JPS60235603A - Method and apparatus for extracting liquid from composite orgas/steam mixture - Google Patents

Abstract

(57) [Summary] This bulletin contains application data before electronic filing, so abstract data is not recorded.

Description

DETAILED DESCRIPTION OF THE INVENTION (Industrial Application Field) The present invention relates to the extraction of liquid from a composite by vaporization in a carrier gas stream and aerodynamic separation of the vaporized liquid from the carrier gas. Regarding things.

In this specification, the term vaporization is used in a broad sense to include the production of steam by chemical reactions such as combustion. Similarly, the term "composite" does not refer to a substance that contains a liquid component, such as wet barley, paper, paper, or gypsum; It is used in a broad sense to include substances that form vapor when mixed with other substances (such as fuel oil, coal, peat, and anything that burns in the air, such as charcoal).

More particularly, the present invention relates to a method for placing working energy in a work area to perform a separation operation.

According to the invention, this working energy is supplied as mechanical energy to the carrier gas by means of one or more blowers, which blow the main stream of the gaseous mixture against its head losses. Vapor separation occurs in an aerodynamic separator with no moving parts, whether closed or open, moving through the entire vaporization and separation circuit.

The first application of the present invention is to industrial drying, where durable and cheap equipment such as blowers and aerodynamic separators are used instead of expensive equipment that is prone to failure such as heat pumps. It recovers water vapor and latent heat from a steam mixture.

A second application of the present invention is the extraction of acid gases such as sulfur dioxide and nitrogen oxides from smoke gases produced by combustion in boilers, furnaces, and incinerators using the above-mentioned durable and inexpensive equipment. The energy consumption is low and is fully compensated by the recovery of latent heat through steam condensation.

The invention has a third application in extracting and increasing the latent heat of vapor condensation in gas/steam mixtures using the robust and inexpensive equipment described above. This application includes methods and equipment for heating, ventilation and air conditioning.

Other applications of the invention will become apparent from the description below.

PRIOR ART AND ITS PROBLEMS In the installation disclosed in French Patent No. 2,535,445 hot air is used as a carrier gas to extract moisture in the form of steam from the composite to be dried. Water vapor is then separated from the carrier air by cooling the air/steam mixture below its dew point and under constant pressure, and separating and collecting the water that condenses therefrom.

For cooling of air/steam mixtures and heating after water separation,
A heat pump condenser and vaporizer are used in series.

The working energy for water separation is supplied as compression work of the working fluid of the heat pump.

Such installations require expensive and failure-prone compression heat pumps that use specialized working fluids at fairly high pressures, as discussed above.

In the method disclosed in French Patent Publication No. 2 444 882, compressed air is used in an air ejection unit to create an aspiration effect that allows the pipes to be dried to be continuously evacuated. After being mixed with the diffusion air in the emitter, the degassed mixture of carrier gas and water vapor is compressed in the diffuser and rejected to the outside without separating the water vapor from the mixture. The working energy for vaporizing the water in the pipe is supplied in the form of external compressed air. The energy efficiency of this method is very poor due to the use of emitters and the need for a high degree of vacuum to allow a sufficient drying effect.

US Pat. No. 3,977,850 discloses a centrifugal separator that separates the liquid content contained in the form of droplets in a gas stream by directing the fluid mixture tangentially to the diameter of the conduit. This device centrifugally separates the liquid phase from the gas phase in a two-phase flow.

Working energy to separate droplets from the mainstream - is the pressure difference of the liquid mixture in the separator.

In this separator, the main stream undergoes two successive diffusions that generate inertial energy, one in the centripetal spinner in the charge zone of the volute pipe, and the second in the discharge zone of the volute pipe. occurs in the discharge nozzle. The inertial energy generated in the fluid by the spinner in the vortex pipe is almost completely lost due to the friction between adjacent streamlines; likewise, the energy performance of the emitter is extremely low;
Only a small portion of the inertial energy of the fluid flowing out of the nozzle at the end of the swirl pipe is recovered in the form of pressure.

