KR101773151B1 - Method for supplying heat source for hydrothermal carbonization of organic waste - Google Patents

Abstract

Disclosed are a heat source supply system for hydrothermal carbonization of organic waste and a heat source supply method using the same. According to an embodiment of the present invention, the heat source supply system for hydrothermal carbonization of organic waste comprises: a first hydrothermal carbonization reactor which stores organic waste; a second hydrothermal carbonization reactor which is connected to the first hydrothermal carbonization reactor in parallel and stores organic waste; a steam supply device which supplies steam to the first and second hydrothermal carbonization reactors; a first transfer line which transfers steam to the first and second hydrothermal carbonization reactors; a second transfer line which transfers steam, remaining in either the first hydrothermal carbonization reactor or the second hydrothermal carbonization reactor, to the other reactor; and a heating means which is installed on the outsides of the first and second hydrothermal carbonization reactors and heats the first and second hydrothermal carbonization reactors. The organic waste, accommodated in the first and second hydrothermal carbonization reactors, is heated multiple times by the steam, supplied by the steam supply device and the second transfer line, and the heating means.

Description

[0001] METHOD FOR SUPPLYING HEAT SOURCE FOR HYDROTHERMAL CARBONIZATION OF ORGANIC WASTE [0002]

The present invention relates to a method of supplying a heat source for hydrothermal carbonization of organic wastes.

The London Convention, concluded in 1972, is a convention on the prevention of marine pollution by dumping of waste and other substances. The Government of the Republic of Korea has enforced the ban on marine dumping of organic wastes such as sewage sludge and livestock manure by 2012 under the London Convention. Therefore, it is urgent to secure alternative technologies for the treatment of organic wastes.

As a result, studies on the resource conversion technology of organic wastes that produce solid fuels and biogas by hydrothermal carbonization of organic wastes are actively under way. In this case, the organic waste can be heated by direct heating (steam) or indirect heating to be hydrothermally carbonized.

However, when the organic waste is heated by the direct heating method (steam), there is a problem that condensation water of about 50 to 60% of the total amount of the organic waste is generated and the system capacity is inevitably increased.

Further, when the organic waste is heated by the indirect heating method, there is a problem that the temperature rise time of the organic waste becomes long due to the high moisture content and high viscosity of the organic waste, thereby lowering the temperature rise efficiency.

Korean Registered Patent No. 10-1087775 (Registered on November 22, 2011)

Embodiments of the present invention provide a heat source supply system for hydrothermal carbonization of organic wastes which can raise the temperature raising efficiency of organic wastes by heating the organic wastes by a direct heating method or an indirect heating method a plurality of times, do.

According to an aspect of the present invention, there is provided a method for producing a hydrothermal reaction product, comprising: a first hydrocracking reactor in which organic wastes are stored; a second hydrocracking reactor connected in parallel with the first hydrocracking reactor, 2 a steam feeder for supplying steam to the hydrothermal carbonization reactor, a first transfer line for transferring the steam to the first hydrocracker and the second hydrocarboner, and a second transfer line for transferring the steam to the first hydrocracker and the second hydrocracker, A second transfer line for transferring the steam remaining in any one of the first hydrocracking reactor and the second hydrocracking reactor to another one of the first hydrocracking reactor and the second hydrocracking reactor and a second transfer line mounted on an outer surface of the first hydrocracking reactor and the second hydrocracking reactor, And a heating means for applying heat to the first hydrocracking reactor and the second hydrocracking reactor, wherein the first hydrocracking reactor and the second hydrocracking reactor 2 A heat source supply system for hydrothermal carbonization of organic wastes, wherein the organic waste contained in the hydrothermal carbonization reactor is heated by the steam feeder, the steam supplied by the second transfer line, and the heating means a plurality of times, may be provided.

