KR101653105B1 - Heat recovery apparatus - Google Patents

Abstract

The present application relates to a heat recovery apparatus and method. According to the heat recovery apparatus and method of the present application, a low-temperature heat source of less than 100 ° C discharged from an industrial site or various chemical processes, for example, The generated steam can be used for various processes. Therefore, it is possible to reduce the amount of high temperature steam used as an external heat source for use in the reactor or the distillation column, thereby maximizing the energy saving efficiency Alternatively, the power consumed in the compressor can be produced by itself, and the vaporization phenomenon of the refrigerant flow through the compressor can be reduced, so that the heat can be recovered with excellent efficiency.

Description

HEAT RECOVERY APPARATUS

The present application relates to a heat recovery apparatus and method.

In a typical chemical process, heat exchange takes place at various routes through the reactor or distillation column, and the waste heat generated after such heat exchange can be reused or discarded. For example, as shown in FIG. 1, when the waste heat is a low-temperature heat source of a sensible state at a level of less than 100 ° C, for example, 50 to 90 ° C, the temperature is too low to be substantially reusable, It is being discarded after being condensed.

On the other hand, low-pressure or high-pressure steam is used in various fields in industry, and in particular, high-temperature and high-pressure steam are mainly used in chemical processes. The high-temperature and high-pressure steam generally produces high-temperature and high-pressure steam by heating water at normal pressure and normal temperature to a vaporization point and applying high pressure to water that has turned into steam to increase internal energy. In this case, In order to vaporize the water of the state, it requires a large amount of energy consumption.

The present application provides a heat recovery apparatus and method.

The present application relates to a heat recovery apparatus. According to the heat recovery apparatus of the present application, it is possible to generate steam using a low-temperature heat source of less than 100 ° C discharged from an industrial site or various chemical processes, for example, a production process of petrochemical products, It is possible to reduce the amount of high temperature steam used as an external heat source for use in the reactor or the distillation column, thereby maximizing the energy saving efficiency. Further, the heat recovery apparatus of the present application can produce power consumed in the compressor itself, and can partially reduce the vaporization phenomenon of the refrigerant flow passing through the compressor, so that heat can be recovered with excellent efficiency.

DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS Reference will now be made in detail to various embodiments of the present application, examples of which are illustrated in the accompanying drawings, which are not intended to limit the scope of the heat recovery apparatus according to the present application.

2 is a diagram schematically showing an exemplary heat recovery apparatus 10 of the present application.

2, the heat recovery apparatus 10 of the present application includes a first heat exchanger 101, a compressor 102, a second heat exchanger 103, and a turbine 104. The first heat exchanger 101, the compressor 102, the second heat exchanger 103 and the turbine 104 may be connected to each other through a pipe. For example, the refrigerant or the fluid may flow through the pipe, And may be fluidically connected. In one example, the pipe through which the refrigerant flows may be a circulation loop or circulation system connected to circulate the first heat exchanger 101, the compressor 102, the second heat exchanger 103 and the turbine 104 in sequence have.

The flow rate of the refrigerant flow circulated through the pipe may be from 5,000 kg / hr to 50,000 kg / hr, for example, from 10,000 kg / hr to 40,000 kg / hr or from 30,000 kg / hr to 45,000 kg / May be, but is not limited to, 25,000 to 35,000 kg / hr.

The first heat exchanger (101) is included in the heat recovery apparatus (10) of the present application in order to exchange heat between the refrigerant flow and the fluid flowing from the outside, and through the heat exchange, the refrigerant is vaporized, The refrigerant can be flowed out from the first heat exchanger 101 in a flow of a relatively higher temperature than the flow of the refrigerant flowing into the heat exchanger. The term " gas phase " means a state in which the gas component flow is rich among all the components of the refrigerant flow, for example, a state in which the mole fraction of the gas component stream in the entire refrigerant flow component is 0.9 to 1.0.

The first fluid stream W ₁ flowing into the first heat exchanger 101 may be, for example, a waste heat stream or a stream of condensate that has passed through a condenser, and the waste heat stream may, for example, Of cooling water, but is not limited thereto. Particularly in the present application, a waste heat stream of a low-temperature heat source in a sensible state at a temperature of less than 100 ° C, for example, 50 to 90 ° C, can be preferably used.

For example, a first fluid flow W ₁ such as a refrigerant flow F _4-2 and a waste heat flow may be introduced into the first heat exchanger 101 through a fluid-connected pipe, The first fluid flow F _4-2 and the first fluid flow W ₁ may be respectively flowed out in the first heat exchanger 101 through the fluid connected piping after mutual heat exchange in the first heat exchanger 101 .

In one example, the temperature of the refrigerant flow F ₁ flowing out of the first heat exchanger 101 and the temperature of the first fluid flow W ₁ flowing into the first heat exchanger 101 satisfy the following formula 1 can be satisfied.

[Formula 1]

1 ° C ≤ T _F - T _R ≤ 20 ° C

_Wherein T _F represents the temperature of the first fluid flow W ₁ flowing into the first heat exchanger 101 and T _R represents the temperature of the refrigerant flow F discharged from the first heat exchanger 101 ₁ ) < / RTI >

That is, the difference between the temperature of the first fluid flow (W ₁₎ flowing in the temperature of the first heat exchanger 101 of the refrigerant flow (F ₁₎ flowing in the first heat exchanger 101 T _F - T _R Can be adjusted to a range of 1 to 20 占 폚, for example, 1 to 15 占 폚, 2 to 20 占 폚, 1 to 12 占 폚, 2 to 12 占 폚, or 5 to 12 占 폚.

When the temperature of the refrigerant flow F ₁ flowing out of the first heat exchanger 101 and the temperature of the first fluid flow W ₁ flowing into the first heat exchanger 101 satisfy the formula 1, By using waste heat of low-temperature waste heat, in particular, a low-temperature heat source of a sensible heat of less than 100 ° C, for example, at a level of 50 to 90 ° C, high-temperature steam can be produced.

If the temperature of the refrigerant flow F ₁ flowing out of the first heat exchanger 101 and the temperature of the first fluid flow W ₁ flowing into the first heat exchanger 101 satisfy the general formula 1, And it can be variously adjusted according to the type of the process to be applied and the conditions of each process. In one example, the temperature of the first fluid stream W ₁ entering the first heat exchanger 101 is in the range of 60 ° C to 100 ° C, for example 70 ° C to 90 ° C, 80 ° C to 95 ° C, 80 ° C Lt; 0 > C to 85 < 0 > C or 83 [deg.] C to 87 [deg.] C, but is not particularly limited thereto. The temperature of the refrigerant flow F ₁ flowing out from the first heat exchanger 101 may be 60 ° C. to 100 ° C., for example, 60 ° C. to 95 ° C., 65 ° C. to 90 ° C., , Or 70 [deg.] C to 85 [deg.] C, but is not particularly limited thereto.

In this case, the temperature of the first fluid flow W ₂ flowing out after the heat exchange with the refrigerant flow in the first heat exchanger 101 is 60 ° C. to 100 ° C., for example, 60 ° C. to 95 ° C. and 65 ° C. Deg.] C to 90 [deg.] C, 65 [deg.] C to 95 [deg.] C, or 70 [deg.] C to 85 [deg.] C.

The temperature of the refrigerant flow F _4-2 flowing into the first heat exchanger 101 is lower than the temperature of the fluid flow W ₁ flowing into the first heat exchanger 101, For example, it may be 60 ° C to 90 ° C, 70 ° C to 80 ° C, 75 ° C to 85 ° C, or 73 ° C to 77 ° C, but is not limited thereto.