From this, the diffusion of the gaseous components of the fluid mixture in this separator is almost isenthalpic. This fact is
This precludes any possibility of separation of the vapor mixed with the carrier gas flowing through the separator, including condensation and subsequent inertial separation.

Belgian patent 514256 discloses a device with the purpose of agglomerating fine solid or liquid particles pre-existing in a carrier gas, in which fine particles of agglomerated liquid are added to the carrier gas. Compressed air is added by air jet to atomize the droplets. An aerosol or a gas stream containing microscopic droplets is passed through a Venturi tube at high subsonic velocity, and the mechanical impact between the particles causes the microscopic particles to agglomerate into larger rasters or particles, which subsequently reduce their size. be sufficient to enable capture by cyclone collectors. The size of the clusters or particles thus obtained can be determined by ionizing the particles at the entrance of the Venturi tube and/or by subjecting the flow from the Venturi tube to a sonic or supersonic standing wave generated by a siren prior to particle collection. By exposing it, it becomes even bigger.

The working energy producing said mechanical impulse is the pressure difference of the fluid mixture in the Venturi tube, external compressed air is used for the air jet and siren, and electricity is used for the ionization of the fine particles to be agglomerated. used for.

This device is capable of increasing the size of pre-existing particles in a two-phase fluid stream consisting primarily of carrier gas by agglomeration without changing their total mass. During the passage of the two-phase fluid stream through the convergence zone of the Venturi tube, the vapor mixed with the carrier gas partially condenses in the form of fine droplets as a result of approximately isentropic diffusion of the vapor and carrier gas mixture. There is.

Also, the droplets, as well as particles contained in the incoming fluid stream, may form agglomerates. However, since no particle collection device is provided near the throat of the Venturi tube, particles remain contained in the mainstream in the expansion region of the Venturi tube, and the carrier gas is heated by approximately isentropic recompression. , the liquid droplets that had been generated by condensation during diffusion are revaporized; such revaporization is complete, if not completely at the outlet area of the Venturi tube, a little beyond it. Put it away.

Because of this, the Venturi section of the separator described in the Belky patent is incapable of separating vapor from a carrier gas contained in a one-phase globular fluid stream.

GB 1283587 discloses a method and apparatus for separating the components of both light and heavy gas mixtures. The method includes: (a) accelerating a gas mixture in a nozzle to form a supersonic diffusion flow in a duct located downstream of the nozzle;

(b) having a plurality of holes facing upstream and forcing the shock wave to form upstream of the tip of the probe means to interrupt the flow on an axis (or the nozzle axis) branching from the nozzle axis at a plurality of transverse intervals; a hollow probe means extending across the width of the duct is placed in the diffusion stream at a sufficient distance from the nozzle to permit removing the probe from the hollow probe means through a channel.

German patent application 2301467 shows a method similar to that disclosed in the above-mentioned British patent, the difference being that probes are installed in at least three different areas of the duct following the supersonic diffusion nozzle. It is in.

The methods described in such British patents and German patent applications rely on the inertial effects produced on the various components of the gas mixture by extremely large decelerations that cause the molecules to move into a stagnant zone immediately after passing through a stationary shock wave. are doing.

It is necessary that the free stream Matsuha number be substantially greater than 1, preferably on the order of 2 to 3 or more. Typical Nusen numbers range from 0.02 to l
It is stated that the isentropic stagnation pressure range for O is from high vacuum to 100 Torr.

The working energy of gas separation is the pressure difference of the fluid mixture in the separator.

The energy performance of such methods and devices is extremely low since the inertial energy loss in the steady shock wave is extremely large. Moreover, very low absolute pressures are required, which is impracticable in the field of application of the invention.

These facts exclude the possibility of separating the vapor mixed with the carrier gas flowing through this separator by condensation prior to inertial separation.

French patent 1230416 discloses a method and apparatus for separating gaseous or vaporous substances, more particularly gaseous mixtures of isotopes.