A first valve installed in a first transfer line connecting the steam feeder and an upper portion of the first hydrocracker, and a first valve installed in a first transfer line connecting the steam feeder and a lower portion of the first hydrocracker A second valve, a third valve installed in a first transfer line connecting the steam feeder and the upper portion of the second hydrocracker, and a third transfer line connecting the steam feeder and the lower portion of the second hydrocracker And a control unit for controlling the amount of opening of the first valve to the fourth valve and the amount of heat generated by the heating unit.

In addition, the heating means may include an outer jacket provided to surround at least a part of an outer surface of the first hydrocracking reactor and the second hydrocracking reactor.

The heat hydrolysis apparatus according to any one of claims 1 to 3, further comprising: a heat oil supplier for supplying heat oil to the heating means; a heat exchanger provided between the heat oil supplier and the first hydrothermal carbonization reactor and the second hydrothermal carbonization reactor, A second hydrocracking reactor, a second hydrocracking reactor, a second hydrocracking reactor, a second hydrocracking reactor, a second hydrocracking reactor, and a second hydrocracking reactor, Further comprising a fruit or vegetable discharge valve for controlling a flow rate of the fruit oil discharged from any one of the hydrothermal carbonization reactor and the second hydrocracking reactor, wherein the opening amount of the fruit or vegetable oil supply valve and the fruit or vegetable discharge valve is controlled by the control unit Lt; / RTI >

Also, the reaction occurring in the first hydrocracking reactor and the second hydrocracking reactor may be a hydrothermal carbonization reaction for hydrothermally carbonizing the organic waste, and the hydrothermal reaction may be performed in the first hydrocracking reactor and the second hydrocracking reactor It can happen alternately.

According to another aspect of the present invention, there is provided a method for producing a hydrothermal reaction product, comprising: introducing an organic waste into a first hydrocracking reactor; firstly heating the organic waste by supplying steam to the first hydrocracking reactor; Heating the organic waste to a second temperature by supplying steam remaining in the connected second hydrocracking reactor to the first hydrocracking reactor, heating the organic solvent supplied to the heating means mounted on the outer surface of the first hydrocracking reactor, A step of raising the temperature of the first hydrocracking reactor by a predetermined amount of time, a step of raising the temperature of the organic wastes by a third time, And supplying the heat to the second hydrothermal reactor using a heat source supply system for hydrothermal carbonization of organic wastes It may provide a supply method.

In addition, the step of maintaining the temperature of the first hydrocracking reactor may be performed simultaneously with the step of injecting the organic waste into the second hydrocracking reactor.

Embodiments of the present invention can provide a heat source supply system for hydrothermal carbonization of organic wastes which can raise the temperature raising efficiency by heating organic wastes by a direct heating method or an indirect heating method a plurality of times, and a method of supplying a heat source using the same.

1 is a view schematically showing a configuration of a heat source supply system for hydrothermal carbonization of organic wastes according to an embodiment of the present invention.
Fig. 2 is a diagram showing the operation sequence of Fig. 1. Fig.
3 is a graph showing sludge viscosity, sludge thermal conductivity, and water thermal conductivity in the process of raising the temperature of the first hydrothermal reactor of FIG.
FIG. 4 is a graph showing the internal temperature of the first hydrothermal reactor in the process of raising the temperature of the first hydrothermal reactor of FIG. 1;

DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS Hereinafter, configurations and operations according to embodiments of the present invention will be described in detail with reference to the accompanying drawings. DETAILED DESCRIPTION OF THE INVENTION The following description is one of many aspects of the claimed invention and the following description may form part of the detailed description of the invention.

However, the detailed description of known configurations or functions in describing the present invention may be omitted for clarity.

While the invention is susceptible to various modifications and its various embodiments, it is intended to illustrate the specific embodiments and the detailed description. It is to be understood, however, that the invention is not to be limited to the specific embodiments, but includes all modifications, equivalents, and alternatives falling within the spirit and scope of the invention.

