KR102168283B1 - System to automatically control the air supply to dry organic sludge - Google Patents

Abstract

The present invention relates to a system for automatically controlling air supply to dry organic sludge, comprising: a bio-drying device in which a bio-drying process is performed while organic sludge and air are supplied and discharged; a first index measuring means which is capable of measuring a first index including a temperature during the bio-drying process; a second index measuring means which is capable of measuring a second index including a CO_2 concentration during the bio-drying process; and a control means which automatically controls air supply of air supplied to the bio-drying device. It is possible to efficiently remove moisture by adjusting air supply in a process of drying organic sludge through a control method according to the present invention.

Description

System to automatically control the air supply to dry organic sludge}

The present invention relates to an air supply amount automatic control system for drying organic sludge, and more specifically, to an air supply amount automatic control system capable of efficiently removing moisture by adjusting the air supply amount in drying the sludge through a bio-drying process. About.

Herein, background art related to the present disclosure is provided, and these do not necessarily mean known art.

In general, sludge is a sediment separated from liquid generated during treatment of sewage and wastewater, and as the construction of domestic sewage and wastewater treatment plants continues to increase along with industrial development, the amount of sludge generated is also increasing.

When sludge is landfilled due to its high moisture content of around 75~80%, it shortens the life of the landfill, generates odors, increases the generation and concentration of leachate, and causes soil and groundwater pollution around the landfill. It provides a reason for increasing the processing cost due to excessive management cost. In addition, such high moisture content decreases the calorific value during incineration, thereby increasing the amount of auxiliary fuel used, and air pollutants such as chlorine compounds and dioxin due to the decrease in incineration temperature are generated.

However, the sludge contains about 80% of moisture, but more than 97% of the remaining moisture is made of organic matter, so the calorific value during drying is approximately 3,000 kcal/kg or more, which is very valuable as an energy source. Therefore, it is known that by drying sewage sludge and developing it into pellet fuel, it is possible to minimize environmental pollution caused by treatment of sewage sludge and to create high economic value.

Conventional treatment of sewage sludge is a method of collecting the sludge, mixing sawdust, waste synthetic resin, coal, etc. into the sludge, molding it, and then drying it again to produce pellet fuel in the form of pellets. These conventional sludge treatment methods and facilities tend to rely on aerobic composting using microorganisms, anaerobic digestion using methane bacteria, and heat drying using steam from a boiler.

Accordingly, it is required to introduce measures for reducing energy costs, improving treatment efficiency, and environmentally friendly treatment that does not cause civil complaints. In particular, when considering the conversion and utilization of new and renewable energy by drying organic wastes such as sewage sludge, continuous structural improvement is required in the future.

The present invention is an air supply amount automatic control system capable of efficiently removing moisture by controlling the air supply amount in the process of drying organic sludge through a series of processes, and can be particularly suitably used for a bio-drying process. It is intended to provide an automatic control system for air supply.

However, the objects of the present invention are not limited to the above-mentioned objects, and other objects that are not mentioned will be clearly understood by those skilled in the art from the following description.

The present invention is a bio-drying apparatus in which a bio-drying process is performed while supplying and discharging organic sludge and air; A first index measuring means capable of measuring a first index including a temperature in the bio-drying process; A second index measuring means capable of measuring a second index including the concentration of CO ₂ in the bio-drying process; And a control means for automatically controlling the supply amount of air supplied to the bio-drying device, wherein the control means sets the input variables and then the air supply amount according to the index value measured by the first index measurement means. It provides an automatic air supply amount control system for drying organic sludge, characterized in that the air supply amount is automatically adjusted by adjusting the air supply amount according to the index value measured by the second index measurement means.

As an air supply amount automatic control system that can efficiently remove moisture by controlling the air supply amount in the process of drying organic sludge through the control method according to the present invention, in particular, automatic control of air supply amount suitable for bio-drying process System can be provided.

1 to 3 illustrate a control method algorithm according to an embodiment of the present invention.
4 to 8 show the configuration of a bio-drying apparatus to which an air supply amount automatic control system for drying organic sludge according to an embodiment of the present invention is applied.

All technical and scientific terms used in the present specification have the same meaning as commonly understood by those of ordinary skill in the art unless otherwise stated. Also throughout the specification and claims, unless otherwise stated, the term "comprise, comprises, comprising" means to include the recited object, step or group of objects, and steps, and any other It is not used to exclude objects, steps, or groups of objects or steps.

Before describing the present invention in detail below, it is understood that the terms used in the present specification are for describing specific embodiments and are not intended to limit the scope of the present invention, which is limited only by the scope of the appended claims. shall.

