KR102535871B1 - Experimental apparatus and method for improving production efficiency of bio-oil - Google Patents

Abstract

An experimental method and apparatus for improving the production efficiency of bio-oil are disclosed. The apparatus of the present invention includes a gas input unit including a ball flowmeter capable of adjusting the flow rate of the fluidization gas for inputting the fluidization gas from the bottom of the reactor, a solid by-product storage tank for storing solid by-products, and a solid by-product storage tank for injecting the solid by-products into the reactor. A sample inlet including a screw motor, three types of fluidized bed reactors according to the change in the shape of the dispersion plate (circular, square, rectangular), a heating element for controlling the input temperature of the fluidized gas, a temperature sensor for measuring the input temperature of the gas, A control unit including a speed controller capable of adjusting the speed of a motor for injecting solid by-products into the bubbled fluidized bed reactor, a pressure sensor for measuring pressure in real time in the bubbled fluidized bed reactor, and a storage device for storing the temperature and pressure data described above. It is possible to derive the pressure drop diagram of the bubble fluidized bed through the pressure data measured in real time while adjusting the flow rate of the fluidizing gas, and through this diagram, the minimum fluidization speed, which is the most important design factor in fluidized bed design, can be obtained.

Description

Apparatus and method for improving production efficiency of bio-oil {Experimental apparatus and method for improving production efficiency of bio-oil}

The present invention relates to an apparatus for improving the production efficiency of bio-oil, and more particularly, a fluidized bed reactor including a dispersion plate also has a circular, square, or rectangular cross section according to a change in the shape of the dispersion plate, and air is released from the bottom of the fluidized bed reactor. It relates to a bio-oil production efficiency improvement device and method that can examine the characteristics of a bubble fluidized bed reactor while changing the flow rate of a fluidizing gas and the shape of a dispersion plate with a structure in which powder or grain in the reactor is fluidized by blowing.

Powder or granular material having a small particle diameter is placed in a container such as a reactor, and gas or liquid is passed through a rectifier such as a dispersion plate at the lower end. When the flow rate is small, the particles, called a fixed bed, are in a stationary state, but when the flow rate exceeds a certain level, When this happens, the flow resistance and gravity applied to the particles become the same, so that the powder or granular material becomes a state in which it can easily flow like a boiling liquid. This phenomenon is fluidization, and the layer in this state is a fluidized bed.

In the fluidized bed, the particles in the container are mixed almost uniformly, the contact between the particles and the fluid is good, and the temperature control is easy, so that a large amount of powder or granular material can be continuously processed with a simple device and a part thereof can be taken out or supplied.

When fluidizing gas is injected into the perforated dispersion plate at the bottom of the reactor, the inert powder (typically sand) starts to flow over the dispersion plate. At this time, when the pressure drop in the reactor becomes the same as the weight of the solid per bed area, the solids start to move mutually. This state is called the minimum fluidization state, and the gas velocity at this time is called the minimum fluidization velocity.

When the flow rate is continuously increased thereafter, the pressure drop remains almost constant, but when the solid layer expands, the solids begin to behave entirely like liquids. In addition, the gas passing through the layer appears in the form of a large ball, which is called a bubble similar to the gas/liquid system, and the behavior of this bubble makes the layer a very violently boiling liquid-like shape. This phenomenon is called a bubbling fluidized bed.

Since the bubbling fluidized bed has an excellent heat transfer rate compared to the fixed bed, it is mainly used in a pyrolysis process, which is one of the methods of energizing biomass. Thermal decomposition is a thermochemical conversion process of biomass performed under anoxic conditions at a reaction temperature of 450 to 550 ° C., and the input biomass is converted into gas and char and discharged from the reactor. However, in the case of char, it accumulates as a thin layer on the sand in the fluidized bed reactor, and this layer hinders the continuous operation of the process.

The minimum fluidization speed is the most important design factor in designing the fluidized bed. Characteristics can be observed while changing the shape of the plate.

Therefore, the present invention is to provide an experimental method and apparatus for improving the production efficiency of bio-oil by identifying the above characteristics.