Terms including ordinals such as first, second, etc. may be used to describe various elements, but the elements are not limited by such terms. These terms are used only to distinguish one component from another.

It is to be understood that when an element is referred to as being "connected" or "connected" to another element, it may be directly connected or connected to the other element, .

The terminology used in this application is used only to describe a specific embodiment and is not intended to limit the invention. The singular expressions include plural expressions unless the context clearly dictates otherwise.

1 is a view schematically showing a configuration of a heat source supply system for hydrothermal carbonization of organic wastes according to an embodiment of the present invention.

In the present specification, Hydrothermal Carbonization (HTC) means a material obtained by mixing a material having a low water content with water or a material having a high water content in a closed type reactor to raise the temperature. When the temperature is raised, water is saturated and water vapor pressure And the carbonization reaction proceeds without water evaporation.

Referring to FIG. 1, a heat source supply system 10 for hydrothermal carbonization of organic wastes according to an embodiment of the present invention includes a first hydrocracking reactor 100, a second hydrocracking reactor 200, a steam supplier 300 The first transfer line 401, the second transfer line 402, the third transfer line 403, the fourth transfer line 404, the fifth transfer line 500, the heating means 600, A feeder 700 and a control unit 800. [

The first hydrothermal reactor 100 may be hydrothermally carbonized by receiving organic waste. In order to supply such organic waste, an organic waste supply unit (not shown) may be disposed at the tip of the first hydrocracking reactor 100. The organic waste supply unit may include an organic waste storage tank (not shown) storing organic waste and a mono pump (not shown) for transporting organic waste.

The first hydrothermal reactor 100 may have a container shape in which organic wastes are accommodated and form an enclosed space. In addition, an agitator (not shown) may be installed in the first hydrocracking reactor 100. The organic waste contained in the first hydrocracking reactor (100) can be uniformly mixed by the stirrer.

Meanwhile, in order to hydrothermally carbonize the organic waste in the first hydrocracking reactor 100, the organic waste must be heated to about 200 ° C. For this, the first hydrocracker 100 may be supplied with steam from the steam supplier 300. For example, the first hydrocracker 100 may be supplied with steam corresponding to about 10% of the total amount of the organic wastes, and the organic wastes may be heated using the steam. Also, the first pyrolysis reactor 100 may be provided with a first reactor thermometer (not shown) for measuring the reaction temperature of the organic waste.

Specifically, the steam feeder 300 is connected to the upper portion of the first hydrocracking reactor 100 or the lower portion of the first hydrocracking reactor 100 via the first feed line 401 and the second feed line 402 .

The first valve 410 may be installed in the first transfer line 401 connecting the upper portion of the first hydrocracking reactor 100 and the steam supply unit 300 and the lower portion of the first hydrocracking reactor 100 A second valve 420 may be installed in the second feed line 402 connecting the steam feeder 300. The first valve 410 and the second valve 420 can control the flow rate of the steam in the first transfer line 401 and the second transfer line 402 and the first and second valves 410, 420 may be disposed at the tip of the steam flow meter (not shown) for measuring the flow rate of the steam.

Steam may be simultaneously introduced into the first hydrocracking reactor 100 and the first hydrocracking reactor 100 through the first transfer line 401 and the second transfer line 402. The steam introduced into the first hydrocracking reactor (100) directly heats the organic waste in the first hydrocracking reactor (100), so that the organic waste can be firstly heated. For example, organic wastes can be heated to about 80 ° C by steam.

Since the contact area between the steam and the organic waste is increased at the same time as the steam is introduced into the upper portion of the first hydrocracking reactor 100 and the lower portion of the first hydrocracking reactor 100, The heating efficiency of the organic waste can be improved.

In addition, the first hydrocracking reactor (100) can receive residual steam remaining in the second hydrocracking reactor (200). Here, the residual steam means steam remaining in the second hydrocracker 200 after the hydrothermal reaction in the second hydrocracker 200 is terminated.