Meanwhile, various embodiments of the present invention may be combined with any other embodiments unless there is a clear opposite point. Any feature indicated to be particularly preferred or advantageous may be combined with any other feature and features indicated to be preferred or advantageous. Hereinafter, embodiments of the present invention and effects thereof will be described with reference to the accompanying drawings.

The automatic air supply amount control system according to the present invention can be particularly suitably applied when the filling ratio of organic sludge is 50% or more. According to the control command of the control means, the amount of air supplied to the bio-drying device is adjusted by adjusting the number of rotations of the blower fan. If the amount of air supply is too large, it is advantageous to discharge the internal air containing moisture, but the internal temperature of the bio-drying device is too low to prevent the decomposition of organic components. Conversely, if the amount of air supply is too small, the internal temperature of the bio-drying device is reduced. It is advantageous for the decomposition of organic components, but it is important to maintain an adequate supply amount because the internal air containing moisture is not discharged smoothly.

When organic sludge is supplied to the upstream side of the bio-drying device, the internal temperature increases as the bio-drying process proceeds toward the downstream side, and accordingly, the amount of water vapor evaporated from the downstream side increases. At this time, if air is supplied to the upstream side along with the organic sludge, the water vapor already contained in the downstream side includes more water vapor that evaporates from the downstream side, so this water vapor reaches a supersaturated state and condenses again and is dried on the downstream side. There is a problem that efficiency decreases.

The automatic control system for the amount of air supply for drying organic sludge according to an embodiment of the present invention is applied to a bio-drying apparatus configured in which the directions in which organic sludge is supplied and discharged and the direction in which air is supplied and discharged are reversed, and supplied dry and It is possible to minimize the decrease in drying efficiency on the downstream side by contacting the low temperature air with the discharged organic sludge to prevent condensation.

The automatic control system for the amount of air supply for drying organic sludge according to an embodiment of the present invention is more specifically a bio-drying device in which a bio-drying process is performed while supplying and discharging organic sludge and air, in the bio-drying process. A first indicator measuring means capable of measuring a first indicator, a second indicator measuring means capable of measuring a second indicator in the bio-drying process, and automatically controlling the supply amount of air supplied to the bio-drying device It includes a control means. For convenience, the side to which organic sludge is supplied is defined as the upstream side and the side from which the dried sludge is discharged is defined as the downstream side.

The first indicator measurement means is a means for measuring a first indicator in the bio-drying process, the first indicator includes temperature information, and may be provided inside the bio-drying apparatus. The organic sludge introduced into the bio-drying device is converted into carbon dioxide (CO ₂ ), water (H ₂ O), ammonia (NH ₃ ), etc. through the metabolism of aerobic microorganisms using oxygen (O ₂ ) in the supplied air. During decomposition, metabolic heat is generated, and moisture is evaporated by the generated metabolic heat, thereby performing a drying process. At this time, there is an optimum temperature for drying and metabolism of aerobic microorganisms, and the drying conditions of the bio-drying device can be controlled by measuring the temperature as a first index.

The first indicator measuring means is provided with at least one or more from the upstream side to the downstream side of the bio-drying device. In the case of having one of the first indicator measuring means, it may be provided on an upstream side, a downstream side, an air supply unit or an air discharge unit of the bio-drying device, and two or more, for example, five first indicator measurement means When equipped, the 1-1 indicator measuring means, the 1-2 indicator measuring means, the 1-3 indicator measuring means, the 1-4 indicator measuring means, the 1-5 indicator measuring means from the upstream side to the downstream side It may be provided at regular intervals.

The second indicator measuring means is a means capable of measuring a second indicator in the bio-drying process, the second indicator including CO ₂ concentration information, and in an upstream side of the bio-drying device or an air discharge pipe It can be provided. A high CO ₂ concentration also means a high temperature, so it is possible to control the drying conditions of the bio-drying apparatus by measuring the CO ₂ concentration as a second indicator.

The present invention is not a method of controlling the air supply amount of the bio-drying process by using only the temperature of the exhaust gas as an independent indicator in the past, and further optimization of drying performance by utilizing the CO ₂ concentration in the exhaust gas as a common indicator for the control of the air supply amount. To induce.

Temperature change is easy to measure and is an indicator that intuitively indicates the dry state of the bio-drying device, but it is affected by various factors such as internal and external factors, and biological, chemical, and physical factors, and the temperature is aerobic decomposition. It is a result of the reaction and is an indicator that acts as an influencing factor of this reaction. Therefore, if the air supply is controlled by measuring only the temperature change, it is difficult to directly identify the cause of the abnormal temperature change due to an excessive increase or decrease in temperature. It is relatively insensitive to changes in the state of sludge (decomposition, etc.), and the rate of temperature change due to heat transfer is also relatively slow, making it difficult to quickly control according to the internal state of the drying means.