KR Registration Patent No. 10-0983074 (2010.09.13)

The present invention to solve these problems derives the minimum fluidization rate according to the change in the shape of the dispersion plate inside the fluidized bed and analyzes the mixing-separation phenomenon of solid by-products in the reactor to provide a device and method for improving the production efficiency of bio-oil aims to

To solve these problems, an apparatus for improving the production efficiency of bio-oil of the present invention is a fluidized bed reactor having a circular, square, or rectangular cross section including a circular, square, or rectangular dispersion plate and a fluidized gas inside the bubbled fluidized bed reactor. A fluidizing gas inlet for injecting, a solid by-product sample inlet for injecting solid by-products into the fluidized bed reactor, a pressure sensor provided on the side of the bubbled fluidized bed reactor to measure pressure in real time, and a pressure sensor measured in real time A controller that operates to receive and store the pressure in a data storage device and adjust the flow rate of the fluidizing gas through the measured pressure data to derive a pressure drop diagram of the bubbled fluidized bed, wherein the controller operates to derive a pressure drop diagram of the fluidized bed through the derived diagram. It can be achieved by configuring to obtain the minimum fluidization speed, which is a design factor.

The control unit includes a heating element for heating the stainless pipe connected to the fluidization gas inlet, a data storage device for storing temperature and pressure data, a temperature sensor for measuring the temperature of the fluidization gas introduced to the bottom of the bubble fluidized bed reactor, and a bubble fluidized bed. A speed control device for adjusting the speed of the screw motor for introducing the solid by-product into the reactor may be further included.

On the other hand, production efficiency improvement using a bio-oil production efficiency improvement device including a fluidized bed reactor having a circular, square, or rectangular cross section including a circular, square, or rectangular dispersion plate of the present invention to solve these problems. The method includes (a) introducing a fluidizing gas and a solid by-product into the fluidized bed reactor, (b) measuring the pressure in real time using a pressure sensor provided on the side of the fluidized bed reactor, (c) the above Receiving the pressure measured in real time in step (b) and adjusting the flow rate of the fluidizing gas through the measured pressure data, (d) deriving a pressure drop diagram of the bubble fluidized bed through the flow rate control in step (c) above The minimum fluidization speed, which is a fluidized bed design factor, can be obtained through the diagram derived in step (d), including

Therefore, according to the bio-oil production efficiency improvement device and method of the present invention, the pressure drop in the bubbled fluidized bed is reduced through pressure data measured in real time while controlling the flow rate of the fluidizing gas introduced through the ball flowmeter at the bottom of the fluidized bed reactor. It is possible to derive a diagram, and through this diagram, the minimum fluidization speed, which is the most important design factor for fluidized bed design, can be obtained.

In addition, according to the bio-oil production efficiency improvement device and method of the present invention, it is possible to derive a mixing index for analyzing the mixing-separation phenomenon of inert granular material and by-products in the reactor by introducing solid by-products.

1 is a main configuration diagram of an apparatus for performing an experiment to improve the production efficiency of bio-oil;
2 is a view showing the shape of a dispersion plate having a circular, square, or rectangular shape;
3 is a view showing a bubbling fluidized bed reactor having a circular, square, or rectangular cross section;
Figure 4 is a flow chart for explaining the method for improving the production efficiency of bio-oil of the present invention;
5 is a reference diagram for explaining a method for obtaining the minimum fluidization speed of the present invention;
6 is an exemplary graph of the derived Mixing Index.

The terms or words used in this specification and claims are not limited to the usual or dictionary meanings, and the inventor can properly define the concept of the term in order to explain his or her invention in the best way. Based on this, it should be interpreted as a meaning and concept consistent with the technical spirit of the present invention.

Throughout the specification, when a certain component is said to "include", it means that it may further include other components without excluding other components unless otherwise stated. In addition, terms such as “… unit”, “… unit”, “module”, and “device” described in the specification mean a unit that processes at least one function or operation, which is implemented as a combination of hardware and/or software. It can be.