The pressure of the refrigerant flows (F _4-2 , F ₁ ) flowing into and flowing out of the first heat exchanger (101) may vary depending on the type of refrigerant and operating conditions, and is not particularly limited. For example, the pressure of the refrigerant flows (F _4-2 , F ₁ ) flowing into and flowing out of the first heat exchanger (101) is 3.0 kgf / cm ² g to 20.0 kgf / cm ² g, But is not limited to, from 4.0 kgf / cm ² g to 10.0 kgf / cm ² g, or from 5.0 kgf / cm ² g to 7.0 kgf / cm ² g. By adjusting the pressure of the refrigerant flow to 3.0 kgf / cm ² g to 20.0 kgf / cm ² g, the compression ratio of the compressor can be easily controlled. Generally, the outlet pressure of the compressor is determined according to the temperature, but if the inlet pressure is increased, the compression ratio can be kept low. The higher the compression ratio is, the higher the steam temperature can be generated from the low-temperature heat source. In this case, however, the coefficient of performance decreases. As the compression ratio decreases, the coefficient of performance increases. However, Difficult problems arise. In the above, the pressure unit kgf / cm ² g means gauge pressure.

The pressure of the first fluid flows (W ₁ , W ₂ ) flowing into and flowing out of the first heat exchanger 101 is not particularly limited, and may be, for example, 0.5 kgf / cm ² g to 2.0 kgf / cm ² g, for example, 0.7 kgf / cm ² g to 1.5 kgf / cm ² g, or 0.8 kgf / cm ² g to 1.2 kgf / cm ² g.

The flow rate of the first fluid flow W ₁ flowing into the first heat exchanger 101 may be 50,000 kg / hr or more, for example, 100,000 kg / hr or more, or 200,000 kg / hr or more, , It may be at least 250,000 kg / hr, but is not limited thereto. As the flow rate of the first fluid flow W ₁ flowing into the first heat exchanger 101 increases, the outflow temperature of the first fluid flow W ₂ flowing out after heat transfer even when the same amount of heat is transferred to the refrigerant is maintained So that the outflow temperature of the refrigerant flow F ₁ flowing out of the first heat exchanger can be maintained at a high level. Therefore, the upper limit of the flow rate of the first fluid flow W ₁ flowing into the first heat exchanger 101 is not particularly limited, but may be 500,000 kg / hr, for example, Or less, or 350,000 kg / hr or less, but is not limited thereto.

The first heat exchanger 101 may be a device or a machine for performing heat exchange between a flowing fluid and a refrigerant. In one embodiment, the first heat exchanger 101 may be configured to convert a liquid refrigerant flow into a gas refrigerant flow And may be an evaporator that evaporates.

The compressor 102 is included in the heat recovery apparatus 10 of the present application in order to compress the refrigerant flow F ₁ flowing out of the first heat exchanger 101 and raise the temperature and pressure, The refrigerant flow F _{2 in} the gaseous phase having a relatively high temperature and a high pressure relative to the refrigerant flow F ₁ flowing out of the first heat exchanger is compressed through the second heat exchanger 103 Can be introduced

For example, the refrigerant flow F ₁ flowing out of the first heat exchanger 101 may be introduced into the compressor 102 through a fluid-connected pipe, and the introduced refrigerant flow F ₁ may flow into the compressor 102 and then through the fluidly connected piping.

In one example, the ratio of the pressure of the refrigerant flow F ₁ flowing out of the first heat exchanger 101 to the pressure of the refrigerant flow F ₂ flowing out of the compressor 102 satisfies the following formula 2 have.

[Formula 2]

2? P _C / P _H ? 5

Where P _C represents the pressure (bar) of the refrigerant flow F ₂ flowing out of the compressor 102 and P _H represents the pressure of the refrigerant flow F ₁ flowing out from the first heat exchanger 101, (Bar).

That is, the ratio P _C / P _H of the pressure of the refrigerant flow F ₁ flowing out of the first heat exchanger 101 and the pressure of the refrigerant flow F ₂ flowing out of the compressor 102 is 2 to 5, For example, in the range of from 2 to 4, preferably from 3 to 4. The ratio of the pressure P _C / P _H is determined by the pressure of the refrigerant flow F ₂ flowing out of the compressor 102 and the pressure of the refrigerant flow F ₁ flowing out from the first heat exchanger 101 to bar , And it is obvious in the art that the ratio of the pressure may not satisfy the general formula 2 when the specific pressure value converted according to the unit of pressure to be measured is changed. Therefore, the formula (2) may include all cases in which the measured pressure value is converted into the pressure unit of bar to be satisfied.

The ratio of the pressure of the refrigerant flow F ₁ flowing out of the first heat exchanger 101 to the pressure of the refrigerant flow F ₂ flowing out of the compressor 102 satisfies the formula 2, The refrigerant vaporized in the second heat exchanger 101 may be compressed to a high temperature and a high pressure state so as to have a sufficient amount of heat to be heat-exchanged with the second fluid flow passing through the second heat exchanger described later.

The pressure of the refrigerant flow F ₁ flowing out of the first heat exchanger 101 and the pressure of the refrigerant flow F ₂ flowing out of the compressor 102 are not particularly limited as long as they satisfy the expression 2, It can be variously adjusted according to the kind of process to be applied and the condition of each process. In one example, in the first heat exchanger 101, the pressure of the refrigerant flow F ₁ flowing out is 3.0 kgf / cm ² g to 20.0 kgf / cm ² g, for example 4.0 kgf / cm ² g To 10.0 kgf / cm ² g, or from 5.0 kgf / cm ² g to 7.0 kgf / cm ² g, but is not limited thereto. The pressure of the refrigerant flow F ₂ flowing out of the compressor 102 is 15.0 to 30.0 kgf / cm ² g, for example, 15.0 to 25.0 kgf / cm ² g, 18.0 to 25.0 kgf / cm ² g, Or 20.0 to 23.0 kgf / cm ² g, but is not limited thereto.

The temperature of the refrigerant flow (F ₂ ) flowing out after being compressed by the compressor 102 may be in the range of 110 ° C to 180 ° C, for example, 120 ° C to 170 ° C, 120 ° C to 130 ° C, , Or from 123 < 0 > C to 128 < 0 > C.

As the compressor 102, various compression devices known in the art can be used without limitation as long as the compressor is capable of compressing the gas phase flow. In one example, the compressor may be a compressor, no.

The second heat exchanger 103 is connected to the heat recovery apparatus 10 of the present application 10 to heat the refrigerant flow F ₂ flowing out of the compressor 102 and the second fluid flow W ₃ flowing from the outside, Through the heat exchange, the refrigerant can be discharged as a relatively low-temperature liquid flow as compared with the refrigerant flow F ₂ flowing out from the compressor after being condensed, and the second fluid flow W ₃ The refrigerant can absorb the latent heat generated during the condensation. The term "liquid phase" as used herein means a state in which the liquid component flow is rich in the entire refrigerant flow component, for example, a state in which the mole fraction of the liquid component flow in the entire refrigerant flow component is 0.9 to 1.0.

In one example, the second fluid entering the second heat exchanger 103 may be make-up water, in which case the heat-exchanged water in the second heat exchanger 103 is cooled It absorbs latent heat generated during condensation and is vaporized and can be discharged in the form of steam.

For example, the second heat exchanger 103 may include a refrigerant flow F ₂ flowing out of the compressor 102 through a fluid-connected pipe and a second fluid flow W ₃ for exchanging heat with the refrigerant flow F ₂ . And the second refrigerant flow F ₂ and the second refrigerant flow W ₃ are exchanged in the second heat exchanger 103 and are then subjected to the second heat exchange (103), respectively.