This method relies on differences in the diffusion rates of different molecules in a gaseous mixture.

The gaseous mixture is initially passed through an ultrasonic nozzle with a diffusion pressure ratio of more than 1000.The effluent stream of the 6 nozzles is introduced into a container in which the inertial energy is recovered without taking any special precautions. The partially branched, unbranched stream is introduced into the second vessel via a truncated cone with wide-angle holes, and the stream is withdrawn at a pressure less than 5% of the pressure of the gas stream entering the ultrasonic nozzle.

The working energy of gas separation is the pressure difference of the fluid mixture in the separator.

The operating conditions in this separator are substantially similar to those described in the aforementioned British and German patent applications.

Due to the extremely low energy efficiency of this separator, the implementation of the present invention in the field of application is not possible and there is no possibility of separating the vapor mixed with the carrier gas flowing through the separator by condensation prior to inertial separation. is also excluded.

US Pat. No. 3,109,721 discloses a method and apparatus for separating fluid mixtures by sonic energy.

This method continuously introduces sound energy into an enlarged cross-sectional area to generate sound waves having an energy gradient, and
By charging this zone with a fluid mixture of multiple components,
It relies on the fact that a fluid mixture of multiple components is separated into a region rich in heavy components and a region rich in light components. The light component-rich portion is condensed in a second zone having a relatively small cross-sectional area.

The charging of the inlet stream and the withdrawal of the stream rich in light and heavy components takes place perpendicular to the axis of the truncated cone in which the resonant standing waves are generated.

As shown in the figures included in the specification.

Separation rate is quite small, feed rate is from 160 to 2640c
c/hour range.

The working energy in this separator is the sound energy generated at the throat of the truncated cone, not the pressure difference of the gaseous mixture in the separator.

A gaseous mixture enriched in light and heavy components is produced in opposing regions of the separator.

This method has very low working efficiency.

This fact excludes the possibility of implementing the invention in the field of application for separating vapor from carrier gas.

Belgian patent 898745 discloses a method and apparatus for separating fluid mixtures with application to gaseous component mixtures.

The method relies on the generation of a resonant acoustic standing wave that interacts with the tip of a moving annular vortex in a gaseous mixture flowing subsonically as an annular flow with cross-sectional area changes through multiple axisymmetric cavities. . As a result of the acoustic pressure field and the strong centrifugal cuff field within the vortex, a spatial separation of a given component of the gaseous or vaporous mixture occurs, which enriches this component via axial and circumferential splitters or traps. This makes it possible to branch gaseous mixtures.

The working energy for separating the inlet gaseous stream into a main exhaust gaseous stream and a branch exhaust gaseous stream of different components is the pressure difference of the gaseous mixture in the separator.

The aerodynamic separation method and device allows for partial separation of vapor mixed with a carrier gas into a vapor-rich substream and a carrier gas-rich main stream.

This method is extremely energy inefficient because the generation of interacting vortices and acoustic standing waves requires walls and flow separation from the recirculation: such a method is While pressure recovery is very low due to losses, it is necessary that a significant amount of inertial energy be generated from the pressure of the gas stream.

Given this, the adiabatic diffusion of the gas stream in this separator is almost isenthalpic.

This fact eliminates the possibility of condensation of the vapor mixed with the carrier gas prior to the inertial separation of the resulting liquid droplets.

To summarize the prior art: None of the known methods and devices separates the vapor from the carrier gas or separates the vapor as a vapor-rich branched gaseous stream with an energy efficiency so low that it is impracticable in the field of application of the present invention. (Objective) The purpose of the present invention is to The extraction of liquid from the composite by vaporization in a gas stream and subsequent separation of the vaporized liquid from the carrier air increases energy efficiency when implemented in the application areas described here, as well as in heat pumps, etc. The object of the present invention is to provide an improved method and apparatus that do not require expensive and failure-prone equipment.