Accordingly, the exhaust gas temperature (or internal temperature) and the CO ₂ concentration are used as common indicators to control the bio-drying process, that is, repeat the routine including the primary control according to the temperature change and the secondary control according to the change of CO ₂ concentration. By doing this, drying performance can be optimized.

In the bio-drying process, metabolic heat of aerobic microorganisms alone or as the main dry heat source is generated from the aerobic decomposition reaction of biodegradable organic substances, and the degree of this decomposition reaction can be specified as the concentration of CO ₂ in the exhaust gas. In addition, since the change of CO ₂ concentration is first observed before the temperature of the exhaust gas changes, it is a reaction index that is more sensitive to determining the activity of microorganisms than the temperature change due to the generation of metabolic heat. Can be controlled.

However, optimal bio by controlling the to measure only the CO ₂ concentration control the air flow rate also is not a suitable control method control according to the temperature change and complementary to exactly proportional to the change in concentration of CO _2, because not the temperature change Automatic control that provides drying effect is possible.

Ammonia generated by the metabolism of microorganisms as said second indicator (NH ₃₎ Concentration can also be used as an index, but the reliability for identifying soluble nature of the drying conditions in the water so dropped as compared with the case of NH ₃ CO ₂ second It is desirable to measure the change in CO ₂ concentration as an indicator.

The control means is a means for automatically controlling the supply amount of air supplied through the air supply unit. By receiving measurement data from the indicator measuring means and controlling (maintaining or changing) the air supply amount by the blower, the biodrying device The internal or exhaust gas temperature and CO ₂ concentration are maintained within a certain range, and the dried state (water content) of the discharged organic sludge is maintained at a certain level.

The control method in the control means is a method of controlling the amount of air supplied from the downstream side in the process of biodrying while organic sludge is supplied to the upstream side of the bio-drying device and transferred to the downstream side, and is considered to start air supply. Change the air supply amount so that the measured current exhaust gas temperature (T _t ) indicates between the upper limit (T _UL ) and the lower limit (T _LL ) after the start of operation of the dryer (t _s ), and additionally measured current It follows an algorithm to change the amount of air supply so that the exhaust gas CO ₂ concentration (C _t ) can indicate between the concentration upper limit (C _UL ) and the lower limit (C _LL ).

At this time, the air supply amount is changed within the range of the upper limit of air supply (F _UL ) and the lower limit (F _LL ), and when the air supply amount is changed based on the current temperature (T _t ), the current air supply amount set value (F _t ) Increase or decrease by the specified change amount (dF ₁ ) in, and when changing the air supply amount based on the current concentration (C _t ), increase or decrease by the specified change amount (dF ₂ ) from the current air supply amount set value (F _t ) or Decrease.

Specifically, the control method according to the present invention includes a setting step (S100) of setting input variables for the control means; Initial supply step (S200) of supplying air to the bio-drying apparatus by starting the operation of the blower connected to the air supply unit; A first control step (S300) of adjusting the air supply amount according to the temperature measured by the first indicator measuring means; And a second control step (S400) of supplying air at the air supply amount controlled in the first control step and then adjusting the air supply amount according to the CO ₂ concentration measured by the second indicator measuring means after a certain period of time elapses. .

In addition, the control method in the control means includes a routine including a first control step and the second control step after a set change air supply amount application time has elapsed after supplying air with the air supply amount controlled in the second control step. After drying the organic sludge that is continuously injected repeatedly, it is continuously discharged. A control method algorithm according to an embodiment of the present invention is shown in FIGS. 1 to 3.

The setting step (S100) is a setting step of setting input variables for the control means, and input variables include a lower temperature limit (T _LL ), an upper temperature limit (T _UL ), a lower limit of CO ₂ concentration (C _LL ), and a CO ₂ concentration. Upper limit (C _UL ), air supply lower limit (F _LL ), air supply upper limit (F _UL ), initial air supply (F _i ), manual operation application time (t _m ), change air supply application time (dt), temperature It includes the amount of change in the amount of air supply (dF ₁ ) and the amount of change in the amount of air supply according to the concentration of CO ₂ (dF ₂ ).

The initial supply step (S200) is a step of supplying air corresponding to the initial supply amount (F _i ) to the bio-drying device by starting the operation of the blower, and an amount of air corresponding to the initial air supply amount (F _i ) is supplied. When possible, the blower is initially operated and the initial air supply start point (t _s ) is input (recorded), and the initial air supply amount (F _i ) is input (recorded) as the current air supply amount (F _t ).

Since it takes some time for the decomposition of the first organic component to start, a constant initial air supply amount (F _i ) is maintained for a certain period of time (t _m ) regardless of the internal temperature or exhaust gas temperature of the bio-drying device.