The temperature and the pressure of the second fluid flow W ₃ flowing into the second heat exchanger 103 are not particularly limited and the second fluid flow of various temperatures and pressures may be introduced into the second heat exchanger 103 . For example, 110 ℃ to 120 ℃, for example, 112 ℃ to 116 ℃, or temperature, and 0.5 to 0.9 kgf / cm ² g in 115 ℃ to 118 ℃, for example, 0.6 to 0.8 kgf / cm ² g The second fluid flow W ₃ can be introduced into the second heat exchanger 103 by the pressure of the second heat exchanger 103.

The flow rate of the second fluid flow W ₃ flowing into the second heat exchanger 103 is not particularly limited and may be 300 kg / hr to 6,000 kg / hr, for example, 500 kg / 1,000 kg / hr, 1,000 kg / hr to 2,000 kg / hr, or 1,200 kg / hr to 1,400 kg / hr.

In one example, the refrigerant (F ₂ ) at high temperature and high pressure discharged from the compressor 102 and the water (W ₄ ) heat-exchanged at the second heat exchanger 103 are heated at a temperature of 115 ° C to 125 ° C, for example, 115 And the second heat exchange with steam having a pressure of from 0.5 to 0.9 kgf / cm ² g, for example, from 0.6 to 0.8 kgf / cm ² g, at a temperature of 120 to 120 ° C, And may be discharged from the vessel 103.

The refrigerant flow F _{3 in} the second heat exchanger 103 that has been heat-exchanged with the second fluid flow W ₃ is heated to a temperature of 115 ° C to 130 ° C, for example, 115 ° C to 128 ° C or 120 ° C to 128 ° C The second heat exchanger 103 at a temperature of 120 to 126 ° C, 118 to 126 ° C, 120 to 126 ° C, or 118 to 122 ° C, but is not limited thereto. The pressure of the refrigerant flow F _{3 that} is heat-exchanged with the second fluid flow W ₃ in the second heat exchanger 103 may vary in various ways depending on the type of refrigerant and the operating conditions, to 30.0 kgf / cm ² g, 15.0 to 25.0 kgf / cm ² g, 18.0 to 25.0 kgf / cm ² g, or at a pressure of 19.0 to 23.0 kgf / cm ² g to be released in the second heat exchanger (103) But is not limited thereto.

The second heat exchanger 103 refers to an apparatus or a machine that performs heat exchange between flowing fluids. In one embodiment, the second heat exchanger 103 condenses the gaseous refrigerant stream into a liquid phase refrigerant stream It may be a condenser.

The exemplary heat recovery apparatus 10 of the present application may further include a storage tank 105. As shown in FIG. 2, the storage tank 105 may be connected to the second heat exchanger 103 through a pipe. The storage tank 105 is a device for supplying a second fluid flow to the second heat exchanger 103. The storage tank 105 is provided with a second fluid flowing into the second heat exchanger 103, For example, water may be stored.

The second fluid flow W ₃ flowing out from the storage tank 105 flows into the second heat exchanger 103 along the pipe and flows through the refrigerant flow F ₂ flowing into the second heat exchanger 103 Heat exchange can be performed. In this case, the heat-exchanged second fluid stream W ₄ , for example, high-temperature and high-pressure water, may be re-introduced into the storage tank 105, and then may be decompressed and discharged in a steam form.

The turbine 104 is included in the heat recovery apparatus 10 of the present application in order to expand the liquid refrigerant flow F ₃ flowing out of the second heat exchanger 103 and lower the temperature and pressure, After flowing through the turbine 104, the refrigerant flow F _4-1 is expanded to a relatively low temperature and a low pressure state relative to the refrigerant flow flowing out of the second heat exchanger, to the first heat exchanger 101 Can be reintroduced.

For example, the second refrigerant flow (F ₃₎ of the liquid flowing out of the heat exchanger 103 may be introduced into the turbine 104 via a fluid associated piping, the inlet, the refrigerant flow (F ₃₎ is the After being expanded in the turbine 104, may flow out through the fluidly connected piping in a relatively low temperature and low pressure state relative to the refrigerant flow exiting the second heat exchanger. In one example, the refrigerant flow (F _4-1 ) flowing out of the turbine 104 is in the range of 60 ° C to 90 ° C, for example 70 ° C to 80 ° C or 75 ° C to 85 ° C, But can be, but is not limited to, the turbine 104 at a temperature of 77 ° C. The pressure of the refrigerant flow F _4-1 flowing out from the turbine 104 may vary depending on the type of refrigerant and the operating conditions. For example, the pressure of the refrigerant flow F _4-1 may range from 5.0 kgf / cm ² g to 10 kgf / cm ² g, for example from 5.5 kgf / cm ² g to 8.0 kgf / cm ² g or from 5.8 kgf / cm ² g to 7.0 kgf / cm ² g, preferably from 5.8 kgf / cm ² g to 6.5 kgf / cm < ² > g of the turbine 104, but is not limited thereto.

The turbine 104 may be a power generation device, and may be, for example, a hydraulic turbine capable of converting the mechanical energy of the refrigerant flowing through the pipe, that is, the fluid, into electric energy. , The power consumed by the compressor can be produced by the heat recovery apparatus 10 itself, so that the coefficient of performance of the recovery apparatus 10 can be increased. Further, for example, in the case where the flow exiting from the second heat exchanger is reintroduced into the first heat exchanger, when the pressure drop device such as a control valve is used to lower the pressure, the enthalpy before and after the control valve is the same, There may be a problem that a part of the refrigerant flow passing through the valve is vaporized. However, when the turbine is used, since the enthalpy difference exists, it is possible to alleviate the problem of vaporization of a part of the refrigerant flow.

In the heat recovery apparatus 10 of the present application, the refrigerant flows passing through the first heat exchanger 101, the compressor 102, the second heat exchanger 103, and the turbine 104 through the pipe are respectively at different temperatures And pressure characteristics and flows into or out of the first heat exchanger 101, the compressor 102, the second heat exchanger 103 and the turbine 104 in a gas-phase and / or liquid-phase flow, The latent heat due to temperature, pressure and state changes can be used as a heat source for steam generation. In addition, in the heat recovery apparatus 10 of the present application, steam can be produced with excellent efficiency by setting optimum temperature and pressure conditions for generating steam using low temperature waste heat of less than 100 캜.

In one example, the refrigerant flow F _4-2 flowing into the first heat exchanger 101 may be a liquid phase stream, and the volume fraction of the liquid phase stream in the refrigerant stream may range from 0.4 to 1.0, 0.9 to 1.0, preferably 0.99 to 1.0.

Also, the refrigerant flow F ₂ flowing out of the compressor 102 may be a gaseous stream, and the volume fraction of the gaseous stream in the refrigerant stream may be from 0.7 to 0.9, for example from 0.75 to 0.85, preferably from 0.8 To 0.85.

The refrigerant flow F ₃ flowing out of the second heat exchanger 103 may be a liquid phase stream and the volume fraction of the liquid phase stream in the refrigerant stream may range from 0.8 to 1.0, for example, from 0.9 to 1.0, 0.99 to 1.0.

In addition, the refrigerant flow out of the turbine 104 may be a liquid phase flow, and the fraction of the gaseous phase flow in the refrigerant flow may be from 0 to 0.5, for example from 0 to 0.3, preferably from 0 to 0.1 .

The volume fraction refers to the ratio of the volume flow rate of the liquid flow or gas phase flow to the volume flow rate of the entire refrigerant flow flowing through the pipe, And can be obtained by the following general formula (4).

[Formula 4]

Volumetric flow rate = Av (m ³ / s)

In the general formula (4), A represents the cross-sectional area (m ² ) of the pipe and v represents the flow rate (m / s) of the refrigerant flow.

Another embodiment of the heat recovery apparatus 10 of the present application includes a third heat exchanger 106. Fig. 3 is a diagram schematically showing a heat recovery apparatus 10 according to another embodiment of the present application.

