KR20130012511A - Apparatus for manufacturing bio-oil and bio-oil manufacturing process using the same - Google Patents

Abstract

PURPOSE: A bio-oil manufacturing apparatus is provided to reduce the cost of manufacturing and the size of a device utilized for a thermal cracking process to raw materials supplied to a reactor. CONSTITUTION: A bio-oil manufacturing apparatus comprises: a reactor(10) receiving bio-mass from a raw material supply part(20); a cyclone(30) processing a separation after accommodating the synthetic gas coming out from the reactor; a condenser(40) producing bio-oil by quenching for the synthetic gas processed to be separable from chua in the cyclone; and a non-condensable gas supply part(80) separating and saving the ejected non-condensable gas in the condenser. The non-condensable gas saved in the non-condensable gas supply part is able to be resupplied to the reactor. The condenser comprises multiple unit condensers and a synthetic gas pipe passing through the unit condensers. The bio-oil produced by the quenching in the condenser functions as a refrigerant for the condenser. The bio-mass is EFB(Empty Fruit Bunch). The bio-oil manufacturing apparatus comprises: a gas controller(70) connected to the non-condensable gas supply part, and receiving the non-condensable gas; a non-combustible gas supply part(50) supplying non-combustible gas to the gas controller; and a control part electrically connected to the gas controller. A pre-heater(60) supplies energy to the gas supplied from the gas controller, and increases the temperature.

Description

Apparatus for manufacturing bio-oil and bio-oil manufacturing process using the same}

The present invention relates to a bio-oil production apparatus and a bio-oil production process using the same, and more particularly, through cooling, heating, and circulating processes for by-products in a state of supplying biomass including an EFB (Empty Fruit Bunch). The present invention relates to a bio-oil manufacturing apparatus capable of maximizing the yield of bio-oil produced and a bio-oil manufacturing process using the same.

In recent years, with the renewed recognition of the superiority of biomass fuels as renewable energy, research has been resumed in various countries around the world, and technology development is being made at a rapid pace. However, since the research and development period has not been long, there are only a few commercially available technologies in the world, and even commercialized facilities are less technically competitive in the fluidized bed method, while only a few EFB-only facilities are used. In Korea, the technology using biomass is a beginner stage, preparing to enter the commercialization, and as an advanced technology that can increase the yield of bio oil, a large number of laboratory-scale researches are being conducted competitively.

Biooil is a liquid fuel similar to crude oil produced by the method of rapid pyrolysis or high temperature and high pressure hydrolysis of wood biomass. As biomass crude oil produced from wood biomass, such as petroleum fuel or crude oil for petrochemical products, can be a raw material of fuel or chemical products, new biorefinery has recently been developed. The concept of industry is being discussed. At present, technology development is in its infancy and the source technology is being accelerated in many countries around the world regarding bio oil production technology using fast pyrolysis technology.

In the process of manufacturing biooil using the rapid pyrolysis technology, woody biomass may be used in consideration of yield or cost, but there are difficulties in practical application due to resource problems.

The present invention, in order to solve the above problems, to select a material that can yield a comparable yield to wood-based biomass, and to implement a suitable process to increase the yield of bio-oil produced by the bio-oil production apparatus and using the same It is an object to provide a bio-oil manufacturing process.

In addition, the present invention to solve the above problems, by effectively supplying and maintaining the heat generated during the manufacturing of the bio-oil to reduce the size of the apparatus required for the pyrolysis operation process for the raw materials supplied to the reactor and at the same time cost The purpose is to reduce the cost.

In order to achieve the above object, it is intended to describe a bio-oil production apparatus and a bio-oil manufacturing process using the same, which can reduce the cost while increasing the yield of bio-oil by replacing the existing wood-based biomass with EFB.

In detail below, a bio-oil production apparatus according to an aspect of the present invention is provided in a reactor for receiving biomass from a raw material supply unit, a cyclone for receiving a synthesis gas discharged from the reactor and performing a separation process, in the cyclone And a non-condensing gas supply unit for separating and storing the non-condensing gas discharged from the condensation unit, and a condensation unit for producing bio-oil through quenching of the syngas that is separably treated. The non-condensable gas stored in the condensation gas supply may be re-supplied to the reactor.

The condensation unit may have a multi-stage cooling structure including a plurality of unit condensation units and a synthesis gas pipe passing through the unit condensation unit.

Bio-oil generated through the cooling in the condensation unit may preferably function as a coolant for the condensation unit.

It may be preferred that the biomass is an empty fruit bunch (EFB).