For the first control step (S300), the control means first inputs the current time (t _a ) (current time) before the air supply amount change, and the current time (t _a ) before the input air supply amount change, and the initial air supply start time. The difference value of (t _s ) is calculated, and at the point when the difference value becomes larger than the set manual operation application time (t _m ) (the current point before the change in air supply amount (t _a )), measured by the first indicator measurement means. Enter the current temperature (T _t ).

When the first control and the second control step immediately after the initial supply step are referred to as the first routine, in the case of the first control according to the second routine after the first routine, the control means is the current point before the change in the air supply amount according to the second routine. (t _a) the input, and changes the air supply amount of the primary routine (or maintained) after calculating a difference value between the current point in time (t _b) and (t _a) prior to the current point in time the air supply amount changes, the difference value is a preset At the point when the change air supply amount becomes greater than the application time (dt) (the present time after the air supply amount change (t _b )), the current temperature (T _t ) measured by the first indicator measuring means is input.

The first control step (S300) is a step of determining whether or not the amount of air supply changes by measuring the current temperature (T _t ) at regular time intervals (dt), the current temperature (T _t ) measured by the first indicator measuring means. ) Is within or out of the range of the lower temperature limit (T _LL ) and the upper temperature limit (T _UL ), and determines whether to adjust the air supply amount according to the calculation result.

More specifically, when it is calculated that the measured current temperature (T _t ) falls within the range of the set lower temperature limit (T _LL ) and the upper temperature limit (T _UL ), this means that the air supply amount and the internal temperature are in balance, The air corresponding to the current air supply amount F _t (in the case of initial operation, the initial air supply amount F _i ) is continuously supplied during the change air supply amount application time dt (S310).

If the measured current temperature (T _t ) is calculated to be higher than the set temperature upper limit (T _UL ), this means that the internal temperature is too high and the moisture-containing air is not discharged smoothly, so the amount of air supplied by the blower is reduced. Increase (S320).

Specifically, the air supply increase control calculates the new current air supply amount (F _t ) by adding the initial air supply amount (F _i ) or the current air supply amount (F _t ) to the air supply amount change amount (dF ₁ ) according to temperature, and Supply. That is, after increasing the air supply amount by the amount of air supply change (dF ₁ ) according to the preset temperature, the second index of the bio-drying process (in this case, the CO ₂ concentration) is observed.

Conversely, when the measured current temperature (T _t ) is calculated to be lower than the lower temperature limit (T _LL ), this means that the moisture-containing air is discharged smoothly, but the internal temperature is too low, and aerobic decomposition of organic components due to insufficient moisture. Since it means that is not active, the amount of air supplied by the blower is reduced (S330).

Specifically, the air supply reduction step (S330) calculates an initial air flow (F _i) or obtained by subtracting the air flow rate change (dF ₁₎ according to the temperature of the current air flow rate (F _t) a new current air flow rate (F _t) and thereby Supply the appropriate air. In other words, after setting the amount of change in the amount of air supply (dF ₁ ) according to the temperature in advance, and once the amount of air supply is reduced by only the amount of change (dF ₁ ) that is set, the second index of the bio-drying process (in this case, the concentration of CO ₂ ) I made it look.

Next, the second control step (S400) measures the current temperature (T _t ) in the immediately preceding first control step (S300) to determine whether or not the amount of air supply has changed. As a step of determining whether the current concentration (C _t ) is changed at each time interval (dt), and the current CO ₂ concentration (C _t ) measured by the second indicator measuring means is the lower concentration limit (C _LL ) and Whether to fall within or out of the range of the upper concentration limit value (C _UL ) is calculated, and it is determined whether to adjust the air supply amount according to the calculation result.

For the second control step (S400), first, the control means inputs the current point t _b after the change (or maintenance) of the air supply amount in the first control step immediately before. In addition, the difference between the current time (t _b ) and the current time (t _a ) before the air supply change is calculated after the change (or maintenance) of the air supply amount, and the difference is greater than the preset change air supply application time (dt). At (the present time after the change in the air supply amount (t _b )), enter the present time (t _a ) before the change in the new air supply amount.

In the drying method according to the present invention, the comparison object of the current time point (t _a ) before the air supply amount change is the initial air supply start time point (t _s ), and the comparison object at the present time point (t _b ) after the air supply amount change is the air supply amount change. As the previous present time point (t _a ), the current time point (t _a , t _b ) is recorded as two types because the targets for comparison are different.

That is, the minimum time (dt) for which the changed air supply amount is applied is set in advance, and the air supply amount (F _t ) increased or decreased by the preset change amount (dF ₁ or dF ₂ ) is applied during the set time (dt). I made it possible.