Another object of the invention is to aerodynamically separate a vapor mixed with a carrier gas into a liquid in an aerodynamic separator having no moving parts, and to reduce the pressure difference of the fluid mixture within the separator. An object of the present invention is to provide an improved method and apparatus in which the main working energy source is:

Other objects, advantages, and features of the present invention will become apparent to those skilled in the art upon reference to this specification and accompanying drawings.

(Structure) In the method and apparatus according to the invention, a carrier gas is fed into the circulation path and extracted from the composite by the vaporization action of the liquid. This mixture of vapor and carrier gas is then introduced into an aerodynamic separator in which the working energy for performing the separation is given by the pressure difference of the air/steam mixture across the separator. Most of the vapor contained in the carrier gas is extracted from the main flow of the carrier gas by the action of the separator, and the branched stream from the first separator contains a large amount of vapor and/or liquid extracted material. If at least a portion of the extracted material is vapor, the vapor contained in the substream is then largely condensed in a heat exchanger, giving its heat of condensation to the main stream of carrier gas exiting the separator. When used in a closed circuit, the carrier gas thus reheated is fed into the charging castle of the circuit and recirculated through the same circuit. In addition, when used in an open circuit, fresh carrier gas is continuously heated in the heat exchanger by the main discharge of the spent carrier gas and by the discharge from the separator of a substream containing separated vapor.

Substantially all of the energy required for the process is provided as mechanical energy, which drives one or more blowers to blow the gaseous mixture against the head losses that occur throughout the blocked or open circuit. move the mainstream of

According to one particular embodiment of the invention, the basic shape of the aerodynamic separator is a converging-diverging nozzle. The mixed flow of steam and carrier gas undergoes adiabatic and quasi-isentropic diffusion in the nozzle convergence region, resulting in a high-speed flow.The steam entrained in the flow becomes condensate as small droplets, but this occurs in the nozzle convergence region. In order to further enhance this condensation effect, auxiliary means can be provided in the nozzle charging area. Since the condensate droplets have a higher specific gravity than when they were in the vapor state, they agglomerate and diffuse due to their inertia in the meandering flow of the compound. A droplet collection chamber is provided in the nozzle throat. This collection chamber is arranged axially and along the inner wall of the nozzle, and immediately after passing through the throat of the separation nozzle, which intersects the droplet flow path, the high velocity stream of carrier gas passes through the separation nozzle. enters the diffusion region of the fluid, where its inertial energy brings about adiabatic-quasi-isentropic recompression of the fluid.A part of the vapor contained in the introduced fluid is separated as a liquid, so that the gas extracted from the separation nozzle The specific enthalpy of the stream is higher than the incoming stream and therefore hotter. Therefore, this discharged flow can be used as a heat source.

According to yet another particular embodiment of the invention, in the aerodynamic separator vessel the mixed stream of vapor and carrier gas undergoes an adiabatic, quasi-isentropic diffusion consisting of a stable component and an oscillatory component; Some of the steam condenses into droplets.
4 + - & Bakachu ILmu X tool ↓ Iji zero Iz X ubl
A droplet collection chamber is provided in a zone that intersects the droplet channel in the discharge area. A stable component of diffusion is obtained by reducing the cross section of the fluid. The vibrational component of diffusion is obtained by the action of high frequency or ultrasound waves within the flowing fluid. Along the oscillation range, the diffusive phase changes into a compressed phase in which it attempts to revaporize the vapor droplets condensed in the diffused phase. However, condensation dominates vaporization because such revaporization occurs only at the droplet surface, whereas condensation is a normal phenomenon in gas softening. After maximum diffusion of the mixed stream and dispersion of the condensed droplets, the high velocity gaseous stream enters the diffusion zone where pressure recovery occurs by adiabatic, quasi-isentropic recompression.

(Example) In the first diagram, the drying process is carried out in a container 1, in which a composite material such as moist germinated barley 2 is placed on a tray 3. The blower 4 operates together with a burner 5, which is supplied with combustion air 6 and fuel 7 to produce combustion gas 8, which is mixed with drying air 9. The burner 5 is adjusted so that the drying air in the lower part 10 of the container 1 reaches a predetermined temperature.