As shown in FIG. 3, the heat recovery apparatus 10 of the present application includes a third heat exchanger (not shown) disposed between the first heat exchanger 101 and the compressor 102 and between the second heat exchanger 103 and the turbine 104 Gt; 106 < / RTI > For example, the third heat exchanger 106 is connected to a pipe connected between the first heat exchanger 101 and the compressor 102 and a pipe connected between the second heat exchanger 103 and the turbine 104 In one example, the third heat exchanger 106 is configured such that the refrigerant flow (F _1-1 ) flowing out of the first heat exchanger 101 passes through the third heat exchanger 106 The refrigerant flow F _3-1 flowing into the compressor 102 and flowing out of the second heat exchanger 103 flows through the third heat exchanger 106 and then flows into the turbine 104 Fluid may be connected. Since the heat recovery apparatus 10 of the present application includes the third heat exchanger 106, it is possible to prevent some vaporization phenomena of the refrigerant generated during the isentropic compression of the refrigerant, whereby the heat recovery apparatus 10 Can be increased. In the above, "isentropic compression" means compressing under the condition that the entropy of the system is kept constant. For example, it means an adiabatic compression process in which the heat is compressed without heat exchange with the periphery of the system.

4 is a graph showing an exemplary temperature-entropy diagram of the refrigerant of the present application. In one example, as shown in FIG. 4, the refrigerant circulating in the heat recovery apparatus 10 is a refrigerant having a slope of a tangent line of a saturated vapor curve of a temperature-entropy line is a refrigerant having a positive slope The slope of the tangent line of the saturated vapor curve of the temperature-entropy curve of the refrigerant in which the horizontal axis is entropy (J / kg · K) and the vertical axis is temperature (° C.) is 1 to 3 Lt; / RTI > In this temperature-entropy diagram, the saturated vapor curve refers to the curve portion on the right side of the line with respect to the critical point of the line. 4, when the refrigerant is equi-entropy-compressed (in the direction of the arrow in FIG. 4), the slope of the tangent line of the saturated vapor curve of the refrigerant has a positive slope There is a section in which a phase change occurs from a gas phase to a liquid phase, so that a part of the refrigerant flow in the compressor 102 may be vaporized. In order to prevent the partial vaporization of the refrigerant, the heat recovery apparatus 10 of the present application may include the third heat exchanger 106, thereby increasing the heat exchange efficiency of the heat recovery apparatus 10 .

As the refrigerant, various refrigerants known in the art may be used, provided that the slope of the tangent of the saturated vapor curve of the temperature-entropy curve has a positive value. However, the refrigerant is not particularly limited and includes, for example, R245fa, R1234ze and R1234yf may be used as the refrigerant.

3, in the heat recovery apparatus 10 according to the embodiment of the present application, the refrigerant flow (F _1-1 ) flowing out from the first heat exchanger 101 flows into the third heat exchanger 106 The refrigerant flow F _3-1 flowing into the compressor 102 and flowing out of the second heat exchanger 103 flows into the third heat exchanger 106 and then flows into the turbine 104 And the refrigerant flow F _1-1 flowing out of the first heat exchanger 101 and the refrigerant flow F _3-1 flowing out of the second heat exchanger 103 flow into the third heat exchanger 106 ). ≪ / RTI >

In one example, the temperature of the refrigerant flow (F _1-2 ) flowing out of the third heat exchanger 106 and flowing into the compressor 102 flows from the second heat exchanger 103 to the third heat exchanger The temperature of the refrigerant flow (F _{3 - 1} ) flowing into the refrigerant flow channel (106) satisfies the following general formula (3).

[Formula 3]

1 ° C ≤ T _R3Hin - T _R3Cout ≤ 20 ° C

T _R3Hout represents the temperature of the refrigerant flow F _1-2 flowing out of the third heat exchanger 106 and flowing into the compressor 102 and T _R3Cin is the temperature of the second heat exchanger 103, And the temperature of the refrigerant flow (F _{3 - 1} ) flowing into the third heat exchanger (106).

That is, the temperature (F _1-2 ) of the refrigerant flowing out of the third heat exchanger 106 and flowing into the compressor 102 flows out from the second heat exchanger 103 and flows into the third heat exchanger 106 The difference in temperature T _R3Hin - T _R3Cout of the incoming refrigerant stream (F _3-1 ) is in the range of 1 to 20 캜, such as 3 to 20 캜, 5 to 17 캜, 10 to 20 캜 or 1 to 17 캜 Lt; / RTI >

The temperature of the refrigerant flow F _1-2 flowing out from the third heat exchanger 106 and flowing into the compressor 102 flows to the second heat exchanger 103 and flows into the third heat exchanger 106 When the temperature of the refrigerant flow (F _{3 - 1} ) satisfies the above-described general formula (3), the temperature of the refrigerant flowing into the compressor 102 can be sufficiently raised to such an extent that the vaporization phenomenon of the refrigerant described above can be prevented, Thus, heat exchange efficiency of the heat recovery apparatus 10 can be increased.

The temperature of the refrigerant flow F _1-2 flowing out from the third heat exchanger 106 and flowing into the compressor 102 flows to the second heat exchanger 103 and flows into the third heat exchanger 106 The temperature of the refrigerant flow (F _{3 - 1} ) is not particularly limited as long as it satisfies the above-mentioned general formula (3), and can be variously adjusted according to the type of the process to be applied and the conditions of each process. In one example, the refrigerant flow F _1-2 flowing out of the third heat exchanger 106 and entering the compressor 102 is at a temperature of 75 ° C to 130 ° C, such as 80 ° C to 125 ° C, 90 ° C To 125 [deg.] C or 110 [deg.] C to 121 [deg.] C, but is not particularly limited thereto. The temperature of the refrigerant flow F _3-1 flowing out of the second heat exchanger 103 and flowing into the third heat exchanger 106 is 115 ° C. to 130 ° C., for example, 118 ° C. to 128 ° C. 120 deg. C to 128 deg. C, or 120 deg. C to 126 deg. C, but is not particularly limited thereto.

In one example, the temperature of the refrigerant flow F _3-2 flowing out of the third heat exchanger 106 and flowing into the turbine 104 is 70 ° C to 130 ° C, for example, 80 ° C to 120 ° C, 90 ° C to 120 ° C, 100 ° C to 118 ° C or 105 ° C to 117 ° C and the refrigerant flow F ₂ flowing out of the compressor 102 is between 110 ° C and 180 ° C, The second heat exchanger 103 may be discharged from the compressor 102 to a temperature of from 180 to 180 DEG C, from 135 DEG C to 175 DEG C or from 135 DEG C to 170 DEG C, but is not limited thereto.

As the heat recovery device of the present application includes the third heat exchanger 106, it is possible to prevent some vaporization of the refrigerant in the compressor. In this case, the refrigerant flow out of the compressor may be a gaseous stream, and the volume fraction of the gaseous stream in the refrigerant stream exiting the compressor may range from 0.95 to 1.0, for example from 0.99 to 1.0, have.

Another embodiment of the present application provides a heat recovery method. The exemplary heat recovery method can be performed using the above-described heat recovery apparatus 10, whereby, as described above, in an industrial field or in various chemical processes, for example, in the production process of petrochemical products It is possible to generate steam by using the discharged low-temperature heat source of less than 100 ° C without discarding it, and since the generated steam can be used for various processes, the amount of high temperature steam used as an external heat source for use in the reactor or the distillation column can be reduced , It is possible to maximize energy saving efficiency. Further, according to the heat recovery method of the present application, the power consumed by the compressor 102 can be produced by itself, and a part of the vaporization phenomenon of the refrigerant flow passing through the compressor 102 can be reduced, Can be recovered.

The heat recovery method according to an embodiment of the present application includes a refrigerant circulation step, a first heat exchange step and a second heat exchange step.