The bio-oil production apparatus is connected to the non-condensable gas supply unit, the gas control unit for receiving the non-condensable gas, the non-combustible gas supply unit for supplying the non-combustible gas to the gas control unit, and is electrically connected to the gas control unit The controller may further include a controller, and the controller may control the discharge of the non-flammable gas or the non-condensed gas stored in the gas controller.

The bio-oil production apparatus may further include a preheater to increase the temperature by supplying energy to the gas supplied from the gas control unit, the preheater may be preferably provided with thermal energy from the synthesis gas discharged from the reactor. .

Bio oil manufacturing process according to another aspect of the present invention is provided by (a) supplying the biomass from the raw material supply to the reactor, (b) the synthesis gas introduced into the cyclone from the reactor by the centrifugal separation (char) Is partially removed and the syngas is separated, (c) cooling is performed in the condensation unit to generate bio-oil, and (d) whether or not the non-condensing gas condensed in the condensation unit is reintroduced into the reactor. Determining, and (e) determining whether to continuously supply biomass from the raw material supply to the reactor.

In the bio-oil production process, the temperature in the reactor may be preferably in the range of 400 to 600 ℃.

Before the step (a), it may be preferable to further include the step of preheating the non-flammable gas stored in the non-flammable gas supply to the reactor.

The step (c) may further comprise (c1) using the cooled bio-oil as cooling oil of the condensation unit.

As described above, the bio-oil production apparatus of the present invention enables high-temperature bio-oil to be produced by rapid pyrolysis using biomass capable of generating high-calorie bio-oil such as EFB.

According to the present invention, after the bio-oil is produced, the non-condensed gas, which is a non-condensed gas, is selectively resupplied, thereby allowing the gas to be recycled and effectively utilizing waste heat.

In addition, the bio-oil production process of the present invention is positive in terms of environmental impact by being able to continuously extract the bio-oil and fuel from the synthesis gas generated in the reactor and then supply to the reactor according to the circulation treatment method.

1 is a configuration diagram of a bio-oil production apparatus according to the present invention,
2 is a detailed view of the condensation unit of FIG. 1, and
Figure 3 is a flow chart showing a time series of bio-oil production process according to the present invention.

These and other objects, features and other advantages of the present invention will become more apparent by describing in detail preferred embodiments of the present invention with reference to the accompanying drawings. The described embodiments are provided by way of example for purposes of illustration, and do not limit the technical scope of the present invention.

Bio-oil manufacturing apparatus of the present invention and each component constituting the bio-oil manufacturing process using the same may be used integrally or separately separated as needed. In addition, some components may be omitted depending on the form of use.

Hereinafter, a bio oil production apparatus and a bio oil production process using the same according to an embodiment of the present invention will be described in detail with reference to the accompanying drawings.

Explanation of Overall Configuration of Bio-Oil Production Apparatus 100

First, referring to Figure 1 looks at the overall configuration of the bio-oil manufacturing apparatus 100 according to the present invention.

The bio-oil production apparatus 100 receives the reactor 10, the raw material supply unit 20 for supplying the biomass to the reactor 10, and the high temperature and high pressure pyrolysis gas and char discharged from the reactor 10. Cyclone 30 to perform the separation process, the condensation unit 40 for producing bio-oil through the cooling (quenching) for the synthesis gas treated in the cyclone 30, the ratio of the non-condensation in the condensation unit 40 The non-condensable gas supply unit 80 for separating and storing the condensed gas, the gas control unit 70 is connected to the non-flammable gas supply unit 50 and the non-condensing gas supply unit 80, and the gas control unit 70 And a preheater 60 to energize the gas to increase the temperature. A plurality of thermometers 2 and pressure gauges 4 may be installed on the pipeline connecting the components of the bio-oil production apparatus 100 as necessary. Components constituting the bio-oil manufacturing apparatus 100 are electrically connected to the control unit and can be adjusted.

The reactor 10 is an early stage apparatus for generating bio-crude by rapidly pyrolyzing a feedstock such as biomass, and may be hollow inside to receive the biomass. The reactor 10 has a distributor 12 and a wind box 14 disposed at the bottom thereof. The reactor 10 may be formed in two stages up and down, and the distributor 12 may flow the non-combustible gas discharged from the non-combustible gas supply unit 50 at a high pressure so that the gas and char are fluidized, and a wind box ( 14 allows the preheated non-combustible gas to reach the distributor 12 in a uniform flow.

