JPS58177106A - Multi-stage type high flow speed gas-liquid contact apparatus - Google Patents

Abstract

PURPOSE:To enhance gas-liquid contact efficiency, by a method wherein plural upright pipes are arranged in a tower so as to be separated to each other in an upper and a lower directions to narrow a gas-liquid flow passage and a gas- liquid contact means consisting of a gas-liquid contact part and a gas-liquid separation part is provided in a multi-stage fashion. CONSTITUTION:When a gas is sent from a gas supply pipe 2 while a liquid is supplied from a liquid supply nozzle 8, the gas and the liquid are violently and sufficiently contacted mainly in an upright pipe 5. After gas-liquid contact, a gas-liquid mixture reaches the upper space of the upright pipe 5 while liquid droplets are scattered to the direction of a tower inner wall by the abrupt reduction in a gas speed and the variation of a gas flow speed to carry out gas- liquid separation. Subsequently, the gas accompanying a slight amount of mist reaches the lower end of the next upright pipe in the next stage and raised therethrough to again carry out gas-liquid contact with the liquid supplied and sprayed by the liquid supply nozzle 8 in the lower and the upper spaces thereof. As the result, gas-liquid contact efficiency is extremely increased.

Description

DETAILED DESCRIPTION OF THE INVENTION The present invention relates to a multistage high flow rate gas quasi-contact iron storm that can obtain the absorption rate in one place by providing multiple gas-liquid contact stages consisting of gas-liquid contact portions and gas-liquid components #1lls. .

As a conventional gas-liquid contact device, plate towers or packed towers are generally used, but these all take measures to reduce entrainment of liquid and pressure loss. If there is a compound, slurry, etc., clogging occurs and causes trouble. In addition, a gas tower is also used, but it is essential to use a dispersion plate to disperse the VC gas in the liquid.In addition, in this case, the waste cylinder velocity is extremely low, and a large volume of waste and fluid It is not suitable for processing.

In order to process a large volume of waste and fluid, there is a high flow rate type gas-liquid contact device m (hereinafter referred to as a flow rate iron tube) that increases the speed of the waste cylinder. , JP 55-32411, JP 55-13117
It is known as No. These flow rate systems do not have internals in the chamber, and the absorption chamber is operated by bringing the supply gas into countercurrent or cocurrent contact with the liquid at a high flow rate.

However, the conventional Shoryu Meisashi Nao, for example, Tokuko Sho 55-
In the case of a vc device such as that described in Publication No. 32411, as will be described later, the pressure loss in the field is large near the feed section and the contact rate is low, but in the higher part of the column, the gas 1 & contact is not necessarily m. I couldn't see that it was being carried out effectively.

In order to obtain high contact efficiency, it is essential to install multiple A towers in series, which eliminates disadvantages such as increased cost and large size. As a result of repeated efforts to improve the above-mentioned drawbacks of the high flow rate device Vc, it was discovered that the flow state near the top of the tower was like a wet wall, leading to the present invention. That is, the present invention arranges several standpipes of vC bales in the column vertically apart from each other to narrow the gas-liquid flow path, and multi-stages the gas-liquid contact stage consisting of the gas-liquid contact section and the gas-liquid separation section. By establishing
The contact efficiency is the same as above.

The present invention will be explained below with reference to the attached drawings t-#.

FIG. 1 shows an embodiment of the present invention, in which a gas supply port 2 is provided at the bottom side of the goki l, a demister 3 is provided at the top, and a waste discharge port 4 is provided at the top end. ing. A plurality of standers t5 are arranged in the tower 1 at predetermined intervals in the vertical direction. These standpipes 5 are fixed in the tower by a bottom plate 6 which closes the gap between the lower edge of the outer edge and the inner wall of the tower 1, and a liquid receiver section 7 is constituted by the inner wall of the tower, the outer wall of the standpipe, and the bottom plate.