A third valve 430 may be installed in the third transfer line 403 connecting the steam supply unit 300 and the upper portion of the second hydrocracker 200. The steam supply unit 300 and the second A fourth valve 440 may be installed in the fourth transfer line 404 connecting the lower portion of the hydrothermal carbonization reactor 200. The third valve 430 and the fourth valve 440 can control the flow rate of the steam in the third transfer line 403 and the fourth transfer line 404 and the third and fourth valves 430, 440) may be disposed at the tip of the steam flow meter (not shown) for measuring the flow rate of the steam.

Specifically, when the first hydrocracking reactor 100 is heated by the steam, the first valve 410 and the third valve 430 are opened, and the remaining residues in the second hydrocracking reactor 200 The steam may be introduced into the upper portion of the first hydrocracking reactor 100 through the third transfer line 403 and the first transfer line 401

However, the spirit of the present invention is not limited thereto. For example, the second valve 420 and the third valve 430 are opened so that residual steam remaining in the second hydrocracker 200 is transferred to the third transfer line 403, the fifth transfer line 500, And the second transfer line 402 to the lower portion of the first hydrocracking reactor 100. [ The second valve 420 and the fourth valve 440 are opened so that the residual steam remaining in the second hydrocracking reactor 200 flows through the fourth transfer line 404 and the second transfer line 402 1 hydrocracking reactor (100). In addition, the first valve 410 and the fourth valve 440 are opened so that residual steam remaining in the second hydrocracking reactor 200 flows through the fourth transfer line 404, the fifth transfer line 500, May be introduced into the first hydrocracking reactor (100) through the first transfer line (401).

Thus, the residual steam flowing into the first hydrocracking reactor 100 can directly heat the organic waste in the first hydrocracking reactor 100, so that the organic waste can be secondarily heated. As an example, the organic waste may be heated to about 120 ° C by residual steam. At this time, the first hydrocracker (100) can receive residual steam corresponding to about 10% of the total amount of steam supplied from the feeder (300).

In order to measure the flow rate of the residual steam, residual steam flow rate measuring devices (not shown) may be disposed at the ends of the first to fourth valves 410, 420, 430 and 440.

After the hydrothermal reaction is completed in the second hydrocracking reactor 200 and the residual steam remaining in the second hydrocracking reactor 200 is transferred to the first hydrocracking reactor 200, The reaction product produced in the reaction vessel 200 may be discharged to the reaction product storage tank (not shown).

Thus, the temperature of the reaction product discharged from the second hydro-carbonation reactor (200) can be lowered. Accordingly, the operation cost can be reduced and the energy efficiency can be improved compared with the conventional method using a cooling utility (not shown) such as a heat exchanger to utilize a high-temperature reaction product.

Since the hydrothermal reaction occurs alternately in the first hydrocracking reactor 100 and the second hydrocracking reactor 200, the first hydrocracking reactor 100 may remain in the second hydrocracking reactor 200, Steam can be supplied. In this way, it is also possible that residual steam remaining in the first hydrocracking reactor 100 after the hydrothermal reaction in the first hydrocracking reactor 100 is supplied to the second hydrocracking reactor 200 .

In addition, the first hydrocracking reactor 100 can be heated by the heating means 600. At this time, the heating means 600 may be an outer jacket mounted on the outer surface of the first hydrothermal reactor (100).

Specifically, the heating means 600 can receive the fruit oil from the fruit juice feeder 700. At this time, a hot water supply valve 710 is provided between the heating means 600 and the hot water supply device 700 to control the flow rate of the hot water supplied to the heating means 600. For this purpose, a heat flow meter (not shown) for measuring the flow rate of the heat of the supplied oil may be disposed at the tip of the heat supply valve 710.

In this case, the heating oil supplied to the heating means 600 can be indirectly heated while being circulated inside the heating means 600. As a result, the organic waste can be heated to a tertiary temperature to reach a hydrothermal reaction temperature. For example, the organic waste can be heated up to about 200 ° C.

