired total vapor flow upward through the tray at a suitable velocity. The uniform circular openings of standard sieve trays are preferred but may be supplemented by vapor flow guide slots. The open area provided by the deck perforations can vary from 5% to as much as 30% to 45% of the tray deck area. The diameter of the circular perforations is typically 0.3cm to 0.6cm, but may be a maximum of 1.87 cm.

As used herein, the term "column" (or "exchange column") refers to a distillation or fractionation column or zone, i.e., a column or zone in which a liquid phase and a vapor phase are countercurrently contacted to effect separation of a fluid mixture, such as by contacting of the vapor and liquid phases on packing elements or on a series of vertically spaced trays or plates mounted within the column.

A divided wall column is in principle a simplification of a thermally coupled distillation column system. In a divided wall column, the dividing wall is located in the interior space of the column. The dividing wall is generally vertical. Two different mass transfer separations can occur on either side of the dividing wall.

Exchange columns typically contain some form of vapor-liquid contacting device, which may be in the form of a packing (such as a random or structured packing) or fractionation tray. Fractionation trays typically include a large flat area, called the deck or contacting deck of the tray, and means for delivering liquid from the next tray above to the tray and removing the liquid for delivery to the next tray below.

The portion of the liquid removed from the tray that flows across the tray is called a downcomer. A downcomer is a conduit for passing liquid downwardly disposed in an opening in a panel contacting a platform. In some downcomers, a portion of the wall of the downcomer may extend above the panel and is referred to as an outlet weir, and a portion of the downcomer that extends below the panel is referred to as a downcomer baffle. However, the outlet weir is typically a separate mechanical piece and not necessarily an extension of the downcomer wall. In fact, the tray can be designed without an outlet weir.

Vapor produced in the lower section of the column passes upwardly through the perforations in the deck, while liquid flows downwardly from tray to tray, countercurrent to the vapor. For a "cross-flow tray," liquid first enters the tray from a downcomer on the tray above. The liquid then passes over the deck of the tray and eventually exits through an outlet downcomer of the tray. One type of "cross-flow tray" is disclosed in us patent No. 6,645,350 (Steacy).

During normal operation, liquid collected on the tray flows over the perforated panel of the deck where it contacts the upflowing vapor passing through the perforations. The liquid then flows into the downcomer over the outlet weir and onto the receiving area of the perforated panel of the tray below, and so on. The downcomers of two adjacent trays are not placed directly above each other, but are spaced apart (or staggered) in the lateral direction in order to prevent liquid from falling directly into the downcomer of the lower tray.

The present invention changes the configuration of the support beams and in some embodiments of the invention, the I-beams are placed at a 45 degree angle to the tray downcomers. This allows thicker I-beams to be used and the height of the I-beams is increased to the full tray spacing (plus flange thickness), significantly increasing its strength and also allowing a single I-beam to support two trays. The trays may be MD trays or ECMD trays known to those skilled in the art. The bottom flange supports one tray and the top flange supports the other tray. In this configuration, the I-beams do not encroach on the movable tray deck because the beams are all in the same orientation, directly above each other. The prior art utilizes beams that are rotated 90 degrees on successive trays to correspond to the MD/ECMD tray orientation. With the I-beams at 45 degrees and all having the same orientation, there is no movable tray deck below them, so there is no need to transport liquid below them as in the previous configuration. This significantly reduces the likelihood of liquid/vapor maldistribution. Research has found that a low tray spacing of 12 inches (30.48cm) can be maintained even at very large diameters approaching 30 feet or more, which should allow for the close spacing of the trays to be maintained even at large diameters. Previously, the diameter limit was closer to 19 feet (5.8 meters), where closely spaced trays were able to maintain a low design tray spacing. In the present invention, the layers of the trays may be spaced 0.3 to 0.76m (11 to 30 inches) apart.

In another embodiment of the invention, the downcomer is oriented at a 45 degree angle to the dividing wall in the dividing wall column. As previously mentioned, fractionation columns have great utility in many industrial processes. Conventional fractionation columns are used to separate an incoming feed stream into two fractions. These are referred to as the overheads and bottoms, where the overheads are the lighter or more volatile components of the feed stream. The feed stream may comprise only two components separated into a high purity stream within the fractionation column. In this case, the top stream and the bottom stream will each be rich in one of the two components of the feed stream. However, in many cases, the feed stream comprises three or more compounds, and in the case of a petroleum refining process, the feed stream may comprise 100 or 200 or more individual volatile chemical compounds. These mixtures are usually separated by boiling point range into fractions which may each contain a number of different volatile compounds.

In order to separate a feed stream containing three compounds into a single product stream using a conventional column, each product stream being enriched in one of these compounds, it is necessary to employ two such fractionation columns. The first fractionation column will form a product stream having a high content of the lightest or heaviest desired components of the feed stream and a second product comprising the remaining components. The second product is then passed to a second fractionation column to divide the second product into two other product streams. It has been recognized about 50 years ago that these two columns could in some cases be integrated into a single column, and that utility and capital costs are advantageously reduced. This evolves through energy coupling and subsequent mechanical integration of the column to produce what are now referred to as "dividing wall" columns. The lower capital and operating costs of divided wall columns are now recognized and they are used more and more frequently in the petrochemical and petroleum refining industries.