Said air passes through the moist germinated barley layer 2 through the upper part 11 and from the lower part 11, which fluctuates during the drying process.
It is discharged from the container l at a temperature ~30° lower. The humid air sucked by the blower 4 in the upper part 11 of the container 1 is blown into a duct 13 as indicated by the arrow 12 and introduced into the aerodynamic separator 14. In this separator 14, the introduced humid air stream is separated into a main stream 22 consisting of moist hot air and a branch stream 20 consisting mainly of cold water and discharged from the duct 21. The main stream is conveyed through the duct 23 to the position indicated by the arrow 9, and the drying process is performed again.

A valve 25 is provided in the duct 23 so that air leaked from all the equipment into the outside air can be replenished.

FIG. 2 shows a variant, in which the air stream 15 discharged from the aerodynamic separator 14 is conveyed via a duct 16 to a heat recovery exchanger 17, a branch 18 from the zero separator 14.
is rich in water vapor and is sent from the duct 19 to the heat exchanger 17, which transfers its heat to the main stream 15 via the heat exchange wall. The branch stream 18 is thus cooled and the water vapor is concentrated and removed from the duct 21 as indicated by the arrow 20. The mainstream heated in the heat recovery exchanger 17 is indicated by arrow 2
It is carried like 2.

As shown in Figures 1 and 2, the method of the present invention is extremely simple. Under steady-state conditions, the energy required for carrying out the process is essentially supplied by the blower 4 as mechanical energy.

The fuel combustion required by burner 5 is achieved by blower 4
The method of the present invention requires a large amount of investment and maintenance costs, compared to the known method, which requires a very small amount of airflow compared to the case where the air flow 9 is discharged from the outside air and the air flow 9 is introduced entirely from the outside air. Energy consumption can be kept to a minimum without any problems.

In fact, all existing methods in this field require a blower 4 and a burner 5. Even if a heat exchanger 17 is used, all existing methods require equipment to recover heat from used air to fresh air, and the investment and maintenance costs thereof are not significant.

The aerodynamic separator 14 is a stationary device and its investment and operating costs are also modest.

In the embodiment shown in FIG. 3, along the axis of the zero separator 26 the moist air flow is introduced into a vertical separator 26 in the form of axially symmetrically convergent-divergent nozzles, with a small-diameter cylindrical collector 27. Humid air introduced in a direction parallel to the axis of the separator in which the separator is installed enters the upper chamber 28 in which means can be provided for creating nucleation centers within the flowing fluid. The means are:
devices for atomizing droplets of water or other substances that stimulate nucleation, and/or sound waves to ultrasound waves and/or e.g. ultraviolet light;
It can consist of devices that generate electromagnetic radiation with appropriate wavelengths, such as laser lines, ionizing radiation, radar waves, and/or electrostatic radiation.

The moisture stream then enters the convergence zone 29 of the separator 26 and diffuses, causing said condensation into finely dispersed droplets on the outer surface of the capture collector 27 and on the inner surface of the separator surrounded by the collection chamber 30. radiated upwards. Over the entire capture length of the collectors 27 and 30, the surfaces thereof are formed of porous material or other known permeable structure materials, through which the condensate consisting of droplets flows into the collectors 27 and the collection chamber 30. from which it is conveyed out of the main circuit by known means.

After the above-mentioned droplet separation is completed, the air flow moves from the throat of the separator 26 to the expansion chamber: it undergoes adiabatic and quasi-isentropic recompression, returns to a level close to the pressure in the upper chamber 28, and returns to the upper chamber 28. 0 rising to a higher temperature level than chamber 28
The throat of the separator has an area of sufficient length to provide effective collection of condensate.

The flow velocity in any part of the main flow in the separation nozzle 26 has only an axial component and a radial component,
It does not have a tangential component; however, the charging area of the separation nozzle 26 may be provided with undulating blades to induce a free swirl flow that overlaps with the axial and radial flows. , which may be of small amplitude compared to the axial and radial components of the mainstream flow velocity, assist in ejecting the condensate droplets onto the inner surface of the collection chamber 30, thereby increasing the droplet separation effect.