Throughout the specification, the term "and/or" should be understood to include all possible combinations from one or more related items. For example, the meaning of “a first item, a second item and/or a third item” may be presented from two or more of the first, second or third item as well as the first, second or third item. A combination of all possible items.

Throughout the specification, identification codes (e.g., a, b, c, ...) for each step are used for convenience of explanation, and the identification code does not limit the order of each step, and each step Unless the specific order is clearly stated in context, it may occur in a different order from the specified order. That is, each step may occur in the same order as specified, may be performed substantially simultaneously, or may be performed in the reverse order.

Hereinafter, an embodiment of the present invention will be described with reference to the drawings.

1 is a main configuration diagram of an apparatus for performing an experiment to improve the production efficiency of bio-oil according to an embodiment of the present invention, and FIG. 2 is a dispersion plate having a circular, square, or rectangular shape according to an embodiment of the present invention. It is a picture showing the appearance of 3 is a diagram showing the appearance of a fluidized bed reactor having a circular, square, or rectangular cross section according to an embodiment of the present invention.

As shown in FIG. 1, the apparatus for performing experiments to improve the production efficiency of bio-oil of the present invention includes a fluidizing gas input unit 100 at the bottom of the reactor, a solid by-product sample input unit 200, a bubble fluidized bed reactor ( 300) and a control unit 400.

The fluidization gas input unit 100 is a module for injecting the fluidization gas into the fluidized bed reactor 300 . The fluidizing gas is connected to a device such as an air compressor (not shown) via a stainless pipe and is injected into the lower portion of the bubbled fluidized bed reactor 300. The gas is injected through the ball flowmeter 110 attached to the bottom of the fluidized bed reactor 300, and the heating element 410 controlled by the controller 400 uses a stainless pipe to keep the temperature of the injected gas constant. ) and a temperature sensor 430 for measuring the input temperature of the gas and transmitting the measured temperature to the data storage device 420 of the control unit 400 is attached.

The solid by-product sample input unit 200 is a module composed of a screw motor 220 for injecting solid by-products from the solid by-product storage tank 210 into the fluidized bed reactor 300 . The speed of the screw motor 220 is controlled by the speed control device 440 included in the controller 400.

The fluidized bed reactor 300 has various cross-sectional shapes, and on the side of the fluidized bed reactor 300, a pressure sensor 320 measures pressure in real time and transmits data to the data storage device 420 of the controller 400. is attached.

Referring to the drawing showing the appearance of the dispersion plate having a circular, square, and rectangular shape in FIG. 2 and the drawing showing a fluidized bed reactor having a circular, square, and rectangular cross section in FIG. It can be seen that is composed of various cross-sectional shapes.

Referring to the drawing, as shown in FIG. 3 according to the change in the circular, square, or rectangular shape of the distribution plate 310 inside the reactor of FIG. 2, it may have a shape having a circular, square, or rectangular cross section.

The control unit 400 includes the stainless tube heating element 410, a data storage device 420 for storing temperature and pressure data, and a temperature sensor 430 for measuring the temperature of the fluidized gas injected from the bottom of the bubble fluidized bed reactor 300. ), a speed controller 440 for controlling the speed of the screw motor 220 for introducing solid by-products into the fluidized bed reactor 300, a pressure attached to the side of the fluidized bed reactor 300 to measure the pressure inside the reactor A sensor 450 is included.

According to the above-described experimental method and device for improving the production efficiency of bio-oil, it is possible to derive a pressure drop diagram of a fluidized bed through pressure data measured in real time while adjusting the flow rate of the fluidizing gas, and this diagram Through this, the minimum fluidization speed, which is the most important design factor for fluidized bed design, can be obtained.

In addition, a mixing index can be derived to analyze the mixing-separation phenomenon of inert powder and granular material and by-products in the reactor by introducing solid by-products.

The production efficiency improvement method of the present invention using the above-described device will be described.

Figure 4 is a flowchart for explaining the production efficiency method of the present invention. As shown, first, using a bubbling fluidized bed reactor having a circular, square, or rectangular cross section including a circular, square, or rectangular dispersion plate A step of introducing a fluidizing gas and a solid by-product into the fluidized bed reactor is performed (S100).

