KR0119766B1 - Vaporizing and concentration drying apparatus and method - Google Patents

Abstract

The latent heat of vaporization obtained by liquefying the heat of vaporization of vapor discharged from the vacuum evaporation or pressure evaporation process is reused for the sake of evaporation energy-saving. The offensive odor and vapor impurities in condensate water are removed by oxidization burning or carbonization at high temperature to give clean distilled water. The high temperature heating energy of water vapor is adsorbed as vapor preheating energy by the heat-exchanger system and reused to produce the high temperature vapor.

Description

Evaporation and Evaporative Concentration Drying Apparatus and Method with Steam Purification Capability

1 is a partial cross-sectional view of a preferred embodiment of the present invention.

2 is a partially enlarged perspective view of the heat vapor heat exchange recovery apparatus of the present invention.

3 is a partial cross-sectional view showing the heat exchange change in the heated steam heat exchange recovery apparatus of the present invention.

4 is a partially enlarged perspective view of the stirring blade and the steam heat exchange panel of the present invention.

5 is a partially enlarged front view of the panel type steam chamber of the present invention.

* Explanation of symbols for main parts of the drawings

1: evaporation object storage tank 10: stirring evaporation and evaporation concentration dryer

11: depression 11s: screw

12: stirring blade 13: panel type steam chamber

14: steam chamber 15 (a), 15 (b): inlet

16: connector 17: overflow prevention chamber

18: U type trap 20: Steam compression turbine

21: preheating air supply control valve 30: steam compression pump

40: auxiliary boiler 41: burner

42: coil type steam heating tube 43: steam heating chamber

50: condensate storage tank 51: regulator

52: drain valve 60: heated steam heat exchange recovery unit

R: Coiled Tube R1-R10: Pipeline

The present invention is to liquefy the vaporization heat of water vapor generated in the process of reduced pressure evaporation or pressure evaporation (latent heat) of the vaporization heat (539 kcal / l in the case of water) Odor and BOD, COD which save energy by regenerating oil and it is contained in water vapor and together evaporates together to deteriorate the water quality of condensed water. Evaporation and evaporation drying drying with steam purification ability to provide clean water condensed water by oxidizing or carbonizing and removing evaporation gas (water vapor impurity) at high temperature. (Iii) The apparatus and method.

Conventional evaporators require an additional amount of cooling water required in the condensation process, in addition to the amount of heat required for evaporation, that is, the amount of heat to boiling point (100 kcal) and the heat of vaporization (latent heat) 539 kcal / l. In the case of distilled water evaporated, vaporized, and condensed through this process, the odor of the odor component of the evaporation object and the B.O.D., C.O.D. Some of the contaminants such as water are vaporized together with the water vapor to be contained in the water vapor and then liquefied. Therefore, the water quality of the distilled water is out of the allowable standard value, and the secondary treatment is inevitably necessary to improve the water quality of the distilled water that falls below the standard. .

In other words, until now, the evaporation apparatus and methods so far cannot reuse the latent heat (539 kcal / l) contained in the evaporation heat during evaporation, but rather, it is thrown out through the condenser system of the cooling condensation process at a high cost. Resulted.

Furthermore, the odors of various odors and the B.O.D., C.O.D. In order to improve the quality of the distilled water because it is not able to remove impurities such as such, it is required to go through another secondary water treatment process, there is a disadvantage that the treatment method is complicated and excessive treatment cost is required.

In addition, even if the vaporized water vapor is evaporated using the reduced pressure evaporation method, the amount of heat for evaporation can be saved as much as the reduced pressure depending on the degree of vacuum. BOD, COD Since such a method is used, a secondary treatment is also required when only the above method is used for deodorization and purification.

However, the evaporator or evaporative condenser of the present invention regarding the evaporation and concentration drying apparatus and method having the steam purification ability overcomes these disadvantages and improves the quality thereof. Its purpose is to save energy by minimizing evaporation energy as well as providing distilled water.It can be used for the distillation water purification treatment of contaminated wastewater and the concentration and drying treatment of various environmental polluted sludge. have.