Although the method and apparatus of the present invention are capable of a number of modifications, it is necessary to mention in particular those shown in Figures 4 and 5.

FIG. 4 shows a main modification of the upper part of the separation nozzle 26 shown in FIG. A plurality of wing pieces are arranged. The series blades impart a tangential component to the vertical flow of the main stream, thereby forming a free swirl flow with an appropriate spread in the vertical flow. Due to the characteristic shape of the convergence zone, the axial component of the vertical flow is gradually replaced by a central radial component and gradually disappears, so that the droplet is controlled by the tangential component of the condensate droplet dropping velocity. A speed change area is formed which has the effect of horizontally moving the main flow toward the outer wall of the convergence area 29 and transferring it against the pressure gradient of the main flow. The condensate reaching the outer wall is sucked into the collection chamber as in the third illustration. Such a special configuration makes it possible to improve the efficiency of droplet separation during diffusion. At the end of this diffusion, as shown in Figure 4, the central radial flow changes direction and becomes an axial flow again by recompression in the convergence zone of the separation nozzle.

In FIG. 5, the main stream of fresh air introduced at 37 is fed into the AC heat exchanger 38, where it is passed through the separation nozzle 26.
It is heated by a stream of dry hot air 22 discharged from.

The main air stream thus heated in the heat exchanger 38 is then introduced into the blower 4 via the duct 39 and fed into the drying container 1 as indicated by arrow 9. The main stream of humid air 12 discharged from the drying vessel l is then introduced into an aerodynamic separation nozzle 26 from which a substream mainly consisting of condensate is separated and discharged as 20, and the main stream of dry hot air 22 is subjected to AC heat exchange. It is fed into a vessel 38, cooled to near ambient temperature, and then released to the atmosphere at 40. Compared to the embodiment of the invention shown in FIG. 1, the modified embodiment of the invention shown in FIG. 5 differs in that a heat exchanger 38 is added. As shown in FIG. 5, when processing in an open circulation system according to the invention, the gas flow passing through the drying vessel can be permanently renewed with only a slight increase in energy consumption. This increase in energy consumption is due to an increase in the output of the blower 4 due to pressure loss due to the addition of the heat exchanger 38, as well as an increase in the output of the blower 4 caused by the addition of the heat exchanger 38.
This is caused by the additional amount of heat to be supplied by the burner 5, which has to be increased in order to partially cover the temperature difference between 0 and 0.

The embodiment shown in FIG. 6 shows an application of the invention for drying humid air. This is carried out in a separator vessel 61 whose basic shape is a symmetrical nozzle. No. 61ii! ! As shown, these components are connected to each other in a curved manner so as not to form a cusp in the axial section of the nozzle. The moist air stream entering the nozzle is forced down generally in the direction of arrow 66. Moisture is pumped into cylindrical chamber 62, where it is generated from surrounding ring 67 using any type of sonic generator known in the art. In response to the acoustic radiation, the front surface of the sound wave in the air inflow castle of the convergence zone 63 is made to form a spherical surface 68 whose geometrical center point lies on the nozzle axis below the minimum part of the narrow passage part 64. There is.

Adiabatic, quasi-isentropic diffusion of the flowing fluid occurs within the frustoconical convergence zone 63. This stable component of diffusion is provided by a decrease in the fluid cross-sectional area between the inlet of the convergence zone 63 of the nozzle 61 and the throat 64. The oscillatory component of this diffusion is provided by a spherical acoustic wave whose tip wave advances from 68 to 610.

All flows within the convergence zone 63 are perpendicular to the acoustic sphere and 6
Convergence area 63 forming a straight line converging to the focal point located at 9
Due to the combined effect of steady diffusion and oscillatory diffusion of the fluid moving within, a portion of the water vapor contained in the moisture inlet stream condenses into droplets. Since the specific gravity of these droplets is about 1000 times greater than the specific gravity of the moisture entering the nozzle throat 64, the droplets flow generally in a straight line toward the focal point 69 and intersect within the nozzle throat 64. It is only slightly deviated from the straight flow path by the air flow.