In one example, the heat recovery method includes a refrigerant circulation step of circulating the refrigerant flow sequentially through the first heat exchanger 101, the compressor 102, the second heat exchanger 103, and the turbine 104 . For example, the heat recovery method may include: (i) introducing a refrigerant flow into a first heat exchanger 101; (ii) flowing a refrigerant flow F ₁ out of the first heat exchanger 101 to a compressor (Iii) introducing the refrigerant flow (F ₂ ) flowing out of the compressor (102) to the second heat exchanger (103), (iv) the flow (F ₃₎ the sikimyeo inlet to the turbine (104), (v) a step of re-circulating the refrigerant flows to the refrigerant flow (F _4-1) flowing out from the turbine 104 to the first heat exchanger (101) .

The heat recovery method may further include a step of performing heat exchange between the refrigerant flow F _4-2 flowing into the first heat exchanger 101 and the first fluid flow W ₁ flowing into the first heat exchanger 101 And a second heat exchange step of exchanging the refrigerant flow (F ₂ ) flowing out of the compressor (102) with the second fluid flow (W ₃ ) flowing into the second heat exchanger (103).

The refrigerant circulation step, the first heat exchanging step, and the second heat exchanging step may be performed sequentially, or independently of each other. In addition, since the processes (i) to (v) of the refrigerant circulation step are a circulation process, any process may be performed first if the refrigerant flow can be circulated as described above.

In one example, the turbine 104 may be a generator and may be, for example, a hydraulic turbine that can convert the kinetic energy of the refrigerant flowing through the piping, that is, the fluid, into electrical energy, When the aberration is used, the power consumed by the compressor 102 can be produced by the heat recovery apparatus 10 itself, so that the coefficient of performance of the heat recovery apparatus 10 can be increased. Further, as described above in the heat recovery apparatus 10, it is possible to prevent a problem that a part of the refrigerant flow is vaporized by using the aberration.

In the exemplary heat recovery method of the present application, the temperature of the refrigerant flow (F ₁ ) flowing out of the first heat exchanger (101) and the temperature of the first fluid flow (W ₁ ) flowing into the first heat exchanger The temperature may satisfy the following general formula (1).

[Formula 1]

1 ° C ≤ T _F - T _R ≤ 20 ° C

_Wherein T _F represents the temperature of the first fluid flow W ₁ flowing into the first heat exchanger 101 and T _R represents the temperature of the refrigerant flow F discharged from the first heat exchanger 101 ₁ ) < / RTI >

When the temperature of the refrigerant flow F ₁ flowing out of the first heat exchanger 101 and the temperature of the first fluid flow W ₁ flowing into the first heat exchanger 101 satisfy the formula 1, It is possible to produce steam by using waste heat of low-temperature waste heat, in particular, a low-temperature heat source of a sensible heat of less than 100 ° C, for example, at a level of 50 to 90 ° C, and the refrigerant flowing out of the first heat exchanger The detailed description of the temperature of the first fluid flow F ₁ and the temperature condition of the first fluid flow W ₁ flowing into the first heat exchanger 101 is the same as that described in the heat recovery apparatus 10 described above, .

In the heat recovery method of the present application, the ratio of the pressure of the refrigerant flow (F ₁ ) flowing out of the first heat exchanger (101) to the pressure of the refrigerant flow (F ₂ ) flowing out of the compressor (102) Can be satisfied.

[Formula 2]

2? P _C / P _H ? 5

Where P _C represents the pressure (bar) of the refrigerant flow F ₂ flowing out of the compressor 102 and P _H represents the pressure of the refrigerant flow F ₁ flowing out from the first heat exchanger 101, (Bar).

When the ratio of the pressure of the refrigerant flow F ₁ flowing out of the first heat exchanger 101 to the pressure of the refrigerant flow F ₂ flowing out of the compressor 102 satisfies the above-mentioned general formula 2, In the heat recovery method of the present application, the refrigerant vaporized in the first heat exchanger (101) can be compressed to a high temperature and a high pressure state so as to have a sufficient amount of heat to generate steam. The detailed description of the pressure of the refrigerant flow F ₁ and the pressure of the refrigerant flow F ₂ flowing out of the compressor 102 is the same as that of the heat recovery apparatus 10 described above.

In the heat recovery method of the present application, details of the temperature, pressure and flow conditions are the same as those described above in the heat recovery apparatus 10, and will not be described.

In another embodiment of the heat recovery method of the present application, in the refrigerant circulation step, the refrigerant is circulated through the first heat exchanger 101, the compressor 102, the second heat exchanger 103 and the turbine 104 in sequence As described above, the refrigerant may be a refrigerant having a positive slope of the tangent of the saturated vapor curve of the temperature-entropy curve, for example, the horizontal axis is entropy (J / kg · K) The slope of the tangent line of the saturated vapor curve of the temperature-entropy curve being in the range of 1 to 3 at 50 < 0 > C to 130 < 0 > C. In this case, in the refrigerant circulation step, the refrigerant flow (F _1-1 ) flowing out from the first heat exchanger 101 flows into the third heat exchanger 106 and then flows into the compressor 102, after the second heat exchanger the refrigerant flow (F _3-1) flowing out of the 103 that flows into the third heat exchanger 106 it may include introducing into the turbine 104. the

In this case, in one example, the heat recovery method is a method in which the refrigerant flow (F _1-1 ) flowing out of the first heat exchanger (101) and the refrigerant flow (F _{3 -1} ) in the third heat exchanger (106). Accordingly, as described above, it is possible to prevent the partial vaporization of the refrigerant, which is generated at the time of isentropic compression of the refrigerant, and to increase the heat exchange efficiency of the heat recovery apparatus 10.

In one example, the temperature of the refrigerant flow (F _1-2 ) flowing out of the third heat exchanger 106 and flowing into the compressor 102 flows from the second heat exchanger 103 to the third heat exchanger The temperature of the refrigerant flow (F _{3 - 1} ) flowing into the refrigerant flow passage (106) may satisfy the following general formula (3).

[Formula 3]

1 ° C ≤ T _R3Hin - T _R3Cout ≤ 20 ° C

Wherein in formula 3, _R3Cout T denotes a temperature of the third flow out from the heat exchanger 106, a refrigerant flow flowing into the compressor _{(102) (F 1-2),} T R3Hin is the second heat exchanger (103) And the temperature of the refrigerant flow (F _{3 - 1} ) flowing into the third heat exchanger (106).

The temperature of the refrigerant flow F _1-2 flowing out from the third heat exchanger 106 and flowing into the compressor 102 and the refrigerant flow F flowing out of the second heat exchanger 103 and flowing into the third heat exchanger 103 _3-1 ) satisfies the above-described general formula (3), the temperature of the refrigerant flow (F _1-2 ) flowing into the compressor 102 can be sufficiently raised to such an extent that the vaporization phenomenon of the refrigerant described above can be partially prevented The heat exchange efficiency of the heat recovery apparatus 10 can be increased. In the heat recovery method, details of the specific temperature, pressure, and flow rate conditions are the same as those described above in the heat recovery apparatus 10, and will not be described.

In one example, in another embodiment of the heat recovery method, the fluid (W ₃ ) entering the second heat exchanger (103) may be water, and the exemplary heat recovery method of the present application And a steam generating step of discharging the heat-exchanged water to the refrigerant flow (F ₂ ) flowing into the two-heat exchanger (103)

Further, another embodiment of the heat recovery method may further include a step of condensing and discharging the first fluid flow flowing out from the first heat exchanger (101).

The heat recovery apparatus 10 and method of the present application can be applied to various petrochemical processes.