A Vc mineral liquid supply nozzle 8 is provided near the lower end of the substantially center of each standpipe 5 so that its jetting nozzle opening opens upward. A plurality of liquid supply nozzles 8 at each stage may be provided depending on the inner diameter of the standpipe 5. In addition, each liquid receiver s7 and the tower bottom end 1C
A discharge 119 is provided to discharge the r1 liquid out of the field.

Stripe 2 Figure 2 shows another center 'hflll of the present invention, and shows the case where the bottom plate 6 is provided above, that is, in the middle of the vertical position t5, and in this way, the gas-liquid aSS area described later is expanded. It turns out.

In addition, FIG. 3 shows still another embodiment of the present invention, in which the apparatus shown in FIGS. In contrast, in the apparatus shown in FIG. 3, the standpipes are arranged so that their central axes do not match.

In this way, in the present invention, the vertical v5 is arranged in multiple stages in the field, and the gap between the vertical v5 and the inner wall of the column is closed with the bottom plate 6, thereby narrowing the gas-liquid flow path and having the following and vc41 characteristics. It is. In such an apparatus of the present invention, when gas is supplied from the gas supply port 2 and liquid is supplied from the liquid supply nozzle 8, the gas and liquid are generated violently in the vertical pipe 5, and the gas comes into contact with light. The absorbed components in the gas are absorbed into the liquid, or the volatile components in the gas are dissipated into the gas and removed. After contact, the gas-liquid mixture reaches the space above the civil servant, and as this space rapidly decreases and expands, the droplets are blown toward the inner wall of the tower due to the sudden decrease in gas velocity and the change in direction of the waste flow velocity. Gas-liquid separation takes place. Next, the gas accompanied by a small amount of mist reaches the lower end of the next stage standpipe, where the gas is supplied and sprayed from the liquid supply nozzle 8 to cause gas-liquid contact, and then the gas and liquid are mixed in the space above the standpipe 5. A separation will take place.

The separated liquid is led to the liquid receiver part tVc and discharged through w9.
It is discharged outside the site along with the liquid that has accumulated at the bottom of the tower. Although not shown, the separated liquid after contact with the gas can be regenerated and used again as a contact liquid. The liquid may be fed to the liquid supply nozzle 8 at a lower stage by using the difference in liquid head.

As described above, in the device of the present invention, the inside of the standpipe and the extended edge of the upper end of the standpipe are mainly the gas-liquid contact area (~), and the upper end of the standpipe is the main part of the space above the standpipe. The mounting line that is separated by the extension line and the inner wall of the column is the gas-liquid part m part (B).
B) A plurality of gas-liquid contact stages consisting of Separated.

Here, a case where a high flow rate device as shown in Fig. 1 in which standpipes 5 are provided in two stages is used, and a case where a conventional high flow rate device as shown in Japanese Patent Publication No. 55-32411 is used. Regarding the raw waste, carbon dioxide gas with a concentration of 340 to 380 ppm (gas cylinder velocity 711 L/s@e) is used, while the ocular fluid is concentrated I! Using a t2.5 vt% caustic soda bath liquid (liquid temperature 28°C, liquid vL amount 400G00KP/j@HR), gas-liquid contact was carried out to absorb carbonate scum by caustic soda, and the height of the absorption tower at that time was If the pressure loss distribution in the direction and the absorption rate of CO and -NaOH are shown, they are #! It will look like Figure 4 and Figure m5. In Fig. 4 and Fig. 5, P and Q respectively indicate the positions of the liquid supply ports, and in the comparative wax of the present invention, the liquid is supplied from P and Q12J, and from P in the conventional device. Only liquid was supplied. Further, the standpipe positions in the apparatus of the present invention are shown as ST and UV. The circles in the figure indicate the results obtained using the device of the present invention in fc, and the triangles indicate the results obtained using the conventional device.