In addition, B.O.D., C.O.D. In order to remove impurities such as impurities and odors, hot steam heated to a high temperature may be recovered as needed by the heated steam heat exchange recovery apparatus of the present invention, thereby significantly reducing the steam heating fuel cost.

Looking at the present invention in more detail in the conventional evaporation method and technology 100kcal for reaching the boiling point 100 ℃ when the amount of heat required to evaporate 1L water based on the atmospheric pressure of 0 ℃ In addition, the total amount of vaporization heat required for evaporation is 539kcal and 639kcal is required. When using a gas, water is boiled at 35 ° C. at a vacuum degree of about 10 Torr (750 mmHg). In cm2 · A, the latent heat is about 570 kcal.)

However, such a conventional reduced pressure evaporation or heating evaporation or heating evaporation apparatus and technology requires a large amount of cooling water for heat exchange by using a condenser to condense and liquefy vaporized water vapor. Was unable to reuse his latent heat (539kcal).

In conclusion, the conventional reduced-pressure evaporation or heating evaporation apparatus and technology require 639 kcal of calorie energy to evaporate 1 liter of water, and additional energy from cooling water supply and circulation of the condenser must be added. In the process, 539 kcal of vaporization is a result of spending a lot of money. In addition, the gas evaporated in the decompression or heat evaporation system of the prior art includes the odor and the B.O.D., C.O.D. These substances are mixed together by evaporation, and there is an uneconomical disadvantage in that they can be discharged only after a specific method of wastewater treatment in order to remove such water vapor impurities and odors.

However, when using the present technology and method can overcome and improve the above-mentioned disadvantages of the prior art and method, the process and apparatus according to evaporation, vaporization, condensation, liquefaction Not only can it drastically reduce the cost, but it also saves energy by 2-10 times more than the conventional technology by regenerating the heat of vaporization, and the odor or impurities contained in the water vapor can also be recovered at the same time without the separate wastewater treatment device. Evaporation and Evaporative Concentration Drying Apparatus and Method with Simple and Excellent Performance of Steam Purification by Oxidation, Combustion or Carbonization to Improve Condensate Water Quality will be.

Hereinafter, described in detail by the accompanying drawings as follows.

First, the apparatus of the present invention will be described as shown in Figure 1, the coiled tube (R) is built-in and the evaporation object inlet (15a) is provided at the top for the condensate waste heat recovery function The upper portion of the evaporation object storage tank (1) and the agitated evaporation and evaporation concentration dryer (10) capable of storing water, for example, wastewater, are provided with an evaporant inlet (15b) which can be used according to circumstances. The lower part has a circular cross section and forms a depression 11 on one side, and there is a screw discharged screw 11s, and as shown in FIG. 4 and FIG. 13 are built vertically at regular intervals and a plurality of stirring blades 12 capable of stirring while rotating between the panel-type steam chamber 13 and the chamber 13 to the length of the evaporation and evaporation dryer 10. Penetrating the middle along It is attached to the shaft (S) equipped with a rocker performs a stirring function while rotating forward and reverse, the chamber 13 is in communication with the steam chamber 14 formed in the agitated evaporation and evaporation condenser dryer (10) The upper one side of the evaporation condenser 10 is connected to the overflow preventing chamber 17 by a connecting tube 16, and a lower U-shaped trap 18 is provided below the chamber 17 to evaporate and evaporate the stirred type. It is connected to the inside of the concentrated dryer (10). The panel-type steam chamber 13 is formed of a subsoil in order to operate the stirring blade 12 smoothly.

And connected to the steam compression turbine 20 having a preheated air supply control valve 21 on the pipeline (R ₁ ) connected to the overflow prevention chamber 17, the pipeline connected from the end of the steam compression turbine (20) (R ₂ ) is connected to the steam compression pump 30 and the pipeline (R ₃ ) therefrom is a heated steam in which the evaporation steam pipe (R ₉ ) is built, as shown in FIGS. 1 to 3. (熱蒸氣) connected to the heat exchange recovery device 60, the pipelines (R ₄ , R ₆ ) attached to both sides of the recovery device 60, the auxiliary boiler 40 having a thermal power therein And agitated evaporation and evaporative concentration dryers 10, respectively. In addition, the conduit (R ₄ ) is connected to the coil-type steam heating tube 42 in front of the burner of the burner 41, the thermal power is directed to the inside of the auxiliary boiler, passing through the steam heating chamber 43 of the central axis to the conduit (R ₅ ) It is connected to the heated steam heat exchange recovery device 60 for reuse of the extracted and heated steam heat, and a pipe line on the upper portion of the auxiliary boiler 40 to discharge the heated steam to the heat exchange recovery device 60 during initial operation. R ₁₀ ) is drawn out and connected to the conduit R ₃ .