For example, in the case of the oxo reaction process in the production of n-butanol, the temperature of the waste heat generated in the process is about 85 ° C, in which case the amount of heat of about 7.6 Gcal / hr is discarded, . In addition, in the process of producing cumene by the alkylation reaction, the amount of heat of about 6.8 Gcal / hr is abandoned, and the present invention can be applied to the production process of the cumene. Further, in the production process of acrylic acid, the temperature of the waste heat generated in the absorber is about 75 DEG C, and in this case, the amount of heat of about 1.6 to 3.4 Gcal / hr is abandoned, so that it is applicable to the production process of acrylic acid.

According to the heat recovery apparatus and method of the present application, it is possible to generate steam by using a low-temperature heat source of less than 100 ° C discharged from an industrial site or various chemical processes, for example, a production process of a petrochemical product, Since the steam can be used in various processes, it is possible to reduce the amount of high temperature steam used as an external heat source for use in a reactor or a distillation column, thereby maximizing the energy saving efficiency, And it is possible to reduce the partial vaporization phenomenon of the refrigerant flow passing through the compressor, so that heat can be recovered with excellent efficiency.

1 is a view schematically showing a conventional waste heat treatment apparatus.
2 is a diagram schematically showing a heat recovery apparatus of an embodiment of the present application.
3 is a view schematically showing a heat recovery apparatus according to another embodiment of the present application.
4 is a graph exemplarily showing the temperature-entropy diagram of the refrigerant of the present application.
5 is a view showing a heat recovery apparatus according to an embodiment of the present application.

Hereinafter, the present application will be described in more detail by way of examples according to the present application and comparative examples not complying with the present application, but the scope of the present application is not limited by the following embodiments.

Example  One

Using the heat recovery apparatus of Fig. 2, steam was generated.

The refrigerant was circulated at a flow rate of 30,000 kg / hr so that the refrigerant (1,1,1,3,3-pentafluoropropane, R245fa) passed sequentially through the first heat exchanger, the compressor, the second heat exchanger and the aberration. Specifically, a refrigerant flow having a gas volume fraction of 0.0 at 75.4 ° C, 6.2 kgf / cm ² g (7.1 bar) is introduced into the first heat exchanger, and at the same time, the temperature of 85.0 ° C. and 1.0 kgf / cm ² g and a gas volume fraction of 0.0 was introduced at a flow rate of 300,000 kg / hr for heat exchange. After the heat exchange, the waste heat was discharged at a flow rate of 300,000 kg / hr at 81.2 ° C., 1.0 kgf / cm ² g and a gas volume fraction of 0.0. The refrigerant flow was 80.0 ° C. and 6.2 kgf / cm ² g ), And flowed into the compressor after flowing out in a state where the gas volume fraction was 1.0. Also, the refrigerant flow compressed in the compressor was discharged from the compressor at 125.0 ° C, 20.7 kgf / cm ² g (21.3 bar), and a gas volume fraction of 0.82. In this case, the amount of work used in the compressor was 214,078.0 W. At the same time, water flowing at 115.0 DEG C, 0.7 kgf / cm < ² > g and a gas volume fraction of 0.0 is introduced into the second heat exchanger at a flow rate of 1,800 kg / hr through the second heat exchanger To perform heat exchange with the refrigerant flow. The water after the heat exchange was discharged into steam at 120.0 ° C, 0.7 kgf / cm ² g and a gas volume fraction of 1.0, and the refrigerant flow was condensed to be 120 ° C., 20.7 kgf / cm ² g (21.3 bar) 0.0 > 0.0, < / RTI > The flow of the refrigerant having passed through the aberration was discharged from the turbine at 75.4 DEG C, 6.2 kgf / cm < ² > g (7.1 bar) and a gas volume fraction of 0.56, and then re-introduced into the first heat exchanger.

In this case, in the aberration, the kinetic energy of the fluid flow was used to generate 6,263.0 W of electrical energy. Further, the performance coefficient of the heat recovery apparatus was calculated by the following Formula 5, and it is shown in Table 1 below. The performance coefficient indicates the amount of heat absorbed by the heat exchange medium with respect to the energy input to the compressor, that is, the ratio of the energy recovered to the energy input amount. For example, if the coefficient of performance is 3, it means that three times as much heat as the input electricity is obtained.

[Formula 5]

In the above general formula (5), Q represents the amount of heat condensed by the second heat exchanger, and W represents the amount of work done by the compressor.

Example  2

Using the heat recovery apparatus of Fig. 5, steam was generated.

Concretely, the refrigerant (1,1,1,3,3-pentafluoropropane, R245fa) is supplied to the first heat exchanger, the third heat exchanger, the compressor, the second heat exchanger, the third heat exchanger, The refrigerant was circulated at the same flow rate of 30,000 kg / hr. ^{75.4 ℃, 6.2 kgf / cm 2} g (7.1 bar), the flow of refrigerant in the state gas volume fraction is 0.0 and the inlet group first heat, and at the same time the first heat exchanger ^{85.0 ℃, 1.0 kgf / cm 2} g, the gas Waste heat flow with a volume fraction of 0.0 was introduced at a flow rate of 300,000 kg / hr to effect heat exchange. After the heat exchange, the waste heat was discharged at a flow rate of 300,000 kg / hr at 81.2 ° C., 1.0 kgf / cm ² g and a gas volume fraction of 0.0. The refrigerant flow was 80.0 ° C. and 6.2 kgf / cm ² g ), And flowed into the third heat exchanger after flowing out with a gas volume fraction of 1.0. The refrigerant flowing out of the first heat exchanger and flowing into the third heat exchanger flows into the compressor, and the refrigerant flowing out of the compressor flows into the second heat exchanger, thereby performing heat exchange with the fluid flowing through the second heat exchanger The refrigerant flow outflowed from the second heat exchanger flows into the third heat exchanger again so that the refrigerant flows out of the first heat exchanger and exchanges heat with the refrigerant flow introduced into the third heat exchanger and then passes through the aberration. Specifically, the refrigerant flow that was heat-exchanged in the third heat exchanger was introduced into the compressor after flowing out from the third heat exchanger at a temperature of 116.1 ° C., 6.2 kgf / cm ² g (7.1 bar) and a gas volume fraction of 1.0. Also, the refrigerant flow compressed in the compressor was discharged from the compressor at 143.0 ° C, 20.7 kgf / cm ² g (21.3 bar), and a gas volume fraction of 1.0. In this case, the amount of work used in the compressor was 240,424.3 W. At the same time, water in a state of 115.0 DEG C, 0.7 kgf / cm < ² > g and a gas volume fraction of 0.0 is introduced into the second heat exchanger at a flow rate of 1,338 kg / hr through the second heat exchanger To perform heat exchange with the refrigerant flow. The water after the heat exchange was discharged into steam at 120.0 ° C., 0.7 kgf / cm ² g and a gas volume fraction of 1.0, and the condensed refrigerant flow was 122.0 ° C., 20.7 kgf / cm ² g (21.3 bar) 0.0 > 0.0 < / RTI > and flowed into the third heat exchanger. The refrigerant flowing into the third heat exchanger after the heat exchange in the second heat exchanger is heat exchanged with the refrigerant flowing out of the first heat exchanger and flowing into the third heat exchanger, and then the refrigerant flows at 116.1 ° C, 20.7 kgf / cm ² g bar), the gas volume fraction was 0.0, and the third heat exchanger was flown into the aberration. The refrigerant flowed into the aberration was introduced into the first heat exchanger after flowing out from the aberration state at 75.4 ° C, 6.2 kgf / cm ² g (7.1 bar) and a gas volume fraction of 0.36.

In this case, in the aberration, the kinetic energy of the fluid flow was used to generate 6,263.6 W of electrical energy. The performance coefficients of the heat recovery apparatus are shown in Table 1 below.