When organic wastes reach the hydrothermal reaction temperature, organic wastes have a high water content, so that carbonization can occur in the first hydrothermal reactor 100 even if no additional water is supplied.

In addition, when the hydrothermal reaction is completed in the first hydrocracking reactor 100, the heating oil supplied to the heating means 600 may be discharged. For this purpose, a heat oil discharge valve 720 is provided between the heating means 600 and the heat oil supply device 700 to control the flow rate of the heat energy discharged. For this purpose, a flow rate meter (not shown) for measuring the flow rate of the heat of the discharged heat can be disposed at the tip of the flow rate sensor 720.

Further, when the heating oil is discharged from the heating means 600, the temperature of the first hydrothermal reactor (100) can be maintained for a predetermined time. At the same time, organic waste can be introduced into the second hydrothermal reactor (200). The organic waste introduced into the second hydrocracking reactor (200) may be heated to the same temperature as that of the first hydrocracking reactor (100). This will be described later.

Although not shown, a solid-liquid separator, a dryer, an anaerobic digester, and the like may be disposed at the rear end of the first hydrocracking reactor 100. Accordingly, the reaction products of the first hydrocracking reactor 100 and the second hydrocracking reactor 200 stored in the reaction product reservoir may be transferred to the solid-liquid separator and separated into a solid product and a gaseous product. At this time, the solid product can be dried in the dryer, and the liquid product can be anaerobically digested in the anaerobic digester. Thus, a solid fuel can be obtained from the dryer, and a biogas can be obtained from the anaerobic digester.

The second hydrocracking reactor 200 has a function of performing a hydrothermal reaction when the hydrothermal reaction is completed in the first hydrocracking reactor 100. The second hydrocracking reactor 200 is connected to the first hydrocracking reactor 100 through a fifth transfer line 500, (100) in parallel

Specifically, the second hydrocracker 200 may be connected to the first hydrocracking reactor 100 through a fifth transfer line 500. At this time, the second hydrocracking reactor (200) can receive the organic waste at the time when the hydrothermal reaction of the first hydrocracking reactor (100) is terminated.

Specifically, the hydrothermal reaction is terminated in the first hydrocracking reactor 100, and the supply of the organic waste is introduced into the second hydrocracking reactor 200 while the temperature is maintained by interrupting the supply of the heat oil to the heating means 600 . Also, the second pyrolysis reactor 200 may be provided with a second reactor thermometer (not shown) for measuring the reaction temperature.

The second hydrocracker reactor 200 receives steam from the steam supplier 300 and the organic waste fed into the second hydrocracker 200 is heated up to about 80 ° C through steam.

As the residual steam remaining in the first hydrocracking reactor 100 is supplied to the second hydrocracker reactor 200, the organic waste can be secondarily heated to about 120 ° C through the residual steam.

In addition, the organic waste can be heated up to about 200 ° C. by the heat oil circulated inside the heating means 600 mounted on the outer surface of the second hydrocracker 200.

Thus, the first hydrocracking reactor 100 and the second hydrocracking reactor 200 can reduce the energy required to raise the temperature of the organic waste by exchanging the residual steam after the hydrothermal reaction.

The control unit 800 includes a first hydrocracking reactor 100, a second hydrocracking reactor 200, a steam supplier 300, first to fourth valves 410, 420, 430, and 440, The hot water supply valve 710, and the hot water discharge valve 720 can be controlled. For example, the control unit 800 receives the measured or analyzed values from the first reactor thermometer, the second reactor thermometer, the steam flow meter, the residual steam flow meter, and the thermal oil flow meter, The first hydrothermal reactor 100, the second hydrocracker 200, the steam supplier 300, the first to fourth valves 410, 420, 430 and 440, the oil feeder 700, (710), and the hot melt discharge valve (720). For example, the controller 800 may be a small built-in computer, and may include a data processor including a program, a memory, and a CPU.