Meanwhile, a conduit R ₇ having a pressure regulating regulator 51 and a drain valve 52 is drawn out below the steam chamber 14 of the stirred evaporation and evaporation concentration dryer 10 to store the evaporation object storage tank 1. The condensed water is collected in the condensed water storage tank 50 through the coiled tube R in the storage tank 1 and the waste heat is deprived.

Looking at the embodiment of the present invention with the device as described above, the evaporation object such as contaminated waste water is introduced into the evaporation object storage tank (1) having the condensate waste heat recovery function through the inlet (15a) to pass through the pipeline (R ₈ ) Evaporated in the stirred evaporation and evaporation condenser 10, the evaporated vapor is passed through the overflow prevention chamber 17, passing through the pipeline (R ₁ ) to the nature of the vaporized impurities contained in the water vapor Therefore, the preheating air supply control valve 21 for the purpose of supplying air for oxidation combustion is entered into the steam compression turbine 20 in a state in which an appropriate amount of preheating air is mixed (carbonization at high temperature without supplying preheating air depending on the properties of the evaporation object). Agitation type evaporation and evaporation concentration dryer (10) causes a vacuum state by the action of the steam compression turbine (20) and the steam compression pump (30) to raise the internal temperature of the evaporation concentration dryer to about 60 ℃, the degree of vacuum Even about 300-400mmHg When the pressure of the steam compression pump 30 is increased, the steam pressure is further increased, and then, through the pipe line R ₃ , the evaporation steam pipe line R ₉ of the heated steam heat exchange recovery device 60, and the pipe line R ₄ . To be discharged. The steam discharged through the conduit R ₄ passes through the steam heating tube 42 and the steam heating chamber 43 in the auxiliary boiler 40 and becomes steam at a high temperature of 600 ° C. to 800 ° C. by the steam heating means. in odor and BOD, COD impurities such as oxidation or combustion by the carbonized vapor state through a pipe (R _5), the pipeline (R ₃₎ a heat recovery steam heat exchanger to heat exchange with steam of 60 ℃ ~100 ℃ introduced through the The steam, which has been sent to the apparatus 60 and heated by the steam heating means, is evaporated in the evaporator 10 and passed to the diaphragm around the evaporation steam pipe line R ₉ through which steam of 60 ° C. to 100 ° C., which has not yet been carbonized, passes. The heat exchange is conducted in the heated steam heat exchange recovery device 60 shown in FIG. At this time, the diaphragm may be absent at regular intervals in the heat exchange recovery device 60 to extend the heat exchange time, thereby making efficient heat exchange.