Example  3

The flow of the refrigerant heat-exchanged in the second heat exchanger was discharged at 122.0 ° C, 20.7 kgf / cm ² g (21.3 bar) and a gas volume fraction of 0.0, and then flowed into the third heat exchanger. Exchanged with the refrigerant flow introduced into the third heat exchanger. In addition, the refrigerant flow that was heat-exchanged in the third heat exchanger was discharged at a temperature of 105.5 ° C., 6.2 kgf / cm ² g (7.1 bar) and a gas volume fraction of 0.0 in the third heat exchanger, And steam was produced in the same manner as in Example 2. In this case, the performance coefficients of the heat recovery apparatus are shown in Table 1 below.

Example  4

^{73.2 ℃, 5.8 kgf / cm 2} g (6.7 bar), and introducing the flow of refrigerant in the state gas volume fraction is 0.0, a group the first heat, and at the same time the first heat exchanger ^{85 ℃, 1.0 kgf / cm 2} g, the gas The refrigerant flow was 73.2 ° C., 5.8 kgf / cm ² g (6.7 bar), and the second heat exchanger was operated at a flow rate of 300,000 kg / hr. And introduced into the third heat exchanger with a gas volume fraction of 1.0. After the heat exchange in the third heat exchanger, the refrigerant flow was introduced into the compressor at a temperature of 110.7 ° C., 5.8 kgf / cm ² g (6.7 bar), and a gas volume fraction of 1.0, After flowing out from the compressor at 138.7 ° C, 19.5 kgf / cm ² g (20.1 bar) and a gas volume fraction of 1.0, the refrigerant flowed into the second heat exchanger for heat exchange and the heat exchanged refrigerant flow in the second heat exchanger Steam was produced in the same manner as in Example 2, except that the gas was flown out at 122.0 ° C, 19.5 kgf / cm ² g (20.1 bar) and a gas volume fraction of 0.0, and then introduced into the third heat exchanger. In this case , And the performance coefficients of the heat recovery apparatus are shown in Table 2 below.

Example  5

After the heat exchange in the third heat exchanger, the refrigerant flow was introduced into the compressor at 120.2 ° C, 4.7 kgf / cm ² g (5.6 bar) and a gas volume fraction of 1.0, and the refrigerant flow compressed in the compressor was 165.4 ° C. , 21.9 kgf / cm ² g (22.5 bar), and a gas volume fraction of 1.0. The refrigerant flowed in the second heat exchanger was heat exchanged at 125.6 ° C, Steam was generated in the same manner as in Example 2, except that the gas was flown out at 21.9 kgf / cm ² g (22.5 bar), the gas volume fraction was 0.0, and then flowed into the third heat exchanger. In this case, Are shown in Table 2. < tb >< TABLE >

Comparative Example  One

Steam was produced in the same manner as in Example 1, except that the refrigerant flowed out from the second heat exchanger was introduced into the control valve instead of the aberration, expanded and then flowed out. In this case, the amount of work used in the compressor was 214,078.6 W, and the performance coefficient of the heat recovery apparatus is shown in Table 3 below.

Example 1 Example 2 Example 3 T _F (° C) T _R (° C) 85.0 80.0 85.0 80.0 85.0 80.0 T _F - T _R (° C) 5 5 5 P _C (bar) P _H (bar) 21.3 7.1 21.3 7.1 21.3 7.1 P _C / P _H 3 3 3 T _R3Hin (占 폚) T _R3Cout (占 폚) n / a n / a 122.0 116.1 122.0 105.5 T _R3Hin - T _R3Cout (占 폚) n / a 5.9 16.5 Q (W) 830,573.0 1,117,401.5 1,021,562.5 Total W (W) 207,815.0 234,160.7 234,028.0 COP 3.99 4.77 4.36 n / a: not available

Example 4 Example 5 T _F (° C) T _R (° C) 85.0 73.2 85.0 80.0 T _F - T _R (° C) 11.8 5 P _C (bar) P _H (bar) 20.1 6.7 22.5 5.6 P _C / P _H 3 4.02 T _R3Hin (占 폚) T _R3Cout (占 폚) 122.0 110.7 125.6 120.2 T _R3Hin - T _R3Cout (占 폚) 11.3 5.4 Q (W) 1,068,510.0 1,131,601.0 Total W (W) 231, 427.2 284,785.0 COP 4.62 3.97

Comparative Example 1 T _F (° C) T _R (° C) 85.0 80.0 T _F - T _R (° C) 5 P _C (bar) P _H (bar) 21.3 7.1 P _C / P _H 3 T _R3Hin (占 폚) T _R3Cout (占 폚) n / a n / a T _R3Hin - T _R3Cout (占 폚) n / a Q (W) 830,573.0 Total W (W) 214,078.6 COP 3.88

10: Heat recovery device
101: first heat exchanger
102: compressor
103: second heat exchanger
104: Turbine
105: Storage tank
106: third heat exchanger
F ₁ : refrigerant flow out of the first heat exchanger
F _1-1 : refrigerant flow flowing out of the first heat exchanger and flowing into the third heat exchanger
F _1-2 : Flow of refrigerant flowing out of the third heat exchanger to the compressor
F _3-1 : refrigerant flow flowing out of the second heat exchanger and flowing into the third heat exchanger
F _3-2 : refrigerant flow flowing out of the third heat exchanger and flowing into the aberration
F ₂ : Refrigerant flow out of the compressor
F ₃ : refrigerant flow out of the second heat exchanger
F _4-1 : Refrigerant flow from the turbine
F _4-2 : refrigerant flow flowing into the first heat exchanger
W ₁ : the first fluid flow into the first heat exchanger
W ₂ : the first fluid flow flowing out of the first heat exchanger
W ₃ : the second fluid flow entering the second heat exchanger
W ₄ : second fluid flow heat exchanged in the second heat exchanger
CP: critical point
SVC: Saturated steam curve

Claims (38)