In the reactor 10, the inlet through which the biomass and the flow sand 11, hot sand is introduced, and the outlet 15 which discharges the fin 15 generated during the rapid pyrolysis of the biomass and the flow sand 11 used during the rapid pyrolysis. ) May be formed. On the other hand, the pressure sensing unit 16 for sensing the pressure in the reactor 10 and the wind box 14 and the input unit 18 electrically connected to the pressure sensing unit 16 may be additionally disposed. The char 15 generated through the pyrolysis process in the reactor 10 is formed into pellets 19 through a separate compression process and discharged through the outlet 17. The pellet 19 can be used as a renewable energy source.

The raw material supply unit 20 may include a hopper for introducing biomass, and a feeder for introducing biomass introduced through the hopper.

In the present invention, biofuel is extracted using EFB (empty fruit bunch), which is a part of palm fruit as biomass, and is highly applicable in that calorie generated during processing is higher than other biomass types.

The characteristic physicochemical properties of the EFB are as follows. The default apparent density is 125.57 (kg / m 3) and the high heating value is 3930.11 (kV / kg). Tables 1,2 and 3 below show elemental analysis, approximate analysis, and chemical composition for EFB, respectively. On the other hand, the data of Tables 1 to 3 shows an example of the experiment can be varied within a few% range.

Type of element C H N O S EFB 41.21% 5.57% 0.76% 37.67% N / D

Moisture Volatile Ash Fixed carbon 9.63% 64.95% 5.94% 19.48%

Cellulose Hemi-cellulose Lignin 59.70% 22.10% 18.20%

The cyclone 30 performs the centrifugal separation process for the gas and the steam flowing from the reactor 10 to remove the steam in the downward direction and discharge the syngas to the top.

The condensation unit 40 selectively extracts the liquid bio oil from the syngas removed from the cyclone 30 by allowing the cooling material supplied from the cooling unit 46 to circulate. The storage unit 48 stores the result.

Meanwhile, referring to FIG. 2 as a specific embodiment of the condensation unit 40, the condensation unit 40 may be configured as a cooling system composed of multiple stages. The multi-stage cooling system includes a first unit condensation unit 41, a second unit condensation unit 42, a third unit condensation unit 43, and the plurality of unit condensation units 41, 42, and 43 in order from the top. It includes a syngas pipe 45 penetrating the interior of the. Each condensation part 41, 42, 43 is provided with cooling water inlets 41a, 42a, 43a and cooling water outlets 41b, 42b, 43b. Cooling material supplied from the cooling unit 46 facilitates the production of bio-oil through heat exchange with respect to the synthesis gas flowing through the condensation units (41, 42, 43) flowing to the synthesis gas pipe (45).

Here, the condensed bio-oil may be supplied to the condensation unit 40 and utilized as cooling oil to increase the cooling efficiency.

The non-condensing gas supply unit 80 collects the non-condensing non-condensing gas while passing through the condensing unit 40 and supplies the same to be reused.

The gas control unit 70 is a place where the non-combustible gas from the non-combustible gas supply unit 50 and the non-condensable gas from the non-condensable gas supply unit 80 are mixed and stored so that the non-condensable gas can be smoothly flowed by the non-combustible gas. It is then supplied to the preheater 60. The gas control unit 70 is connected to the wind box 14 through the non-condensable gas supply line 62.

A controller (not shown) electrically connected to the gas control unit 70 controls the discharge of non-combustible gas or non-condensable gas stored in the gas control unit 70. In an embodiment, before the biomass is introduced into the reactor 10 to start pyrolysis, only the non-combustible gas is supplied to perform internal cleaning of the reactor 10, or the non-condensable gas may be smoothly transferred during the pyrolysis process. In order to do this, additional non-combustible gas may be added.

The raw material inlet control unit 24 is installed on the non-condensable gas supply line 62, and the raw material inlet control unit 24 is electrically connected to the raw material supply unit 20 through the raw material supply line 22.

The non-flammable gas supply unit 50 is preferably used to remove the unneeded gas remaining in the reactor 10 during the process in the bio-oil production apparatus 100 and to enable the smooth transfer of non-condensable gas. can do.

On the other hand, a plurality of devices may be added on the conduit between the condensation unit 40 and the non-condensing gas supply unit 80. Specifically, the wet gas meter 92, the EP 94, the micro GC 96, and the gas sampling port 98 are included. A non-condensable gas flow control unit 97 is disposed between the EP 94 and the micro GC 96, and the non-condensable gas flow control unit 97 is configured to remove a portion of the non-condensable gas discharged from the condensation unit 40. Flow to a micro GC 96 or gas sampling port 98.