However, in the initial operation, the water in the auxiliary boiler 40 is heated by a heating means so that the vaporized temperature passes through the pipe line R ₁₀ and the pipe line R ₃ and the evaporation steam pipe line R _{9 in} the heat exchange recovery device 60. ) Is heated by the high temperature heating means in the steam heating tube 42 and the steam heating chamber 43, and the impurities proceed in the heat exchange recovery apparatus 60 in the reverse direction again in the state of oxidizing combustion or carbonization. It is sent to the panel-type steam chamber 13 and the steam chamber 14 in the evaporator 10 can be heat-exchanged with the evaporation object to make a vapor of 60 ℃ to 100 ℃. The heat exchange with steam of 60 ℃ ~100 ℃ becomes action is set to the 450 ℃ ~600 ℃ temperature steam discharged by the pipeline (R _4), a pipe (R ₆₎ roneun temperature by heat exchange in the heat recovery device (60) The lowered steam is discharged toward the evaporator 10 (see FIG. 3 of the drawing). The preheated steam of 450 ° C to 600 ° C discharged to the pipe line R ₄ is as described above. While heating to a high temperature by the heating means in the auxiliary boiler 40, it enters into the coil-type steam heating tube 42 and the steam heating chamber 43, and burns or carbonizes at a high temperature of 600 ° C to 800 ° C. through the pipeline (R ₅₎ in the state, is evaporated from the evaporator 10, steam pipe (R ₉₎ proceeds to the opposite direction of the steam 60 ℃ ~100 ℃ flowing in, and in the heating steam heat recovery device (60) Heat exchange takes place. At this time, the heating energy inputted by the heating means to obtain high temperature steam of 600 ° C to 800 ° C is heat exchanged in the heat exchange recovery device 60 (see FIG. 3). The steam is preheated with hot steam at 450 ° C. to 600 ° C. and reused to recover steam, thereby generating the effect of saving heating energy of the heating means. In addition, 150 ° C. to 200 ° C. of impurities discharged into the conduit R ₆ are burned or carbonized, and the vapor is sent to the panel-type steam chamber 13 and the steam chamber 14 of the evaporation concentrator 10, and the The heat of vaporization and the evaporation heat is removed in the process of liquefaction, the liquefied high temperature condensate (about 80 ℃ ~ 120 ℃) is evaporated through the pipeline (R ₇ ) through the pressure regulating regulator 51 and the drain valve 52 Waste heat is recovered from the coiled tube (R) in the object storage tank (1) and collected in the condensate storage tank (50). At this time, the condensed water in the condensate storage tank 50 may be filtered to remove carbonized water vapor impurities to obtain high quality distilled water.

Although the present invention as described above has been applied under reduced pressure, it may be applied in a pressurized state by evaporating to a high pressure above atmospheric pressure as necessary.

Looking at the effects of the present invention made of the configuration and method as described above are as follows.

The evaporation object in the evaporation storage tank 1 recovers waste heat from the liquefied high-temperature condensate in the coiled tube (R) and naturally flows through the decompression action of the steam compression turbine (20) and the steam compression pump (30). ₈ ) is drawn into the stirring evaporation and evaporation dryer 10, the treatment object is mixed in an even distribution by the stirring blades 12 in the stirring evaporation and evaporation concentration dryer 10 and the final sludge ( 11) is discharged out of the evaporation concentration dryer 10 by the extrusion screw (11s), the evaporation object in the evaporation and evaporation concentration dryer 10 is 150 in the panel-type steam chamber 13 and the steam chamber 14 The overflow prevention chamber 17 and the pipe line in which the U-shaped trap 18 is drawn out at the lower part to recover the heat of vaporization from the high temperature steam at which the temperature is between 200 ° C. and 200 ° C., and to prevent the liquid from overflowing into the vaporizer. (R ₁₎ a binary vapor compression turbine 20 through the In this case, the evaporation gas entering the steam compression turbine 20 is mixed with a predetermined amount of preheating air by a preheating air supply control valve 21 positioned immediately before the entrance of the steam compression turbine 20 when necessary. .

The evaporated gas thus entered is compressed by the steam compression pump 30 through the steam compression turbine 20 to increase the vapor pressure. At this time, the evaporation object introduced into the stirring type evaporation and evaporation concentration dryer 10 is a vapor compression turbine 20. And evaporation while maintaining the evaporation temperature of about 60 ℃ due to the reduced pressure environment in the agitation type evaporation and evaporation dryer 10 reaching a vacuum degree of about 300mmHg-400mmHg by the action of the steam compression pump 30). As can be seen from the following Equation (E-1) regarding the law of an ideal gas that holds for a gas mixture, the vapor compression turbine 20 and the vapor compression pump are used to generate high temperature liquefaction under the high vapor pressure. By 30, the vapor pressure can be increased. Instead of the steam compression turbine 20 used as the steam compression means, a vacuum booster, a vacuum molecular pump and other suitable steam compression means may be used.

PV = nt RT… … (E-1)

Where P is the gas component pressure, V is the volume, T is the absolute temperature of the gas component, R is the gas constant, and nt is the sum of the moles of gas in the volume V.