The program may be used to determine the operation of the first hydrocracking reactor 100 based on the values measured or analyzed from the first reactor thermometer, the second reactor thermometer, the steam flow meter, the residual steam flow meter, The operation of the second hydro-carbonation reactor 200, the operation of the steam supplier 300, the operation of the hot oil supplier 700, the opening amount of the first to fourth valves 410, 420, 430 and 440, An algorithm for controlling the amount of opening of the valve 710 and the amount of opening of the filler oil discharge valve 720. The program may be stored in a memory unit such as a flexible disk, a compact disk, a hard disk, or an MO (magneto optical disk), and installed in the control unit 800.

In addition, the control unit 800 can automatically store values measured or analyzed from the first reactor thermometer, the second reactor thermometer, the steam flow meter, the residual steam flow meter, and the flow rate meter continuously in a database , Various alarm system for safety can be built to prepare for safe driving

According to the present invention, the heat source supply system 10 for hydrothermal carbonization of organic wastes according to an embodiment of the present invention raises the temperature of organic wastes to hydrothermally carbonize organic wastes without moisture evaporation, Since all of the heating methods are used, the temperature rise time can be reduced.

In addition, since residual steam generated in the process of hydrothermal carbonization of organic wastes is used again to raise the temperature of the organic wastes, the energy consumption can be reduced compared with the conventional method, and the heating energy required for raising the organic wastes can be reduced can do.

Hereinafter, the operation sequence of the heat source supply system for hydrothermal carbonization of the organic waste according to one embodiment of the present invention will be described with reference to FIG. Fig. 2 is a diagram showing the operation sequence of Fig. 1. Fig.

Referring to FIG. 2, the heat source supply system 10 for hydrothermal carbonization of organic wastes may alternately operate the first hydrothermal reactor 100 and the second hydrothermal reactor 200.

The operation of the first hydrocracking reactor 100 and the second hydrocracking reactor 200 can be performed by a) supplying organic wastes, b) heating the organic wastes first, c) heating the organic wastes secondarily, d) Temperature rise step, e) temperature holding step, f) residual steam exchange step, and g) reaction product discharge step.

In the meantime, any one of the first hydrocracking reactor 100 and the second hydrocracking reactor 200 may be operated in the first hydrocracking reactor 100 or the second hydrocracking reactor 200 It is assumed that the other of the first hydrocracking reactor 100 and the second hydrocracking reactor 200 is restarted.

Herein, " initial operation " means that any one of the first hydrocracking reactor 100 and the second hydrocracking reactor 200 is heated by the steam of the steam feeder 300, Means that the first hydrocracking reactor 100 and the second hydrocracking reactor 200 are heated once by the steam of the steam feeder 300, The steam is once again heated by residual steam remaining in the hydrothermal reactor 100 and the other hydrothermal reactor 200 and is heated again by the oil of the heating means 600.

a) Organic waste  Supply step

A predetermined amount of organic waste is supplied to the first hydrothermal reactor (100).

b) Organic waste  Primary Heating  step

The first valve 410 and the second valve 420 are opened so that the steam is simultaneously introduced into the upper and lower portions of the first hydrocracking reactor 100 and the organic waste is firstly heated up to about 80 ° C.

c) Organic waste  Secondary Heating  step

The first valve 410 and the third valve 430 are opened so that residual steam remaining in the second hydrocracking reactor 200 flows through the third transfer line 403 and the first transfer line 401, And then flows into the upper part of the hydrothermal reactor (100) for about 30 minutes.