The control means inputs the current CO ₂ concentration (C _t ) measured by the second indicator measuring means at the current time point (t _a ) before the new air supply amount change. Thereafter, the same process as the process after the above-described first calculation step is repeated while the calculation is performed on the input current CO ₂ concentration (C _t ).

Specifically, the current CO ₂ concentration (C _t ) measured by the second indicator measuring means in the second control step (S400) falls within the range of the lower limit of CO ₂ concentration (C _LL ) and the upper limit of CO ₂ concentration (C _UL ). It calculates whether or not it is out of range, and adjusts the air supply amount again according to the calculation result.

The second control step (S400) is a step of increasing, decreasing, or maintaining the amount of air supplied by the blower according to the calculated result, control for continuously supplying air (S410), control for increasing the air supply amount (S420). ) Or control (S430) to reduce the amount of air supplied may be performed.

More specifically, in the second control step (S400), when the current CO ₂ concentration (Ct) is calculated to fall within the range of the set lower limit of CO ₂ concentration (C _LL ) and the upper limit of CO ₂ concentration (C _UL ), the change air Air corresponding to the current air supply amount (F _t ) is continuously supplied during the supply amount application time (dt) (S410).

In the second control step (S400), if the current CO ₂ concentration (Ct) is calculated to be higher than the set CO ₂ concentration upper limit (C _UL ), it is expected that the internal temperature will be too high and the moisture-containing air is discharged smoothly. Since it is expected not to lose, the air supply amount is increased (S420).

Specifically, increasing the control air feed is present in the air feed rate (F _t) plus the air supply amount of change (dF ₂₎ calculating a new current air flow rate (F _t) and supplies the air equivalents. That is, after increasing the amount of air supply by the amount of change in the amount of air supply set in advance (dF ₂ ), the change of the internal index (in this case, temperature) of the bio-drying device is observed.

On the contrary, in the second control step (S400), if the current CO ₂ concentration (C _t ) is calculated to be lower than the set lower limit of CO ₂ concentration (C _LL ), it is expected that the moisture-containing air is discharged smoothly, but the internal temperature is too low. Since it is expected, the amount of air supply is reduced (S430).

Specifically, the air supply reduction step (S430) calculates the new current air flow rate (F _t) present in the air feed rate (F _t) obtained by subtracting the air flow rate change (dF ₂₎ and supplying air equivalents. That is, the change in the amount of air supply (dF ₂ ) is set in advance, and the amount of air supply is reduced only by the set amount of change (dF ₂ ), and then the change in the internal index (in this case, temperature) of the bio-drying device is observed.

The control means checks the current concentration (C _t ) through the second control step and measures the current temperature (T _t ) again after a certain period of time (dt/2) from the point when it determines whether or not the air supply amount changes, and changes the air supply amount. Return to the process of determining whether or not.

More specifically, the difference between the current time point (t _b ) after the change in air supply amount and the present time point before the change in air supply amount (t _a ) is calculated, and the difference value is greater than the change air supply amount application time (dt). At the time point t _b , a new routine is performed by repeating the operation of inputting the current time point t _a before the new air supply amount change. That is, similar to the first control step in the first routine, at the current time (t _a ) before the change in the new air supply amount, the current temperature (T _t ) measured by the first indicator measuring means is input and the input current temperature ( While performing an operation on T _t ), the above-described process is repeated.

The position where the current CO ₂ concentration is measured for the control according to the present invention is provided with the second indicator measuring means on the upstream side of the bio-drying means or on the line through which air is discharged, and the value measured at the corresponding position is the current CO ₂ concentration. It is used as (C _t ).

The location for measuring the current temperature can be set in various ways. First, if one first indicator measuring means is provided, it is installed at any position of the bio-drying means, and the value measured at that position can be used as the current temperature (T _t ), but preferably upstream of the bio-drying device. It is recommended to use the current temperature (T _t ) installed on the side or downstream side and measured at the location. More preferably, it is preferable to use the current temperature (T _t ) as the value measured at the corresponding position by being installed on the upstream side of the bio-drying device or in the line through which air is discharged.

Even when a plurality of first indicator measuring means are provided, they may be installed at any position of the bio-drying means, and in this case, the average value of the measured values at each position may be used as the current temperature (T _t ).

As an air supply amount automatic control system that can efficiently remove moisture by controlling the air supply amount in the process of drying organic sludge through the control method according to the present invention, in particular, automatic control of air supply amount suitable for bio-drying process System can be provided.

The automatic control system for the amount of air supply for drying organic sludge according to an embodiment of the present invention is a bio-drying apparatus in which a bio-drying process is performed while supplying and discharging organic sludge and air configured as shown in FIGS. 4 to 8 ( It can be particularly suitably applied to automatically control the amount of air supplied to 20).