When the fluidization gas and the solid by-product are introduced into the fluidized bed reactor in step S100, the pressure is measured in real time using a pressure sensor provided on the side of the fluidized bed reactor (S200).

The control unit receiving the pressure measured in real time in step S200 performs a step of adjusting the flow rate of the fluidizing gas through the measured pressure data (S300).

The step (S400) of deriving the pressure drop diagram of the bubble fluidized bed through the control of the flow rate in step S300 is performed to obtain the minimum fluidization rate, which is a fluidized bed design factor, through the derived diagram.

Referring to the drawing for explaining the method for obtaining the minimum fluidization velocity of the present invention of FIG. 5, a pressure drop diagram of the fluidized bed according to the shape of the fluidized bed reactor and the superficial gas velocity change is shown.

The minimum fluidization velocity, which is the most important design factor for fluidized bed design, was obtained, and the stable flow region and the choking region leading to fast fluidization were obtained. Observation of the flow phenomenon according to the change in superficial velocity shows that when the superficial velocity is very small, gas passes between the solid particles to form a stagnant solid particle layer. At this time, the pressure drop increases until it becomes equal to the weight of the solid particle layer , no appreciable movement of the particle layer is seen.

This region is called a fixed bed, and the flow rate at which the fluid does not pass through the packed bed is determined. It is confirmed that this fixed bed area continues to a certain point, shows a maximum pressure drop, and then rapidly decreases. After that, if the superficial velocity is further increased at a constant speed, the solid particles float little by little and the pressure drop decreases and a transition phenomenon occurs. . The superficial velocity at this time is called the minimum fluidization velocity, and the red line in the figure represents the minimum fluidization velocity condition derived for each shape.

Referring to the drawing, it can be confirmed that there is no significant difference according to the change in the shape of the dispersion plate and the shape of the column through the pressure drop diagram according to the change in superficial velocity for each shape derived. It can be seen that the pressure drop in the fixed bed region increases until it becomes equal to the weight of the solid particle layer, and the decrease in pressure drop when entering the bubble flow region does not show much difference according to the shape change.

Hereinafter, a specific method for deriving a mixing index for analyzing the mixing-separation characteristics of solid by-products in the fluidized bed and the minimum fluidization speed at which the characteristics can be observed while changing the flow rate of the injected fluidization gas and the shape of the dispersion plate will be described. .

It is calculated using Kramer's Mixing Index derivation formula in Equation 1.

[Equation 1]

In Equation 1, X _i represents the mass fraction of char in each sampling cell, and σ ₀ ² is the standard deviation of the mass fraction of the solid byproduct when the inert granular material (sand) and the solid byproduct (char) are completely separated. am. σ _r ² is the standard deviation of the mass fraction of the solid by-product when the inert granular material and the solid by-product are completely mixed. M = 1 represents complete mixing and M = 0 represents complete separation.

에서는 유동층 고체 입자와 char가 서로 분리되지 않고 혼합된 상태를 유지하며, 이후 공탑속도가 증가할수록 유동층 고체 입자와 char는 기포 유동과 밀도차에 의해 분리되며 mixing index는 감소한다. Mixing index는 세 유동층 반응기 형상 모두

에 최소로 나타나며, 이는 모래와 char가 최대로 분리된 상태를 의미한다. 이후

를 기점으로 공탑속도가 증가할수록 모래와 char는 서로 혼합되며 mixing index는 증가한다. 유동층 column 형상에 의한 두 고체 혼합물의 mixing index는 U/Umf=1.14 이하에서는 원형 형상이 최소로 나타나고, U/Umf=1.14 이상에서는 직사각 형상이 최소로 나타난다.The air velocity in the fluidized bed reactor was dimensionless by dividing the superficial velocity by the minimum fluidization velocity. tower speed

In , the fluidized bed solid particles and char do not separate from each other and remain mixed. As the superficial velocity increases, the fluidized bed solid particles and char are separated by bubble flow and density difference, and the mixing index decreases. Mixing indices for all three fluidized bed reactor geometries

, which means that sand and char are separated to the maximum. after

As the superficial velocity increases from , sand and char are mixed together and the mixing index increases. The mixing index of the two solid mixtures by the fluidized bed column shape has a circular shape at a minimum when U/Umf = 1.14 or less, and a rectangular shape at a minimum when U/Umf = 1.14 or higher.

