JPS5916687Y2 - floating heat exchanger - Google Patents

Description

[Detailed description of the invention] This invention consists of a hot gas duct and a separator, and has a diameter of 10 μm.
The present invention relates to a floating heat exchanger for cement raw materials, alumina, fly ash, etc. containing the following particles, and particularly relates to improvements in a separation chamber for separating gas from powder particles after heat exchange is completed.

There are conventional floating heat exchangers that use a cyclone as a separator, and those that use inertia, collision, or gravity as shown in FIG. 1.

However, in the former case, two types of vortex flows (forced vortex flow and quasi-free vortex flow) are formed in the gas flow inside the cyclone, so the flows interfere with each other, resulting in a large pressure loss, and the separation efficiency is also reduced. On the other hand, since the air flow in the upper discharge side connecting duct is a swirling upward flow having a velocity distribution in the radial direction, the powder particles in the duct are unevenly distributed outward in the radial direction due to centrifugal force, which is disadvantageous for heat exchange.

Furthermore, in the case of a cyclone, the height of the precipitator itself is increased because the angle of inclination of the lower part is large.

As a result, when a heat exchanger is formed by stacking several heat exchange stages constructed from these stages, the pressure loss of the heat exchanger increases, and the total height increases.

In the latter case, although the pressure loss is low, powder particles within the separation chamber may be re-splattered due to the change in the direction of the airflow.
They have drawbacks such as poor separation efficiency, and when a heat exchanger is formed by stacking them in multiple stages, the thermal efficiency becomes poor.

Further, as another prior art, there is a heat exchanger as shown in Japanese Utility Model Publication No. 48-34014 (see FIG. 2).

According to this, the powder supply pipe 12 and the gas supply pipe 14 are separately connected to the main body 15 of the heat exchanger, and the gas supply pipe 1
The hot gas from 4 and the powder from the powder supply pipe 12 are not mixed well, which is disadvantageous for heat exchange.

Furthermore, a powder discharge pipe 13 is installed so that the powder and granular material is discharged in the extending direction of the air flow swirled in the connection direction of the main body 15 by the gas supply pipe 14, and the hot gas after heat exchange is The purpose of this invention is to improve the heat exchange efficiency of powder particles and the collection rate after heat exchange, eliminate pressure loss, and have a compact structure. An object of the present invention is to provide a floating heat exchanger.

In the present invention, a side wall 1a of a separation chamber 1 formed of a flat or curved surface and long in one horizontal direction is tangentially directed toward the top of one end in the horizontal length direction of the separation chamber 1 along the ceiling 1b of the separation chamber. The introduction-side connecting duct 3 has an introduction opening, and the introduction-side connecting duct 3 has a vertical duct portion 10 extending in the vertical direction and a wall surface 11a connected to the ceiling 1b, and connects the vertical duct portion 10 to the separation chamber 1. It consists of an inclined duct portion 11 having a rectangular cross section perpendicular to the axis and inclined obliquely upward,
A powder particle input pipe 7 is provided in the middle of the vertical duct portion 10, and a collection chamber 2 is provided at the bottom of the separation chamber 1 over the entire length of the separation chamber 1 in the axial direction. The other end wall 1e in the horizontal length direction is formed into a funnel shape that becomes narrower as it goes away from the one end wall 1d, and a discharge side connecting duct 4 is connected to the tip of the end wall 1e. It is a floating heat exchanger.

FIG. 3 is a perspective view of an embodiment of the present invention.

The separation chamber 1 consists of a flat rectangular parallelepiped long in one horizontal direction, and is provided with a collection chamber 2 for powder particles at its lower part.

A gas introduction side connecting duct 3 equipped with a powder particle input pipe 7 is connected to the upper part of one long side end of one side wall 1a of the separation chamber 1 so as to run along the ceiling 1b of the separation chamber 1.

The duct 3 has a vertical duct portion 10 extending in the vertical direction (up and down direction in the drawing) and an inclined duct portion 11 that is inclined obliquely upward from the vertical duct portion 10 toward the separation chamber 1 to introduce the powder particles. Pipe 7 is vertical duct part 10
is connected to.