The bio-drying device 20 is a means for performing a bio-drying process for organic sludge treatment that improves the fermentation efficiency of microorganisms and efficiently removes moisture evaporated by the fermentation decomposition heat, and induces eco-friendly drying. It includes a drum dryer, which is a means of inducing rotation to secure voids while maintaining the composition of.

4 to 8 are exemplary diagrams showing the bio-drying apparatus in more detail, FIG. 4 is a plan view schematically showing an internal and external configuration of the bio-drying apparatus, and FIG. 5 is a schematic diagram showing a configuration different from that of FIG. It is an exemplary side view indicated by. In addition, FIG. 6 is an exemplary view showing a shape of a front part and a part of the central part of the bio-drying device viewed from the direction A of FIG. 4, and FIG. 7 is a view illustrating a shape of the first mantle part viewed from the direction B of FIG. 5. This is an example diagram. In addition, FIG. 8 is an exemplary view showing a spiral configured in all of the bio-drying apparatus.

4 to 8, the bio-drying apparatus 20 of the present invention includes a drum 23, a mantle 21, 22, a driving unit 24: 24a, 24b, and an air supply unit 28. do.

The drum 23, together with the mantle portions 21 and 22, serves to form a space for drying the organic sludge and to blend the organic sludge. Specifically, the drum 23 is formed in the shape of one long pipe in one direction, and the first mantle portion 21 and the second mantle portion 22 are respectively coupled to the front opening and the rear opening to close the front opening and the rear opening. do. Organic sludge is injected into the drum 23 through the first mantle part 21, air is discharged, and the dried organic sludge is discharged through the second mantle part 22. In the drum 23, a means for crushing, blending, and transferring organic sludge is provided, and the means for crushing, blending, and transporting are fixedly installed on the drum 23 and the organic sludge is rotated by the rotation of the drum 23. Is crushed, blended and transferred. To this end, a driving unit 24 for rotating the drum 23 is coupled to the outside of the drum 23. Basically, the drum 23 continuously rotates in one direction and blends by dropping the organic sludge to induce contact with the air and prevent agglomeration and coagulation between particles.

The drum 23 may be divided into three sections: a front portion 23a, a middle portion 23b, and a rear portion 23c. Here, the section is for convenience of description and does not necessarily have to be classified as such. However, as will be described below, each section has a different moving speed of the organic sludge, and each section is classified according to the moving speed. That is, the bio-drying apparatus 20 of the present invention changes the moving speed of the organic sludge in the drum in which drying is performed, so that the optimum drying efficiency is achieved. This change in movement speed is achieved by means such as the spiral 25 and the lift blade 27 in contact with the organic sludge, and in the present invention, the drum 23 is installed and used in a parallel state that does not tilt. .

Specifically, organic sludge having a high moisture content is injected through the first mantle portion 21 to the entire 23a of the drum 23. The organic sludge having a high moisture content has a high viscosity due to the moisture content, is attached to and fixed inside the drum 23, and forms a lump between the organic sludges. Therefore, the moisture content is rapidly lowered in the whole 23a, and the organic sludge in the form of a lump is crushed, as well as rapid transfer and stirring. To this end, the entire 23a is provided with a spiral 25 and a wire 26.

It serves to raise the organic sludge by the rotation of the drum 23 of the spiral 25 and to rapidly move toward the central portion 23b when falling. To this end, the spiral 25 is arranged so that a plurality of blades form a spiral inside the drum 23 and serves to move the organic sludge injected into the entire 23a to the rear, and this operation is performed to lift the organic sludge. & Is proceeded by the fall process.

The wire 26 is installed so as to cross the inside of the drum 23 by connecting two points of the inner wall of the drum 23 as shown in FIGS. 4, 5 and 6. A plurality of such wires 26 are installed, and as shown in FIGS. 4 and 5, one end and the other end of the wire 26 are coupled to the inside of the drum 23 so as to deviate from each other. That is, one end is coupled to the front of the front end (23a), the other end is coupled to the inner wall of the drum 23 by retreating in the direction of the central portion (23b) compared to the one end. At this time, the wire 26 is installed so as to pass through the center of the cross section of the drum 23. Accordingly, when a plurality of wires 26 are installed, the wires 26 are arranged radially based on the cross-sectional center as shown in FIG. 6, and the wires 26 meander and cross each other when viewed from the side.

The wire 26 allows the organic sludge lifted and widened by the spiral 25 to be divided and crushed by contact with the wire 26 when it falls, so that primary blending is performed. This wire 26 serves to pulverize the agglomeration of organic sludge, which has a strong initial viscosity, but has low mechanical strength, so that the organic sludge is kept as small particles, and air discharged through the first mantle part 21 and By increasing the contact rate of, it enables rapid initial drying.