The second valve 420 and the third valve 430 are opened while residual steam remaining in the second hydrocracking reactor 200 flows into the upper portion of the first hydrocracking reactor 100, Residual steam remaining in the reactor 200 flows through the third transfer line 403, the fifth transfer line 500, and the second transfer line 402 to the lower portion of the first hydrocrack reactor 100 for about 30 minutes ≪ / RTI >

Thereby, the organic waste is secondarily heated to about 120 캜.

d) Organic waste  Third Heating  step

By supplying the heating oil to the heating means 600 and heating it, the organic waste is thirdly heated to about 200 占 폚.

e) temperature maintenance step

The heating means 600 cuts off the supply of the fruit oil. And the temperature of the first hydrothermal reactor (100) is maintained for about 30 minutes. Meanwhile, organic wastes are supplied to the second hydrocracking reactor 200 at this stage, and the second hydrocracking reactor 200 repeats steps a) to g) from this point.

f) Residual steam exchange step

The first valve 410 and the third valve 430 are opened so that residual steam remaining in the first hydrocracking reactor 100 flows through the first transfer line 401 and the third transfer line 403, And then flows into the upper part of the hydrothermal reactor (200).

The first valve 410 and the fourth valve 440 are opened while residual steam remaining in the first hydrocracking reactor 100 flows into the upper portion of the second hydrocracking reactor 200, Residual steam remaining in the reactor 100 flows into the lower portion of the second hydrocrack reactor 200 through the first transfer line 401, the fifth transfer line 500, and the fourth transfer line 404.

g) Reaction product discharge step

The residual steam is discharged from the first hydrocracking reactor 100 and the lowered temperature reaction product is discharged to a separate reaction product storage tank (not shown).

The first hydrocracking reactor 100 and the second hydrocracking reactor 200 are different from the first hydrocracking reactor 100 and the second hydrocracking reactor 200 only at the starting point of step a) Can be carried out sequentially in steps a) to e).

Hereinafter, an experiment for raising the temperature of the organic waste for hydrothermal carbonization of the organic waste using the heat source supply system for hydrothermal carbonization of the organic waste according to an embodiment of the present invention will be described with reference to FIG. 3 and FIG. FIG. 3 is a graph showing sludge viscosity, sludge thermal conductivity and water thermal conductivity in the course of raising the temperature of the first hydrothermal reactor of FIG. 1, FIG. 4 is a graph showing the sludge viscosity, A graph showing the internal temperature of the carbonization reactor.

Referring to FIG. 3, a heater is installed in the center of the first hydrocracking reactor 100 and the second hydrocracking reactor 200, and a temperature sensor is installed at equal intervals to measure the temperature from the heater by distance.

In order to measure the thermal conductivity of the organic waste (objective sample), the temperature difference of the substance (reference sample) having a known thermal conductivity under the same output was measured, and the temperature difference of the organic waste was measured under the same conditions. Then, the thermal conductivity of the organic waste was derived from the following equation (1). At this time, the reference sample was selected as water containing a large amount of organic waste.

[Equation 1]

Ka = Kb *? Tb /? Ta

Here, Ka denotes the thermal conductivity of the target sample, Kb denotes the thermal conductivity of the reference sample, ΔTb denotes the instantaneous temperature difference of the target sample, and ΔTa denotes the instantaneous temperature difference of the reference sample.

As a result of calculating the thermal conductivity value according to the temperature difference of the organic waste based on the measurement of the thermal conductivity, the organic waste has a low thermal conductivity value of about 0.05 W / m ° C at the early stage (about 20 ° C). However, as the hydrothermal reaction proceeds, the organic waste has a thermal conductivity value of about 0.7 W / m DEG C at about 190 DEG C, as the physical properties of the organic waste change. This is a value of thermal conductivity similar to that of water. From this viewpoint, it can be seen that heat transfer is smooth as the temperature of the organic waste increases.

As a result, as the temperature of the organic waste increases, the thermal conductivity of the organic waste increases, and the rate of temperature rise of the organic waste increases.

The viscosity of the organic waste was measured by sensing the shear force generated between the impeller and the organic waste by the torque value and quantifying the relationship between the torque and the viscosity while operating the stirrer at the same rotational speed in the hydrothermal reaction process.