Therefore, these evaporation gas is passed through the evaporation steam pipe line (R ₉ ) in the heated steam heat exchange recovery device 60 in a state in which the vapor pressure is further increased by the steam compression turbine 20 and the steam compression pump 30, Injected into the heating chamber 43 and heated to a high temperature of 600 ℃ ~ 800 ℃ by the heating means and sent to the heated steam heat exchange recovery device 60 in a combustion or carbonized state, the steam of 60 ℃ ~ 100 ℃ flow inside Due to the diaphragm for extending the heat exchange time around the evaporation steam pipe (R9), heat exchange takes place in a zigzag fashion in the opposite direction to each other (see FIG. 2). As a result, at a temperature of 450 ° C to 600 ° C. The preheated evaporator gas is sent to the steam heating tube 42 and the steam heating chamber 43 attached to the steam heating means to maintain a high temperature of 600 ° C. to 800 ° C. through the conduit R ₄ . Take away 150 ℃ -20 The evaporation gas having a temperature lowered to 0 ° C. flows through the conduit R6 and flows into the panel-type steam chamber 13 and the steam chamber 14 in the stirring-type evaporation and evaporation dryer 10, where the evaporation object and It heat-exchanges and liquefies to the temperature of about 80 degreeC-120 degreeC. This is due to the liquefaction of the steam at a temperature proportional to the vapor pressure, as can be seen by the above formula (E-1), because the vapor of the high vapor pressure is liquefied at a high temperature proportional to the vapor pressure.

The water liquefied at a high temperature is sent to the coiled tube (R) through the pipe line (R ₇ ) through the pressure regulating regulator (51) and the drain valve (52) and the evaporation object in the evaporation object storage tank (1) and 2 After the heat exchange to take the waste heat is collected in the condensate storage tank (50). On the other hand, 60 ° C to 100 ° C evaporated water vapor that is recovered by evaporation and evaporation heat from the evaporation and condensation dryer 10 is sent to the heated steam heat exchange recovery device 60 through the overflow prevention chamber 17.

In addition, the odor of water vapor mixed with water vapor by evaporation with evaporation gas, or B.O.D., C.O.D. Impurities such as steam heating means are mixed with a predetermined amount of preheated air supplied by opening and closing control of the preheated air supply control valve 21 installed immediately before the entrance of the steam compression turbine 20 to facilitate oxidation. Depending on the impurity properties of the vaporized state contained in the vapor, removed or oxidized and burned by a high temperature environment of 600 ° C to 800 ° C while passing through the in-coil type steam heating tube 42 and the steam heating chamber 43 Carbonization only in the high temperature environment (600 ℃ ~ 800 ℃) of steam heating chamber 43 without mixing preheating air It is possible to remove impurities such as, and the heating energy introduced by the heating means to create a high temperature environment of 600 ℃ ~ 800 ℃ is recovered by the heated steam heat exchange recovery device 60 to reuse the heating energy as preheated You have the advantage of saving. In addition, although not shown in the drawings of the present invention, the heat treatment of the evaporation storage tank 1, the evaporation and evaporation concentration dryer 10, the auxiliary boiler 40, etc. can further increase the energy efficiency.

The results of the examples using the apparatus and method of the present invention are shown in Table 1 below, which is the result obtained by high-temperature heating and oxidizing combustion or carbonization at 620 ° C. using manure as an evaporation object. As can be seen from the following results, the evaporation object using the present invention can be remarkably purified.

As described above, the present invention can produce high-quality distilled water at a low price, because it can secure economic advantages and high performance, which can be supplied at a significantly lower price than a conventional device and equipment operation cost. Of course, there are features that can be widely used for the evaporative drying of toxic wastewater or environmental pollution wastewater, the evaporation of various waste sludges, the concentrated drying and the end treatment. In addition, B.O.D., C.O.D. Many fuel costs required by heating means for heating to a high temperature for the removal of impurities such as odors and the like can be reused as steam preheating energy by the heating steam heat exchange recovery device 60, thereby reducing the steam heating fuel cost. There is an advantage.

The evaporation and evaporation concentration drying apparatus and method having the above-described vapor purification ability can be mobilized by using various evaporators, heating means and heat exchange means under reduced pressure or pressure, if necessary. Applicable to appropriate design changes to belong to the gist of the present invention, it is believed that those skilled in the art can clearly understand.