A plurality of lift blades 27 are provided in the central portion of the drum 23. The lift blades 27 are provided in plural at regular intervals such that the blade blades are parallel to the longitudinal direction of the drum 23 (a direction connecting the first mantle portion and the second mantle portion) (a direction orthogonal to the cross-sectional direction). As shown, a plurality of lift blades 27 are installed in a circumferential direction to form one row, and such blade rows are installed across the central portion 23b at regular intervals.

The lift blade 27 serves to lift and fall of the organic sludge transferred from the front 23a, and serves to be transferred to the rear at a very slow speed. To this end, as shown in FIG. 6, the blade end of the lift blade 27 may be bent at a predetermined angle (eg, 120° to 140°) so that a large amount of organic sludge can be lifted. This bent portion may be determined in an area not exceeding half the length of the lift blade 27.

In addition, the organic sludge may be disposed at an angle within several degrees in a state parallel to the longitudinal direction so that the organic sludge can move in the direction of the rear part 23c at a very slow speed within the drum 23. That is, as shown in FIG. 4, the lift blades 27 are arranged in the longitudinal direction L and the blades side by side, and at this time, the lift blades 27 may be coupled into the drum 23 so as to be oblique with respect to the line connecting the longitudinal direction L. That is, the organic sludge is disposed obliquely in this form, so that the organic sludge can be moved backward little by little in the process of lifting or falling. Through this, it is possible to move the organic sludge at a very slow speed compared to the whole 23a in the central part 23b, and it is possible to increase the contact time with air. In particular, when moving at a high speed, the efficiency of using the inner space of the drum 23 is reduced, but due to the movement at a slow speed, the organic sludge can be sufficiently filled inside the drum, thereby preventing a decrease in efficiency.

On the other hand, a lift blade 27 for mixing or lifting organic sludge is not installed at the rear of the drum 23. The length of the rear part 23c can be changed in various ways depending on the amount of organic sludge to be dried, the diameter and length of the drum 23, and the moving speed of the organic sludge, but about 1/4 to 1/6 of the total length Can be determined as

The organic sludge dried in the middle part 23b is transferred to the rear part 23c. At this time, since the blade lift 27 for transport is not installed, the accumulated state is maintained, and the accumulated organic sludge acts as an obstacle to the organic sludge passing through the central portion 23b. That is, the movement in the rear portion 23c is performed as the organic sludge accumulated in the rear portion 23c is pushed out according to the transfer of the organic sludge dried in the middle portion 23b. The moving speed of the organic sludge moving in the middle part 23b is lowered by the organic sludge accumulated in the rear part 23c, and through this, the filling rate of the inside of the drum 23, that is, the organic sludge existing in the The amount will increase. That is, the organic sludge stays inside the drum 23 for a long time, and the contact between the organic sludge containing a large amount of microorganisms and the organic sludge containing relatively few microorganisms increases, thereby preventing a decrease in drying efficiency. As described above, it is possible to increase the utilization rate of the inner space of the drum 23.

The organic sludge accumulated in the rear part 23c is gradually pushed out and moved to the second mantle part 22, and transfer means connected to the second mantle part 22 or the heat provided in the second mantle part 22 It is discharged to the outside through the joint 36.

The mantle portions 21 and 22 are provided to seal the openings before and after the drum 23 and to connect the inside and the outside of the drum 23. To this end, the mantle portions 21 and 22 are configured to include a first mantle portion 21 and a second mantle portion 22.

The first mantle portion 21 is coupled to the front opening 23a side. The first mantle part 21 is provided with an inlet 30 so that organic sludge is injected from a mixer (not shown). In particular, a discharge pipe 31 to which a dust collection pipe (not shown) is connected may be provided in the first mantle part 21. The discharge pipe 31 is connected to the inlet 30 pipe so that the air inside the drum 23 discharged through the inlet 30 pipe can move to the dust collector (not shown) through the dust collection pipe. To this end, the discharge pipe 31 is coupled to an opening formed at an upper end of the inlet 30. On the other hand, at one end of the discharge pipe 31, that is, a portion exposed to the inside of the drum 23, a dust discharge port 29 is provided.

The dust outlet 29 is formed in a tubular shape in communication with the inlet 30, and is installed standing up toward the top of the drum (here, the upper end means the far side from the ground) in a direction forming a right angle with the inlet 30 . The suction part of the dust discharge port 29 protrudes into the drum as shown, and the lower part (a part facing the floor) is formed to be inclined. The lower part is communicated and internal air is sucked into the dust discharge port 29 through the lower part. In the lower portion of the drum 23, a strainer may be provided to limit the discharge of dust inside the drum 23 through the dust discharge port 29.