Moreover, the inclined duct portion 11 has a rectangular cross section perpendicular to its axis, and the upper wall surface 11 a is connected to the ceiling 1 b of the separation chamber 1 .

One end wall 1d in the horizontal length direction of the separation chamber 1 is formed into a planar shape, and the other end wall 1e is formed into a funnel shape that becomes narrower as it gets farther from the one end wall 1d.

A discharge side connecting duct 4 is connected to the tip of the other end wall 1e for guiding the gas in the separation chamber 1 upward to form an upper heat exchange region.

A powder particle input pipe (not shown) to the upper heat exchange area is connected to the discharge side connecting duct 4.

The collection chamber 2 has a downwardly tapered funnel shape, and the separation chamber 1
The powder particle discharge pipes 5 are disposed at the bottom thereof, and the powder particle discharge pipes 5 are disposed at the bottom thereof.

Next, the operating state will be explained.

The mixed gas sucked from the lower heat exchange area is well mixed with powder particles from the powder particle input pipe 7 provided in the middle of the vertical duct portion 10, so that the heat exchange efficiency is improved.

Furthermore, the mixed gas is guided from the vertical duct section 10 of the inlet side connecting duct 3 to the inclined duct section 11.

At this time, the direction of the mixed gas changes from vertically upward to obliquely upward, so centrifugal force acts on the mixed gas, and the powder particles in the mixed gas are gathered near the upper wall surface 11a.

Therefore, the powder particle concentration near the wall surface 11a becomes large,
Moreover, since the wall surface 11a is a flat surface, its concentration distribution is uniform along the width direction perpendicular to the flowing direction of the mixed gas.

With the powder particles gathered near the wall surface 11a, the mixed gas is introduced into the separation chamber 1 along the ceiling 1b, forming a swirling flow with a velocity distribution in the radial direction as indicated by the arrow A.
), move in the long direction without turning.

Due to this swirling flow, the powder particles in the mixed gas are further pressed against the wall surface of the separation chamber under the action of centrifugal force, separated from the gas flow, and fall along the inner wall surface, passing through the collection chamber 2 and passing through the powder particle discharge pipe. It is discharged from 5.

Here, in the separation chamber 1, since the collection chamber 2 is provided with the lower part of the inner surface recessed below the swirling flow along the inner surface of the separation chamber, the powder once dropped into the collection chamber 2 and collected is Particles are prevented from being re-entrained by the swirling flow.

Furthermore, since the collection chambers 2 are arranged along the entire length of the separation chamber 1 in the axial direction (the total length in the left-right direction in FIG. 3), the collection efficiency is improved.

Furthermore, unlike a cyclone, two types of vortex flows are not formed, so the pressure loss within the separation chamber 1 is small.

On the other hand, the gas flow separates the powder particles while swirling inside the separation chamber 1, and further advances to the other end wall 1e, and flows through the discharge side connecting duct 4.
and is led to the upper heat exchange area.

Generally, when the radius of curvature of the portion where the swirling flow flows becomes smaller, the rotational momentum of the gas flow is constant, so the swirling force increases.

By reducing the radius of curvature of the separation chamber in which the powder particles contained in the gas stream are separated, the centrifugal force on the powder particles is increased by the above-mentioned effect.

In the present invention, since the other end wall 1e is constricted into a funnel shape, the swirling flow that is weakening inside the separation chamber 1 is strengthened.
Therefore, the separation efficiency of powder particles in the separation chamber 1 is further improved.

Moreover, the separation chamber 1 can be shortened laterally.

Since the end wall 1e has a funnel shape that becomes narrower as it gets farther from the end wall 1d, pressure loss can be reduced.

The separation chamber 1 may be formed with a curved surface other than the flat surface of the above embodiment.

Further, the collection chamber 2 may be formed in the shape of a plurality of funnels.

As described above, the present invention includes a collection chamber below a separation chamber formed by a flat or curved surface, and introduces a mixed gas of powder particles from one end of the separation chamber in a tangential direction along the ceiling to swirl the mixture. Since a flow is generated and the powder particles are centrifuged while the gas flow swirls and moves to the other end, the separation process between the gas and powder particles can be lengthened without increasing the height of the separation chamber. Therefore, separation of the powder particles and gas is ensured, and since the powder particles separated in the separation chamber have a downward inertial force, the powder particles can be easily guided to the collection chamber.