Claims (3)

An evaporation storage tank (1) having an evaporation object inlet (15a) at the top for recovering condensate waste heat and having a coil-shaped tube (R) connected at one end thereof to the condensate storage tank (50); In order to recover the heat of vaporization by heat exchange, the upper part has an inlet 15b, the lower part is formed in a circular cross section, and the recess 11 is formed on one side to impart a waste discharge screw 11s, and the steam chamber 14 and A plurality of plate-shaped semicircular panel-type steam chambers 13 communicated vertically at regular intervals, and a plurality of stirring vanes capable of stirring while rotating between the panel-type steam chambers 13 and the chambers 13. (12) are attached to the shaft (S) is installed to penetrate the center along the length and performs the stirring function while rotating forward and reverse, the lower panel type steam chamber 13 is the pressure regulating regulator 51 and the drain valve (52) is connected to the coiled tube (R) by a pipe line (R ₇ ), the upper side is connected to the tube 16 is drawn out to prevent the overflow of the U-shaped trap 18 is drawn out at the bottom It is in communication with the chamber 17, the upper portion of the side An agitated evaporation and evaporation concentration dryer 10 in which a pipe line R ₈ is drawn out to suck an evaporation object from the lower part of the object storage tank 1; In order to recover the heat of steam heated by the heating means in the sub-boiler 40, a plurality of evaporative steam pipe (R ₉ ) is horizontally installed and a plurality of diaphragms are vertically laid at regular intervals to improve heat exchange capacity. At one end, a pipe (R ₃ ) is drawn out to connect with the evaporative concentration dryer (10), and at the other end, a coil type steam heating tube (42) in the auxiliary boiler (40) having a burner (41) attached to one side. And a pipe line R ₄ is drawn out to connect with the steam heating chamber 43, and a lower part of the pipe line R ₄ is connected to the panel-type steam chamber 13 and the steam chamber 14 in the evaporative concentration dryer 10. (R ₆ ) is drawn out and heat steam heat exchange recovery with the pipe (R ₅ ) drawn out to connect to the coil-type steam heating tube 42 and the steam heating chamber 43 in the auxiliary boiler 40 on the other lower side At the time of initial operation with apparatus 60 In order to discharge the heated steam to the heat exchange recovery device 60, a pipe line R ₁₀ is drawn out and connected to the pipe line R ₃ , and a burner 41 is attached to the side, and the coil-type steam is connected to the heat tube 42. The steam heating chamber 43 is internally installed, and the pipeline R ₄ through which the steam preheated by the heated steam heat exchange recovery device 60 is drawn out, and the steam is heated or heated by a heating means to burn or carbonize it. An auxiliary boiler 40 in which a conduit R ₅ is drawn out to be discharged to the furnace; And between the pipe line R ₃ drawn from the heated steam heat exchange recovery device 60 and the connection pipe 16 drawn from the top of the evaporation concentration dryer 10 to connect with the evaporation concentration dryer 10. Chamber 17, conduit (R ₁ ), preheating air supply control valve 21, steam compression turbine 20 and the conduit (R ₂ ) for increasing the vapor pressure by compressing the vapor evaporated in the evaporative condensation dryer (10) Evaporation and evaporation and drying apparatus having a steam purification capability, characterized in that the absence of a steam compression pump (30) connected by. The panel type according to claim 1, wherein the stirring blades 12 placed on the shaft S passing through the center along the length in the evaporation dryer 10 are formed in the upper and lower straits to smoothly operate. Evaporation and evaporation concentrated drying apparatus having a steam purification capability, characterized in that consisting of a steam chamber (13). Evaporation steam pipe (R ₉ ) in the heat exchange recovery device (60) through the pipe (R ₁₀ ) and pipe (R ₃ ) produced steam by heating the water in the auxiliary boiler 40 by the heating means at the initial operation. Oxidative combustion or carbonization in the steam heating tube 42 and the steam heating chamber 43 by means of a high temperature heating means is carried out again