These droplets are then arranged along the axis of the nozzle enlargement 65 and have a small diameter such that the center of the inlet hole cross section coincides with the focal point 69 or is located slightly below this point in the flow direction. is collected in a hollow cylindrical collection chamber 611.

The residual gas flow that separates the agglomerate droplets in the nozzle throat region enters the enlarged diameter section 65 and undergoes adiabatic, quasi-isentropic recompression, absorbing the inertial energy imparted at the nozzle throat. Convert to enthalpy.

As shown in Figure 6, the working energy required to separate the fluid mixture within the nozzle 61 is substantially supplied as a pressure difference of the fluid mixture across the separating nozzle, and the amount of acoustic energy radiated by the sound waves is equal to the working energy. It only accounts for a part. Furthermore, the required amount of energy for the acoustic radiation may be provided from the working energy by an acoustic effect connecting the surrounding ring 67 and the fluid in the nozzle top 62.

One embodiment of the invention utilizes acoustic radiation generated within the moisture main stream by a blower. A blower increases the flow pressure of the main stream. Such acoustic radiation is emitted by an optional blower both as a downward flow and also as an upward flow. The acoustic radiation may be intensified as necessary to form a mental spherical wave directed to a focal point located at point 69. Alternatively, the wave tip of this acoustic radiation may advance in the direction opposite to the flow of the main flow, and in this case, the shape of the wide diameter part of the separation nozzle is also truncated, similar to the shape of the convergence zone of the nozzle. It is necessary to have a conical shape.

Whether the wave front of the acoustic radiation is advanced or retracted within the separation nozzle, its energy peak is imparted within the throat of the nozzle.

Instead of generating acoustic radiation from fluid pressure or using acoustic radiation generated using a blower, the possibly required acoustic radiation can be generated separately, for example by electromagnetic variation! g! It can be generated using a sound generator such as a horn or a siren. In this case, the acoustic energy is supplied from an external source.

Although the method and apparatus according to the present invention have been described above with reference to specific examples for industrially applied drying treatment, the application of the present invention is not limited thereto. When separating and extracting a composition from the mixed gas, the mixed gas is subjected to adiabatic and quasi-isentropic diffusion, whereby the composition to be extracted is partially condensed and is widely applied to separate as a condensate.

The composition of the condensate thus obtained depends on the composition of the gas mixture to be treated.6 For example, when the method of the present invention is applied to treat smoke from a coal-burning industrial boiler, the condensate obtained is pure water. Not 502 -No・NO2・C0
It is called an aqueous solution of one or more components contained in secondary smoke.

This is very characteristic, since not only can condensable vapors be treated, but even gases that are difficult to condense can be treated according to the invention if they are soluble in the condensate of easily condensable vapors. This means that it can be used as a target for separation and removal processing. Such condensable steam thus has a cleaning or sorting effect.

If the vapor content in the carrier gas is insufficient to extract the specific gas to be separated from the carrier gas, or if the extraction action itself is insufficient, the mixture to be separated may be Components capable of having a cleaning or sorting effect on the above-mentioned specific gases in the form of gases and/or liquids and/or solids (droplets or particles in suspension) may be added to the mixture. Sulfur 1so2 is very easily adsorbed by the added chain acid and the vapor is easily condensed,
Easily adsorbed by water vapor condensates. Thus 30
2 can be separated and extracted and recovered by treating the separated liquid by any known means.

According to the method and apparatus according to the embodiment of the present invention shown in FIG.
Since the ratio between the initial pressure of the gas mixture to be treated and the instantaneous minimum pressure of the gas mixture during flow can be extremely large, the region of steam and gas that can be extracted in this embodiment is extremely wide. It corresponds to the product of the pressure ratio of the stable component of diffusion and the pressure ratio of the oscillating component of diffusion. The greater the overall pressure ratio obtained, the greater the enthalpy drop and accompanying temperature drop that occur after diffusion, and the greater the separation effect due to condensation.