Meanwhile, the dust outlet 29 and the discharge pipe 31 may be connected through the inlet 30, but a connection pipe connecting the dust outlet 29 and the discharge pipe 31 may be provided in the inlet 30. However, if the amount of organic sludge discharged through the discharge pipe 31 is sufficient and the discharge port of the organic sludge provided in the discharge pipe 31 is formed toward the bottom of the discharge pipe 31, the connection pipe is omitted and the discharge pipe ( Using the upper space of 31), the dust discharge port 29 and the discharge pipe 31 can be communicated.

The second mantle portion 22 is coupled to an opening on the rear portion 23c side of the drum 23. When the second mantle part 22 is provided with the connector 36, the dried organic sludge is discharged through the connector 36. A hopper or a conveyor is connected to the connector 36 to transfer the organic sludge to an intermediate storage tank or a secondary drying device (not shown).

In addition, an air supply pipe 28 is installed through the second mantle 22. More specifically, the air supply pipe 28 is configured in plural and collected by the second mantle part 22, and the collecting part 35 is connected to the air supply to supply air into the drum 23.

The driving unit 24 rotates the drum 23 by contacting the outside of the drum 23. To this end, it includes a wheel 32 that rotates in contact with the surface of the drum 23 and a driving device 33 that provides a driving force to the wheel 32. One or more of these driving units 24 are installed as shown in FIGS. 4 and 5 to rotate the drum 23.

The air supply unit 28 supplies air for drying and microbial activity in the drum 23. This air supply unit 28 is connected by a single pipe connected to an air supply (not shown, for example, a blower) and a collecting unit 35, and a plurality of air supply pipes 28a, 28b by the collecting unit 35 , 28c) and installed inside the drum 23.

In particular, the air supply pipes 28a, 28b, and 28c are formed to have different lengths so that the air nozzles are provided at different portions of the drum 23. As shown, one air supply pipe supplies air to the boundary between the front (23a) and the central part (23b), the other to the center of the central part (23b), and the other to the boundary between the central part (23b) and the rear part (23c). Can be provided.

Through this, by continuously supplying air containing oxygen to the microorganisms at each location of the drum 23, it is possible to maintain the activity of the microorganism in a high state. In addition, quick drying can be achieved by lowering the humidity of each location. In addition, air passes through the bio-drying device in a direction opposite to the passage direction of the organic sludge, and is continuously discharged through the discharge pipe 31 provided on the upstream side of the bio-drying device.

In the bio-drying apparatus having the above configuration, a non-rotating sludge wall is formed in the rear part of the drum to prevent sludge accumulation. As a result, the sludge is evenly stirred and the space is kept constant, so that the filling ratio of the sludge inside the dryer rises to 50% or more.

The features, structures, effects, and the like illustrated in each of the above-described embodiments may be combined or modified for other embodiments by a person having ordinary knowledge in the field to which the embodiments belong. Accordingly, contents related to such combinations and modifications should be interpreted as being included in the scope of the present invention.

Claims (10)

A bio-drying device in which a bio-drying process is performed while supplying and discharging organic sludge and air;
A first index measuring means capable of measuring a first index including a temperature in the bio-drying process;
A second index measuring means capable of measuring a second index including the concentration of CO ₂ in the bio-drying process; And
Includes; control means for automatically controlling the supply amount of air supplied to the bio-drying device,
The control means sets input variables, adjusts the air supply amount according to the index value measured by the first index measurement unit, and then adjusts the air supply amount according to the index value measured by the second index measurement unit By continuously repeating, the air supply amount is automatically adjusted to dry the continuously supplied organic sludge and then continuously discharged.
The bio-drying apparatus includes a drum formed in the shape of a pipe that is long in one direction, and a space is provided therein, and a stirring means is provided therein so that organic sludge is introduced and fermented and dried; A mantle portion including a first mantle portion and a second mantle portion to which the drum is rotatably coupled to both ends of the drum; A driving unit that rotates the drum; And an air supply unit connected to an air supply unit and disposed inside the drum through the mantle unit to supply air into the drum,
The drum is divided into a plurality of sections including a whole into which organic sludge is injected, a rear part from which the organic sludge is discharged, and a middle part between the whole and the rear part,
On the inner surface of the drum, a spiral is installed in the entire portion, a lift blade is installed in the middle portion, and a lift blade is not installed in the rear portion, so that the movement speed becomes slower as the organic sludge proceeds from the front portion to the rear portion. An automatic control system for the amount of air supplied for drying organic sludge, characterized in that.
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