in the heat exchange recovery apparatus 60 to reverse the panel in the evaporative concentration dryer 10. The evaporation object storage tank is introduced into the type steam chamber 13 and the steam chamber 14 by heat exchange with the evaporation object, and is provided through a pipe line R ₇ having no pressure regulating regulator 51 and a drain valve 52. Sending to the coil-shaped tube (R) built in (1) to recover the waste heat; By evaporating or depressurizing the inside of the stirring type evaporation and evaporation concentration dryer 10 by the vapor compression turbine 20 and the vapor compression pump 30, the evaporation object is stored in the evaporation object storage tank 1 through a conduit R ₈ . Aspirated, heat exchanged with the carbonized steam of 150 ° C. to 200 ° C. introduced into the panel-type steam chamber 13 and the steam chamber 14 through the conduit R ₆ , and the connection pipe 16 to the steam of 60 ° C. to 100 ° C. The discharged through the), the object to be treated is uniformly mixed by the forward and reverse rotation of the stirring blade 12 in the evaporation concentration dryer 10 and the final sludge is the evaporation concentration dryer (10s) by the extrusion screw (11s). Moving the sludge to the depression 11 to discharge it outward; The overflowed liquid, such as a liquid contained in the vapor at 60 ° C. to 100 ° C. discharged to the connection pipe 16 drawn out on the evaporation condenser 10, is U-shaped at the bottom through the overflow prevention chamber 17. The steam of 60 ° C. to 100 ° C. flowing into the evaporation dryer 10 again through the trap 18 and flowing through the pipe line R1 connected to the connecting pipe 16 is preheated air air control valve 21. ) Is mixed with preheated air (may not mix preheated air depending on the nature of the evaporation object), steam compression turbine 20, pipeline (R ₂ ), steam compression pump (30) and pipeline (R ₃ ) Flowing through the plurality of evaporation steam pipes (R9) in the heated steam heat exchange recovery device (60) through; The steam of 60 ° C. to 100 ° C. introduced into the evaporation steam pipe line R _{9 is} provided by the burner 41, the coil type steam heating tube 42, and the steam heating chamber 43 which are installed in the auxiliary boiler 40. High temperature heating is introduced into the heat exchange recovery device 60 through the pipe line (R ₅ ), 600 ℃ ~ 800 ℃ high temperature steam flowing in a zigzag flow guided by a plurality of diaphragms arranged vertically at regular intervals And the heat exchange is performed in a reverse direction to each other, the steam of 600 ℃ ~ 800 ℃ is lowered to 150 ~ 200 ℃ discharged through the pipe line (R ₅ ) to evaporate and evaporation concentrated dryer 10 in the panel-type steam chamber (13) And a coil type steam heating tube 42 which is introduced into the steam chamber 14 and the steam having a temperature of 60 ° C. to 100 ° C. is preheated to 450 ° C. to 600 ° C. and installed in the auxiliary boiler 40 through a conduit R ₄ . And flowing into the steam heating chamber 43; And the steam preheated to 450 ℃ ~ 600 ℃ by the heat exchange recovery device 60 is the coil-type steam heating tube 42 and the steam heating chamber 43 which is installed in the auxiliary boiler 40 through the conduit (R ₄ ). Heat steam heat exchange recovery unit through the pipe line (R ₅ ) to a high temperature steam of 600 ℃ ~ 800 ℃ is reheated by the burner 41 and the odor and impurities such as BOD, COD are removed by oxidative combustion or carbonization 60) flows in the reverse direction with the steam of 60 ℃ ~ 100 ℃ in the evaporation steam pipe (R ₉ ) and heat exchanged and descended to 150 ℃ ~ 200 ℃ discharged through the pipe (R ₆ ) evaporation condensation dryer (10) The latent heat (539 kcal / l) is taken into the evaporation energy in the process of liquefying heat by entering into the panel-type steam chamber 13 and the steam chamber 14 in the panel-type heat exchanger 10 again. The water liquefied at 120 ° C regulates the pressure regulating regulator (51) and the drain valve (52). Evaporation with the steam purification capability, characterized in that the second heat exchange with the evaporation object while passing through the coiled tube (R) in the evaporation object storage tank (1) and storing the waste heat in the condensate storage tank (50) And evaporative concentration drying method.