In fact, the present invention can be applied to the extraction of any liquid from a compound, without any limitation, the compound to be treated having any composition of several chemical or isentropic components. The liquid to be extracted may be a single substance or a mixture or combination of several chemical or isentropic components in any composition; the carrier may be a mixture or a combination; The gas may be composed of any components of any composition.

The present invention can have many embodiments without departing from its scope, and all matters described herein or shown in the attached drawings are merely illustrative and should not be construed as limiting in any way. must not.

[Brief explanation of the drawing]

Figure 1 shows an example in which the present invention is applied to a blockage type industrial drying process, and Figure w42 shows a modification of the blockage process type in which an aerodynamic separator is used to produce water vapor instead of liquid wood. FIG. 3 shows a converging-expanding separation nozzle according to an embodiment of the present invention, and FIG. 4 shows a converging part of the converging-expanding separation nozzle. FIG. 5 shows an example of the application of the present invention to an open process industrial drying process, and FIG. 6 shows a special embodiment of an aerodynamic separator, in which a spherical This shows a type in which high-frequency sound waves are placed on a diffusion flow within a truncated cone-shaped convergence section, and fluid pressure is recovered at a diffusion section within the truncated cone-shaped enlarged section. Patent Applicant Bergo Neucleur Société φ Anonym Agent Patent Attorney Shuhei Matsuoka Figure 1 Figure 3 Figure 6 Procedural Amendment (Voluntary) May 24, 1980 Name Bergo Neucleur Italian Société Nationality As per Belgian Country Attachment

Claims (3)

[Claims] (1) At least a portion of the liquid contained in the composite by vaporizing the liquid in an open or closed circuit in a carrier gas stream and then separating at least a portion of the vaporized liquid from the carrier gas stream. The separation is carried out in an aerodynamic separator with no moving parts, and the substantial energy source required for the separation is provided by at least one blower for transporting the carrier gas. It is characterized in that it is given by the pressure difference of the carrier gas across the entire area inside the separator. Liquid extraction method. (2) The aerodynamic separator (a) accelerates the mixture of seedlings and carrier gas adiabatically and quasi-isentropically at the 1112-level of the Ilv*-expanding nozzle, thereby (b) passing a fluid through the throat of the nozzle at a high velocity while diffusing it so that the diffusion results in condensate droplets of liquid material condensed from the mixture; (b) in the axial direction of the nozzle and along the nozzle wall; and (C) extracting the condensate droplets from the fluid in the nozzle throat by a collection means disposed at a point intersecting the flow path of the droplets; and (C) a mixture of carrier gas and residual vapor; 2. The liquid extraction method according to claim 1, wherein the high-speed flow of the nozzle is adiabatically and quasi-isentropically decelerated in the enlarged portion of the nozzle. (3) At least a portion of the liquid contained in the composite by vaporizing the liquid in an open or closed circuit in a carrier gas stream and then separating at least a portion of the vaporized liquid from the carrier gas stream. (a) an aerodynamic separator without moving parts in which the substantial energy source required for the separation action is provided by a pressure difference in the carrier gas across the vessel; (b) at least one blower for transporting carrier gas against a pressure difference across the separator. (0) The aerodynamic separator (a) has a throat portion, and allows a mixture consisting of steam and a carrier gas to pass through the throat portion at high speed while diffusing the fluid, and as a result of the diffusion, the mixture is separated from the mixture. a converging-diverging nozzle for producing condensate droplets of condensed liquid material; (b) disposed along the axis of the nozzle and along the nozzle wall and intersecting the flow path of the droplets; (C) collecting means for adiabatically and quasi-isentropically extracting and collecting the condensate droplets from the fluid in the nozzle throat; 4. The liquid extraction device according to claim 3, further comprising means for adiabatic and quasi-isentropic deceleration.