From these figures 4 and 5, in the conventional high-flow rate equipment, effective gas-liquid contact is carried out from the #'i semi-supply section to about 2 to 311 degrees, but beyond that point, the pressure loss decreases rapidly. It can be seen that the absorption efficiency also takes a nearly constant value, and absorption due to gas-liquid contact does not substantially occur in the subsequent parts. When the state of the liquid was observed in the area from 2 m to B+a from the liquid supply part, the liquid flowed like a dripping wall and became a two-phase fluid. On the other hand, the device K of the present invention is constructed so that a two-phase fluid with a flat wall does not occur, and furthermore, the absorption efficiency is improved because the liquid is supplied to bring about gas-liquid contact.

Therefore, although the height of the standpipe 5 constituting the gas-liquid contact section ((transfer) of the device of the present invention depends on the superficial velocity of the waste and the amount of liquid supplied,
Generally, it is preferable to set it to about 2 to 3 degrees. Here, the relationships among the dimensions of the embodiments of the apparatus of the present invention will be schematically illustrated as follows. Now, if the inner diameter of the standpipe 5 is D, it is preferable that the inner diameter of the column 1 is approximately 2D. Therefore, in this case, the standpipe 5 is arranged near the center of the column 1, and if the @ of receiver s7 becomes 3AD. It is preferable that the distance from the upper end of the standpipe 5 to the lower end of the standpipe 5 installed above it be approximately 3AD. Example 2 of the present invention
In a preferred embodiment, the standpipe 5 has the above-mentioned dimensional relationships.
The tube 11i1it-20. As a result, an example of each dimension will become clear since the pipe ^ of the standpipe 5 has 2 to 3 legs. However, these dimensions do not limit the present invention in any way, and the number of standpipes installed in the tower,
In other words, whether the gas-liquid contact stage is provided with a thin film or whether the central axes of the standpipes are made to be mismatched as shown in FIG. 3 is determined by the gas and/or liquid to be treated. Note that preferably the width of the liquid receiver is at least SOO simple.

The number of liquid supply nozzles 8 installed in each gas-liquid contact stage is determined according to the inner diameter of the standpipe 5. For example, if the inner diameter of the standpipe is 50.
It is preferable to use 1 gA location for 0φ, 3 locations for 50φ, and 4 locations for 1000φ.

In such an apparatus of the present invention, when the scum and liquid are supplied into the column, sufficient gas-liquid contact and gas-liquid separation are performed, and the liquid is prevented from flowing along the walls and becoming a two-phase fluid. Since the next gas-liquid contact stage is installed at a position where the gas-liquid contact efficiency almost disappears, the gas-liquid contact efficiency increases steadily.

According to the present invention as described above, the gas-liquid flow path is narrowed by a plurality of vertically spaced vertical pipes arranged in the column, and the gas-liquid contact part (^) and the gas-liquid separation part (B ), the gas-liquid contact efficiency is dramatically increased.
This means that a tower is sufficient, and a device that is advantageous in terms of cost and installation area can be obtained. The present invention is particularly suitable when the supply gas has an original pressure and when the liquid contains a polymer or a slurry.

[Brief explanation of the drawing]

Figures 1 to 3 are schematic explanatory diagrams showing embodiments of the present invention, Figure 4 is a pressure loss distribution diagram of the gas ascending section in the height direction of the tower, and Figure 5 is a Co1 distribution diagram in the vertical direction of the tower. −
A distribution map of NaOH-based absorption is shown. l...Tower 2...Gas supply port 3...
Demister 4...Gas discharge port 5...Vertical W
6... Bottom plate 7... Liquid receiver is part 8... Liquid supply nozzle 9... Discharge pipe Hayabusa 4 Figure CO2aFLA'l'f"e'llJ

Claims (1)

[Claims] 1. Inside the tower, which has a waste supply port at the bottom and a gas discharge port for pain relief, multiple standpipes are installed in a multi-tiered system with a bottom plate that vertically blocks and seals the gap between the inner wall of the tower and the outer wall of the standpipe. ni1i8i
1. The liquid receiver is made up of the bottom plate, the inner wall of the column, and the outer wall of the tower, and a liquid supply nozzle is provided near the lower end of each standpipe, and the receiver is the part and the at-discharge pipe that discharges to the outside of the tower. A multi-stage high fL continuous gas-liquid contact device.