Of the bio-oil manufacturing apparatus 100 Working process  Explanation

Hereinafter, an operation process of the bio-oil production apparatus 100 of the present invention will be described with reference to FIGS. 1 to 3.

First, before supplying biomass through the raw material supply unit 20, nitrogen stored in the non-combustible gas supply unit 50 is supplied to the reactor 10 by passing through the gas control unit 70 and the preheater 60 (S10). The step S10 is to increase the efficiency in the rapid pyrolysis process by removing the oxygen component remaining in the reactor 10 by performing a process for filling the reactor 10 with nitrogen.

Thereafter, the EFB is supplied through the raw material supply unit 20, thereby improving reactivity in the rapid pyrolysis process by pulverizing to a size of about 2 to 3 mm in the supply process (S20). In addition, the temperature in the reactor 10 to maintain the range of 400 to 600 ℃, preferably can be maintained at about 500 ℃.

The resultant discharged from the reactor 10 is introduced into the cyclone 30, the process is carried out by a centrifugal separation method is partially removed and the remaining syngas is discharged to the top (S30). Specifically, products such as vapor products, aerosols, and non-condensable vapor products, which are gas phase rapidly pyrolyzed in the reactor 10, are produced, and some char, which is a solid phase, is also produced. Some of the products are removed during the process in the cyclone (30).

On the other hand, in the process of proceeding the step S30, it is possible to recover the thermal energy from the result of the high temperature state discharged from the reactor 10 and to transfer it to the preheater (60). This is advantageous in terms of effectively recycling the waste heat generated in the process of operating the bio-oil production apparatus 100.

Next, cooling is performed in the condensation unit 40. The steam product is converted into a liquid oil mist and the aerosol is agglomerated to finally become bio oil (S40). The final generated biooil is collected in the bio oil storage unit 48, and in this process, the bio oil may be easily collected in an electrostatic precipitating module that may be installed in the bio oil storage unit 48 because the bio oil is a polar material. On the other hand, in the present invention by utilizing the condensed bio-oil as a cooling oil it can increase the cooling efficiency by applying with the water generally used in the cooling unit.

The synthesis gas from which the bio-oil discharged from the condensation unit 40 is extracted is introduced into the non-condensing gas supply unit 80 in the state where 촤 is removed again from the EP 94 (S50).

The non-condensed gas stored in the non-condensed gas supply unit 80 may refer to a gas in which condensation does not proceed, and most of the unnecessary components 촤 are removed and re-reacted as unreacted materials due to various circumstances in the reactor 10. It goes through the process of input.

The gas discharged from the non-condensed gas supply unit 80 undergoes a process of determining whether to re-enter the gas control unit 70 to the reactor 10 (S60). That is, the gas control unit 70 passes through the gas delivered from the non-condensable gas supply unit 80 before supplying the gas to the preheater 60 to complete the adjustment. That is, according to the processing in the reactor 10 may be supplied a non-condensed gas in which the amount of nitrogen supplied from the non-flammable gas supply unit 50 is adjusted.

In step S60, when it is determined that re-condensation of the non-condensed gas is necessary, the heated non-condensed gas that has passed through the gas control unit 70 and the preheater 60 is transferred to the reactor 10 through the non-condensed gas supply line 62. Supplied to the wind box 14 of (S70). On the other hand, in the step S60, when it is determined that the non-condensed gas re-injection is not necessary, preheating and supplying nitrogen from the non-flammable gas supply unit 50 (S72). In the case of preheating the non-condensable gas or nitrogen through the preheater 60, the preheater 60 may receive heat energy from the high temperature product discharged from the reactor 10.

Next, the control unit determines whether to continuously supply the biomass to the reactor 10 through the raw material inlet control unit 24 during the non-condensed gas is re-introduced into the reactor 10 (S80). In the step S80, when it is determined that the reaction material is insufficient in the reactor 10, since the continuous supply of biomass is required, the raw material inlet control unit 24 is appropriately opened to supply biomass (S90). If, in step S80, the reaction material is sufficient in the reactor 10, the raw material inlet control unit 24 may be temporarily closed.

Hereinafter will be described in detail data tested by the applicant in order to verify the effect of the bio-oil manufacturing process according to an embodiment of the present invention. This experiment is through a rapid pyrolysis process through a fluidized bed reactor of 300 (g / hr) class, specific experimental conditions are shown in Table 4 below.