The Mixing index derived through the above process is illustrated in FIG. 6 .

As can be seen in the Mixing index graph of FIG. 6, when the superficial speed is greater than the minimum fluidization speed, it was confirmed that the mixing degree of inert granular material and solid by-products was the lowest in the rectangular shape, which is an essential condition for increasing bio-oil production efficiency. It is considered that the rectangular shape is most advantageous for the application of the solid by-product separation device for continuous process design. Therefore, it is judged that it is desirable to consider a rectangular shape for the shape of the rapid pyrolysis hot-bed device for future bio-oil production.

According to the bio-oil production efficiency improvement device and method of the present invention described above, while controlling the flow rate of the fluidizing gas introduced through the ball flowmeter at the bottom of the fluidized bed reactor, the pressure drop in the bubbled fluidized bed is reduced through pressure data measured in real time. It is possible to derive a diagram, and through this diagram, the minimum fluidization speed, which is the most important design factor for fluidized bed design, can be obtained.

In addition, according to the bio-oil production efficiency improvement device and method of the present invention, it is possible to derive a mixing index for analyzing the mixing-separation phenomenon of inert powder or granular material and by-products in the reactor by introducing solid by-products.

Although the present invention has been described in detail with respect to the specific embodiments described above, it is obvious to those skilled in the art that various changes and modifications are possible within the scope of the technical idea of the present invention, and it is natural that these changes and modifications fall within the scope of the appended claims.

100: fluidization gas input unit 200: solid by-product sample input unit
300: fluidized bed reactor 400: control unit

Claims (11)

A bubbling fluidized bed reactor comprising a rectangular dispersion plate, having a pressure sensor for measuring pressure in real time and transmitting data to a side thereof, and having a rectangular cross section;
a fluidization gas input unit for injecting fluidization gas into the bubble fluidized bed reactor;
a solid by-product sample inlet unit for injecting solid by-products into the fluidized bed reactor;
A control unit that receives the pressure measured by the pressure sensor in real time, stores it in a data storage device, and at the same time adjusts the flow rate of the fluidizing gas through the measured pressure data to derive a pressure drop diagram of the bubbled fluidized bed;
a heating element for heating the stainless pipe connected to the fluidization gas inlet;
a data storage device for storing temperature and pressure data;
A temperature sensor for measuring the temperature of the fluidizing gas introduced to the bottom of the bubble fluidized bed reactor; And
a speed control device for adjusting the speed of a screw motor for injecting solid by-products into the fluidized bed reactor;
including,
The control unit
Using the pressure drop diagram of the fluidized bed according to the shape of the fluidized bed reactor and the superficial gas velocity, the minimum fluidization velocity, which is a fluidized bed design factor, is obtained,
The fluidizing gas input unit
It is connected through a stainless pipe to inject fluidized gas into the bottom of the bubbled fluidized bed reactor, and the gas is injected through a ball flowmeter attached to the bottom of the bubbled fluidized bed reactor. In order to keep the temperature of the injected gas constant The bio-oil production efficiency improvement device, characterized in that the stainless pipe is attached with a temperature sensor for measuring the input temperature of the heating body and gas adjusted by the control unit and transmitting the measured temperature to the data storage device of the control unit.
delete delete delete The method of claim 1,
The minimum fluidization rate is
Determine the flow rate of the fixed bed where the fluid does not pass through the packed bed, and increase the superficial velocity at a constant rate at the point where the pressure drop rapidly decreases after the area of the fixed bed shows the maximum pressure drop, thereby reducing the pressure drop in which solid particles float. and a bio-oil production efficiency improvement device determined by the superficial speed when the transition occurs. delete delete delete delete delete delete

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