Moreover, since the collection chamber is recessed from the inside of the separation chamber and provided below, the powder particles in the collection chamber that have been separated will not be scattered again due to the influence of the swirling flow, and at the same time, they will be properly moved by the swirling flow. (The horizontal pitch prevents re-scattering due to the mutual influence of adjacent swirling flows.)

Therefore, the separation efficiency between gas and powder particles is improved.

Further, the collection chambers are arranged along the entire length of the separation chamber in the axial direction (the total length in the left-right direction in the drawing), thereby improving the collection rate.

In addition, the swirling flow moves in one direction without turning back, like a cyclone, and the amount of powder particles circulating in the separation chamber is small.
Since the pressure loss of the separator is small and the separation chamber has a horizontal axis, it is possible to obtain high dust collection efficiency without increasing the height, especially when a heat exchange device is constructed by stacking multiple separators. Beneficial.

Since the inlet side connecting duct consists of a vertical duct portion and an inclined duct portion having a rectangular cross section and a wall surface connected to the ceiling of the separation chamber, centrifugal force acts on the mixed gas in the inclined duct portion.

Therefore, the powder particles in the mixed gas have a high concentration near the wall surface, and the mixed gas is introduced into the separation chamber in a state where the powder particles are separated to some extent.

For the mixed gas, a powder particle input pipe is provided in the middle of the vertical portion of the inlet-side connecting duct, and the hot gas and powder particles are mixed well, so that the heat exchange rate is improved.

Inside the separation chamber, the powder particles will move tangentially along the ceiling and descend along the inner walls of the collection chamber.

Since the collection chamber is shaped like a funnel that tapers downward, powder particles along the walls of the collection chamber can enter the collection chamber smoothly, and the swirling flow is not disturbed. This has the excellent effect of preventing

Moreover, since the powder particles, which have a high concentration in advance, are introduced along the ceiling of the separation chamber, the separation efficiency is improved.

Furthermore, since the other end wall in the horizontal length direction of the separation chamber is constricted into a funnel shape, the swirling flow that is weakening within the separation chamber is strengthened, which also improves the separation efficiency.

Moreover, the separation chamber can be laterally shortened.

Moreover, since the end wall 1e is configured in a funnel shape that becomes narrower as it goes away from one end, pressure loss can be reduced.

Since the collection chamber 2 is disposed below the separation chamber 1 over its entire axial length, as the mixed gas of hot gas and powder particles swirls within the separation chamber, the powder particles in the gas are The concentration gradually decreases.

The amount of powder particles discharged is therefore very small.

As mentioned above, this improves the collection rate.

[Brief explanation of the drawing]

FIGS. 1 and 2 are diagrams for explaining each prior art, and FIG. 3 is a perspective view of an embodiment of the present invention. 1...Separation room, 11]...Ceiling, 1d
...One end wall, 2... Collection chamber, 3...
...Introduction side connecting duct, 4...Discharge side connecting duct, 5...Powder particle discharge pipe, 10...
... Vertical duct part, 11... Inclined duct part, 11a... Wall surface.

Claims (1)

[Scope of utility model registration request] An introduction-side connecting duct is connected to the top of one end of the separation chamber 1 in the horizontal length direction of the side wall 1a of the separation chamber 1, which is formed of a flat or curved surface and is long in one horizontal direction, in a tangential direction along the ceiling 1b of the separation chamber. 3 is an introduction opening, and the introduction-side connecting duct 3 has a vertical duct portion 10 extending in the vertical direction and a wall surface 11a connected to the ceiling 1b, and extends obliquely upward from the vertical duct portion 10 toward the separation chamber 1. A powder particle input pipe 7 is provided in the middle of the vertical duct part 10, which is separated from the inclined duct part 11 having a rectangular cross section perpendicular to the axis, and is provided in the lower part of the separation chamber 1. A collection chamber 2 is provided over the entire length in the axial direction, and the other end wall 1e in the horizontal length direction of the separation chamber 1 is configured in a funnel shape that becomes narrower as it goes farther from the one end wall 1d. A floating heat exchanger characterized in that a discharge-side connecting duct 4 is connected to the tip of 1e.