Reactor type Fluidized bed reactor Feed amount (g) 265 Particle size (mm) 1mm or less Feeding time (min) More than 180 Feeding rate (g / min) 10.8 N2 Volume flow rate (L / min) 28 Cooling temp (℃) 8 Reactor setting temp (℃) 560 Reactor mean temp (℃) 512 Residence time (s) 2.07

Table 5 below shows the yields of bio oils, chars, and other gases produced based on the experimental conditions. As shown in Table 5, as a result of performing the process using EFB it can be seen that the excellent yield of more than 50 (wt.%).

Oil (wt.%) Char (wt.%) Gas (wt.%) 54.2 25.4 20.4

As described above, the present invention is a bio-oil production apparatus of the present invention by producing a high-purity bio-oil by rapid pyrolysis using a biomass capable of generating a high caloric value, such as EFB, after producing a bio-oil is a non-condensable gas By selectively refeeding non-condensable gas, waste heat can be effectively utilized while recycling the gas.

In addition, there can be an advantage that a relatively high HHV and viscosity can be obtained and a good yield can be obtained as compared with palm bark and pine as the main materials for producing conventional bio-oil.

While preferred embodiments of the present invention have been described above, the present invention is not limited to the above-described specific embodiments. It will be apparent to those skilled in the art that numerous modifications and variations can be made in the present invention without departing from the spirit or scope of the appended claims. And equivalents should also be considered to be within the scope of the present invention.

10: reactor
11: floating yarn
12: distributor
14: windbox
16: pressure sensing unit
18: input unit
20: raw material supply unit
24: raw material inlet control unit
30: cyclone
40: condensation unit
50: non-flammable gas supply unit
60: preheater
70: gas control unit
80: non-condensing gas supply unit
92: wet gas meter
94: EP
96: micro GC
98 gas sampling port
97: non-condensing gas flow control unit
100: bio oil manufacturing apparatus

Claims (10)

A reactor receiving biomass from a raw material supply unit;
A cyclone that receives the synthesis gas discharged from the reactor and performs a separation process;
A condenser for producing bio-oil through quenching of the syngas that is separable from the cyclone in the cyclone; And
A non-condensing gas supply unit for separating and storing the non-condensing gas discharged from the condensation unit;
Including;
Characterized in that the non-condensing gas stored in the non-condensing gas supply can be supplied to the reactor,
Bio oil manufacturing device.
The method of claim 1,
The condensation unit is characterized by consisting of a multi-stage cooling structure comprising a plurality of unit condensation unit and the syngas pipe passing through the unit condensation unit,
Bio oil manufacturing device.
The method of claim 1,
Bio oil generated through the cooling in the condensation unit, characterized in that it functions as a coolant for the condensation unit,
Bio oil manufacturing device.
The method of claim 1,
The biomass is characterized in that the EFB (empty fruit bunch),
Bio oil manufacturing device.
The method of claim 1,
The bio oil production device,
A gas control unit connected to the non-condensing gas supply unit to receive the non-condensing gas;
A non-flammable gas supply unit which supplies a non-flammable gas to the gas control unit; And
A control unit electrically connected to the gas control unit;
Further comprising:
The control unit is characterized in that for controlling the discharge of the non-combustible gas or the non-condensed gas stored in the gas control unit,
Bio oil manufacturing device.
The method of claim 5, wherein
The bio oil production device,
Further comprising: a preheater to increase the temperature by supplying energy to the gas supplied from the gas control unit,
The preheater is characterized in that for receiving thermal energy from the synthesis gas discharged from the reactor,
Bio oil manufacturing device.
(a) supplying biomass from the raw material supply to the reactor;
(b) removing some of the char from the syngas introduced into the cyclone from the reactor by centrifugal separation and separating the syngas;
(c) cooling the condensing unit to produce bio oil;
(d) determining whether to re-inject the non-condensed gas condensed in the condenser into the reactor; And
(e) determining whether to continuously supply biomass from the raw material supply to the reactor;
/ RTI >
Bio oil manufacturing process.
The method of claim 7, wherein
In the bio-oil manufacturing process,
The temperature in the reactor is characterized in that the range of 400 to 600 ℃,
Bio oil manufacturing process.
The method of claim 7, wherein
Before the step (a)
(f) preheating the non-flammable gas stored in the non-flammable gas supply unit and supplying it to the reactor;
Characterized in that it further comprises,
Bio oil manufacturing process.
The method of claim 7, wherein
The step (c)
(c1) further comprising using the cooled bio-oil as cooling oil of the condensation unit.
Bio oil manufacturing process.

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