As previously mentioned, the primary function of the downcomer of the fractionation tray is to separate the mixed phase material. ("froth") that enters the downcomer as "clarified liquid" and vapor, with the vapor being released through an inlet at the top of the downcomer and the clarified liquid being carried to the next lower tray. The vapor present above the trays has contacted the liquid on the trays and should be in equilibrium therewith. There is no need to recontact the vapor with the liquid. Entraining the vapor into the liquid being sent to the next lower tray reduces the performance of the tray and, therefore, the performance of the column. Thus, entrainment of vapor into the liquid is undesirable.

The present invention allows for the use of low tray spacing for very large diameter columns based on hydraulic constraints and is not altered by mechanical constraints. The invention may be better understood by reference to the following drawings. Figure 1 shows an example of the orientation of a downcomer relative to an I-beam that acts as a support for the downcomer in assembly 10. The I-beam 25 (also referred to herein as a support beam) is shown having an upper flange 30 and a lower flange 35. A top layer of downcomers 15, each having an extension 40 that rests on the flange 30 of the I-beam 25. The top downcomer 15 is shown abutting the I-beam 25 at a 45 degree angle. The lower downcomer 20 is also shown having an extension 40 that rests on the lower flange 35 of the I-beam 25. When the downcomer is described as being at a 45 degree angle to the support beam, the 45 degree is within 0.5 degrees, as any greater deviation will not work. The top downcomer and the bottom downcomer are then at 90 degrees or perpendicular to each other.

FIG. 2 shows a side view of the apparatus of the present invention wherein the I-beam 25 has a top flange 20 and a bottom flange 35. A top downcomer 15 and a lower downcomer 20 are shown.

FIG. 3 shows the relative orientation of the top downcomer 15 and the bottom downcomer 20 with respect to each other and with respect to the I-beams 25. The top and bottom layers are oriented perpendicular to each other.

Figure 4 shows a typical deck floor that can be located between multiple sets of downcomers. In this example, the platform 50 is typically a metallic material suitable for the pressures and temperatures present within a reactor having a plurality of generally circular openings 55 and slots 60 suitable for the passage of vapor and liquid. In some embodiments of the invention, the platform has only circular openings 55.

Fig. 5 shows a divided wall column 60 with a support 65. Extending downwardly from support member 65 is a dividing wall 70 having a plurality of trays 75, which are shown as being similar to the plurality of trays of the previous figures.

Any of the above-described catheters, cell devices, stents, surroundings, areas, or the like may be equipped with one or more monitoring components, including sensors, measurement devices, data capture devices, or data transmission devices. The signals, process or condition measurements, and data from the monitoring components can be used to monitor conditions in, around, and associated with the process tool. The signals, measurements, and/or data generated or recorded by the monitoring component may be collected, processed, and/or transmitted over one or more networks or connections, which may be private or public, general or private, direct or indirect, wired or wireless, encrypted or unencrypted, and/or combinations thereof; the description is not intended to be limited in this respect.

The signals, measurements, and/or data generated or recorded by the monitoring component may be transmitted to one or more computing devices or systems. A computing device or system may include at least one processor and memory storing computer-readable instructions that, when executed by the at least one processor, cause the one or more computing devices to perform a process that may include one or more steps. For example, one or more computing devices may be configured to receive data from one or more monitoring components relating to at least one piece of equipment associated with the process. One or more computing devices or systems may be configured to analyze the data. Based on the data analysis, one or more computing devices or systems may be configured to determine one or more recommended adjustments to one or more parameters of one or more processes described herein. One or more computing devices or systems may be configured to transmit encrypted or unencrypted data including one or more recommended adjustments to one or more parameters of one or more processes described herein.

Detailed description of the preferred embodiments

While the following is described in conjunction with specific embodiments, it is to be understood that this description is intended to illustrate and not limit the scope of the foregoing description and the appended claims.

A first embodiment of the invention is a tray assembly for a distillation column comprising a support beam or wall, a plurality of downcomers contacting the support beam or wall and extending from the support beam or wall at a 45 degree angle. An embodiment of the invention is one, any or all of prior embodiments of this paragraph up through the first embodiment of this paragraph wherein the tray assembly further comprises a plate having a plurality of openings above the downcomer. An embodiment of the invention is one, any or all of prior embodiments in this paragraph up through the first embodiment in this paragraph wherein the tray assembly comprises a support beam having an upper flange and a lower flange extending along an entire length of the support beam. An embodiment of the invention is one, any or all of prior embodiments in this paragraph up through the first embodiment in this paragraph wherein the support beam is an I-beam. An embodiment of the invention is one, any or all of prior embodiments of this paragraph up through the first embodiment of this paragraph wherein the tray assembly comprises an upper downcomer and a lower downcomer. An embodiment of the invention is one, any or all of prior embodiments of this paragraph up through the first embodiment of this paragraph wherein the upper downcomer is perpendicular to the lower downcomer. An embodiment of the invention is one, any or all of prior embodiments of this paragraph up through the first embodiment of this paragraph wherein the tray assembly has a diameter of from 0.9m to 15.2 m. An embodiment of the invention is one, any or all of prior embodiments of this paragraph up through the first embodiment of this paragraph wherein the tray assembly has a diameter of 9.1 m. An embodiment of the invention is one, any or all of prior embodiments in this paragraph up through the first embodiment in this paragraph wherein each of the layers is spaced 0.3m to 0.76m (11 inches to 30 inches). An embodiment of the invention is one, any or all of prior embodiments in this paragraph up through the first embodiment in this paragraph wherein the tray assembly further comprises at least one of: a sensor for sensing at least one parameter and capable of generating a signal from the sensing; a component capable of generating and transmitting a signal; means capable of generating and transmitting data relating to the operation of the tray assembly.