In addition, the torque value of a substance having a known viscosity (water contained in a large amount of organic waste) is measured first, and then the torque change value of the organic waste is measured based on the measured torque value, Respectively.

As a result, organic wastes have a high viscosity value of about 220,000 cP at initial (about 20 ° C), but when organic wastes are heated to about 80 ° C, the viscosity of the organic wastes sharply decreases to about 55,000 cP, It can be seen that when the temperature is raised to about 200 ° C, the organic waste has a low viscosity of about 2 cP.

From this viewpoint, as the temperature of the organic waste increases, the viscosity of the organic waste decreases, so that the efficiency of stirring the organic waste can be maximized and the rate of temperature rise of the organic waste can be accelerated.

4, the first hydrocracking reactor 100 is firstly heated using steam, and then secondarily heated using residual steam of the second hydrocracking reactor 200. Then, And the mixture was heated with oil three times. The first hydrocracking reactor 100 is divided into an upper region, an intermediate region, and a lower region, and a temperature sensor is installed in each region.

Also, in consideration of the load of the agitator due to the high viscosity of the organic waste, the agitator is operated at about 50 rpm when the feed rate of the organic waste is 50%, and when the feed rate of the organic waste is 100% And when the internal temperature of the first hydrothermal reactor 100 reached 100 캜, the stirrer was operated at about 150 rpm.

As a result, it can be seen that the temperature of the first hydrocrack reactor 100 gradually increases in both the upper region, the middle region, and the lower region.

While the present invention has been described in connection with what is presently considered to be practical exemplary embodiments, it is to be understood that the invention is not limited to the disclosed embodiments, but, on the contrary, You will understand. For example, a person skilled in the art can change the material, size and the like of each constituent element depending on the application field or can combine or substitute the embodiments in a form not clearly disclosed in the embodiments of the present invention, Of the range. Therefore, it should be understood that the above-described embodiments are to be considered in all respects as illustrative and not restrictive, and that such modified embodiments are included in the technical idea described in the claims of the present invention.

10: Heat source supply system for hydrothermal carbonization 100: First heat hydrolysis reactor
200: Second hydrocarbonation reactor 300: Steam supplier
401: first conveyance line 402: second conveyance line
403: Third conveying line 404: Fourth conveying line
410: first valve 420: second valve
430: third valve 440: fourth valve
500: fifth conveying line 600: heating means
700: Fruit feeder 710: Fruit feeder valve
720: Fruit-oil drain valve 800:

Claims (7)

A supply step of supplying the organic waste to the first hydrothermal reactor;
A first step of raising a temperature of the organic waste supplied to the first hydrocracking reactor by supplying steam to the first hydrocracking reactor;
A second step of raising the temperature of the primary heated organic waste by supplying residual steam remaining in the second hydrocracking reactor connected in parallel with the first hydrocracking reactor to the first hydrocracking reactor;
A third temperature raising step of raising the temperature of the secondarily heated organic waste by supplying the thermal oil to the heating means mounted on the outer surface of the first hydrothermal reactor;
Maintaining the temperature of the first hydrocracking reactor for a predetermined time by shutting off supply of the heat oil from the heating means; And
And a steam exchange step of supplying residual steam remaining in the first hydrocracking reactor to the second hydrocracking reactor,
In the temperature maintenance step,
The step of supplying the organic waste to the second hydrocracking reactor is performed,
In the primary heating step,
The steam is supplied to the upper and lower portions of the first hydrocracking reactor when the steam is supplied to the first hydrocracking reactor,
In the secondary heating step,
Wherein the residual steam is supplied to upper and lower portions of the first hydrocracking reactor when the residual steam is supplied from the second hydrocracking reactor to the first hydrocracking reactor,
Method of supplying heat source for hydrothermal carbonization of organic waste.
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