A first heat exchanger, a compressor, a second heat exchanger and a turbine fluidly connected through a pipe through which refrigerant flows,
The refrigerant flow entering the first heat exchanger is heat exchanged with the first fluid flow entering the first heat exchanger,
The refrigerant flow out of the first heat exchanger flows into the compressor,
The refrigerant flowing out of the compressor flows into the second heat exchanger and is heat-exchanged with the second fluid flowing into the second heat exchanger,
The refrigerant flow out of the second heat exchanger flows into the turbine,
The refrigerant flowing out of the turbine flows into the first heat exchanger,
The turbine is an aberration that converts the kinetic energy of the refrigerant flow into electric energy,
The first heat exchanger is an evaporator for evaporating a liquid refrigerant flow into a gaseous refrigerant flow,
Wherein the second heat exchanger is a condenser for condensing the gaseous refrigerant flow into a liquid refrigerant flow. delete The heat recovery apparatus according to claim 1, wherein the temperature of the refrigerant flow flowing out of the first heat exchanger and the temperature of the first fluid flow flowing into the first heat exchanger satisfy the following formula 1:
[Formula 1]
1 ° C ≤ T _F - T _R ≤ 20 ° C
In the above general formula (1), T _F represents the temperature of the first fluid flowing into the first heat exchanger, and T _R represents the temperature of the refrigerant flowing out of the first heat exchanger. The heat recovery apparatus according to claim 1, wherein the ratio of the pressure of the refrigerant flow flowing out of the first heat exchanger to the pressure of the refrigerant flow flowing out of the compressor satisfies the following formula 2:
[Formula 2]
2? P _C / P _H ? 5
In the general formula 2, P _C represents the pressure (bar) of the refrigerant flow flowing out of the compressor, and P _H represents the pressure (bar) of the refrigerant flow flowing out of the first heat exchanger. The heat recovery apparatus according to claim 1, wherein the flow rate of the refrigerant flowing through the pipe is 5,000 kg / hr to 50,000 kg / hr. The apparatus of claim 1, wherein the temperature of the refrigerant stream flowing into the first heat exchanger is between 60 ° C and 90 ° C. The heat recovery apparatus of claim 1, wherein the first fluid stream entering the first heat exchanger is a stream of condensed water that has passed through a waste heat stream or condenser. The heat recovery apparatus of claim 1, wherein the flow rate of the first fluid flow into the first heat exchanger is 50,000 kg / hr to 500,000 kg / hr. The apparatus of claim 1, wherein the temperature of the first fluid stream entering the first heat exchanger is between 60 ° C and 100 ° C. The heat recovery apparatus of claim 1, wherein the temperature of the first fluid stream exiting the first heat exchanger is 60-100 占 폚. The apparatus of claim 1, wherein the temperature of the refrigerant flow exiting the first heat exchanger is between 60 ° C and 100 ° C. The heat recovery apparatus of claim 1, wherein the temperature of the refrigerant flow exiting the compressor is between 110 ° C and 180 ° C. The heat recovery apparatus of claim 1, wherein the second fluid introduced into the second heat exchanger is water, and the heat-exchanged water in the second heat exchanger is discharged into steam. The heat recovery apparatus of claim 1, wherein the temperature of the refrigerant flowing out of the second heat exchanger is in the range of 115 to 130 캜. 14. The heat recovery apparatus of claim 13, wherein the temperature of the steam is 115 to 125 DEG C and the pressure of the steam is 0.5 to 0.9 kgf / cm < ² > g. The heat recovery apparatus of claim 1 wherein the temperature of the refrigerant stream exiting the turbine is between 60 ° C and 90 ° C. The heat recovery apparatus of claim 1, wherein the flow rate of the second fluid flow entering the second heat exchanger is 300 kg / hr to 6,000 kg / hr. 2. The heat recovery apparatus of claim 1, wherein the refrigerant is a refrigerant having a slope of a tangent line of a saturated vapor curve of a temperature-entropy line having a positive slope. 19. The heat recovery apparatus of claim 18, wherein the slope of the tangent of the saturated vapor curve of the temperature-entropy line is 1 to 3 at 50 占 폚 to 130 占 폚. 19. The heat recovery apparatus according to claim 18, wherein the refrigerant is at least one selected from the group consisting of R245fa, R1234ze, and R1234yf. 19. The apparatus of claim 18 further comprising a third heat exchanger fluidly connected to the piping between the first heat exchanger and the compressor and the second heat exchanger and the turbine,
The refrigerant flowing out of the first heat exchanger flows into the compressor after being introduced into the third heat exchanger,
The refrigerant flowing out of the second heat exchanger flows into the turbine after being introduced into the third heat exchanger,
Wherein the refrigerant flowing out of the first heat exchanger and the refrigerant flowing out of the second heat exchanger are heat-exchanged in the third heat exchanger. The method according to claim 21, wherein the temperature of the refrigerant flowing out of the third heat exchanger and flowing into the compressor and the temperature of the refrigerant flowing out of the second heat exchanger and flowing into the third heat exchanger satisfies the following formula 3 Device:
[Formula 3]
1 ° C ≤ T _R3Hin - T _R3Cout ≤ 20 ° C
In the formula (3), T _R3Cout represents the temperature of the refrigerant flowing out of the third heat exchanger and flowing into the compressor, and T _R3Hin represents the temperature of the refrigerant flowing out of the second heat exchanger and flowing into the third heat exchanger . 22. The apparatus of claim 21, wherein the temperature of the refrigerant stream flowing out of the second heat exchanger is between about < RTI ID = 0.0 > 115 C < / RTI > 22. The heat recovery apparatus of claim 21, wherein the temperature of the refrigerant flow exiting the third heat exchanger and flowing into the turbine is between 70 DEG C and 130 DEG C. 22. The heat recovery apparatus of claim 21, wherein the temperature of the refrigerant flow exiting the third heat exchanger and entering the compressor is between 75 DEG C and 135 DEG C. 22. The heat recovery apparatus of claim 21, wherein the temperature of the refrigerant flow exiting the compressor is between 130 ° C and 180 ° C. The refrigerant flowing into the first heat exchanger, the refrigerant flowing out of the first heat exchanger into the compressor, the refrigerant flowing out of the compressor into the second heat exchanger, and the refrigerant flowing out of the second heat exchanger A refrigerant circulation step of introducing a flow of the refrigerant into the turbine and flowing a refrigerant flow out of the turbine into the first heat exchanger;
A first heat exchanging step of exchanging a refrigerant flow flowing into the first heat exchanger with a first fluid flow flowing into the first heat exchanger; And
And a second heat exchange step of exchanging a refrigerant flow out of the compressor with a second fluid flow flowing into the second heat exchanger,
The turbine is an aberration that converts the kinetic energy of the refrigerant flow into electric energy,
The first heat exchanger is an evaporator for evaporating a liquid refrigerant flow into a gaseous refrigerant flow,
Wherein the second heat exchanger is a condenser for condensing a gaseous refrigerant flow into a liquid refrigerant flow. delete The heat recovery method according to claim 27, wherein the temperature of the refrigerant flow flowing out of the first heat exchanger and the temperature of the first fluid flow flowing into the first heat exchanger satisfy the following formula 1:
[Formula 1]
1 ° C ≤ T _F - T _R ≤ 20 ° C
In the above general formula (1), T _F represents the temperature of the first fluid flowing into the first heat exchanger, and T _R represents the temperature of the refrigerant flowing out of the first heat exchanger. The heat recovery method according to claim 27, wherein the ratio of the pressure of the refrigerant flow out of the first heat exchanger to the pressure of the refrigerant flow out of the compressor satisfies the following formula 2:
[Formula 2]
2? P _C / P _H ? 5
In the general formula 2, P _C represents the pressure (bar) of the refrigerant flow flowing out of the compressor, and P _H represents the pressure (bar) of the refrigerant flow flowing out of the first heat exchanger 28. The method of claim 27, wherein the refrigerant is a refrigerant having a slope of the tangent of the saturated vapor curve of the temperature-entropy curve having a positive slope. 28. The method of claim 27, wherein the slope of the tangent of the saturated vapor curve of the temperature-entropy line is 1 to 3 at < RTI ID = 0.0 > 50 C & 28. The method as claimed in claim 27, wherein the refrigerant circulation step comprises: flowing the refrigerant flowing out of the first heat exchanger into the third heat exchanger, then flowing the refrigerant into the compressor, flowing the refrigerant flowing out of the second heat exchanger into the third heat exchanger To the turbine. The heat recovery method according to claim 33, further comprising a third heat exchange step of exchanging a refrigerant flow out of the first heat exchanger and a refrigerant flow out of the second heat exchanger in a third heat exchanger, Way. The method according to claim 33, wherein the temperature of the refrigerant flowing out of the third heat exchanger and flowing into the compressor and the temperature of the refrigerant flowing out of the second heat exchanger and flowing into the third heat exchanger satisfy the following formula 3: Way:
[Formula 3]
1 ° C ≤ T _R3Hin - T _R3Cout ≤ 20 ° C
In the general formula (3), T _R3Cout represents the temperature of the refrigerant flowing out of the third heat exchanger and flowing into the compressor, and T _R3Hin represents the temperature of the refrigerant flowing out of the second heat exchanger and flowing into the third heat exchanger. 28. The method of claim 27, wherein the second fluid entering the second heat exchanger is water. The heat recovery method according to claim 36, further comprising a steam generating step of discharging the heat exchanged water to the refrigerant flow flowing into the second heat exchanger as steam. 28. The method of claim 27, further comprising condensing and discharging the fluid stream exiting the first heat exchanger.

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