WO2020136824A1

WO2020136824A1 - Treatment device for palm oil mill residue, and treatment method therefor

Info

Publication number: WO2020136824A1
Application number: PCT/JP2018/048231
Authority: WO
Inventors: 眞一下瀬
Original assignee: 株式会社下瀬微生物研究所
Priority date: 2018-12-27
Filing date: 2018-12-27
Publication date: 2020-07-02
Also published as: WO2020137003A1

Abstract

This treatment device for palm oil mill residue is provided with: a reduced-pressure fermentation dryer 3 in which palm oil mill residue is accommodated in a closed container 30 and stirred while being heated to a predetermined temperature range under decompression, and in which microbes are used to break down organic components of the organic matter to obtain a reduced-volume dried product; and a heat source apparatus 7 for combusting the dried product obtained at the reduced-pressure fermentation dryer 3 to generate a heat source. As such, fermentation of the organic matter contained in the palm oil mill residue can be accelerated, and further, the dried product thereof can used as fuel.

Description

Palm oil factory residue treatment apparatus and method thereof

The present invention relates to a treatment device for a residue produced in a palm oil factory and a treatment method thereof.

Conventionally, in a palm oil factory that produces palm oil from the fruits of palm palm, in the oil production process, empty fruit clusters, mesocarp fibers, palm palm shells, and sludge due to centrifugal separation in the oil production process are used. And sludge occur. In the case of empty fruit bunches and palm palm shells, these residues are dried and then incinerated, and for mesocarp fibers, they are composted and reused as fertilizers and animal feed, and in sludge and sludge. After purification treatment, it is discharged into rivers.

However, incinerating or purifying a large amount of residue has a problem in terms of processing cost. In addition, empty fruit bunch and mesocarp fiber had an environmental problem because they started to crumble when they were piled up in large amounts as compost, and they also had a bad odor.

The applicant of the present application efficiently stores organic waste in a closed container such as a tank and stirs it while heating it to a predetermined temperature range under reduced pressure, as described in Patent Document 1, for example. A patent application has been filed for a reduced pressure fermentation dryer capable of promoting the fermentation of organic substances by removing water and drying, and adding predetermined microorganisms to the organic waste treated in this way.

JP, 2007-319738, A Japanese Patent No. 4153685

The present invention has been made in consideration of the above-mentioned circumstances, and an object thereof is to effectively decompose organic matter contained in a residue produced in a palm oil factory with microorganisms to promote fermentation. Another object of the present invention is to provide a processing apparatus and a processing method for using the dried material as fuel.

The present invention has the following means for solving the above-mentioned problems. That is, the present invention stores the residue generated in the palm oil factory in a closed container and stirs it under reduced pressure while heating it to a predetermined temperature range, and decomposes and reduces organic components of organic matter by utilizing microorganisms. It is characterized by comprising a vacuum fermentation dryer for obtaining a dried product contained therein, and a heat source device which is arranged at a subsequent stage of the vacuum fermentation dryer and which burns the dried product to generate a heat source.

According to the present invention, since the palm oil factory residue can be effectively fermented and reduced in volume by the vacuum fermentation dryer, the processing cost of the palm oil factory residue can be significantly reduced. In addition, since it is possible to generate a heat source with a heat source device by using the dried product obtained by the reduced pressure fermentation dryer as a fuel, it is possible to effectively reduce the amount of waste generated by effectively utilizing the dried product, while reducing the amount of steam and the like. It is possible to generate a heat source.

In the present invention, it is preferable that the palm oil factory residue contains at least one of empty fruit bunch, mesocarp fiber and palm palm shell. Furthermore, the palm oil factory residue preferably contains sludge and sludge in addition to the empty fruit bunch and the like. According to this configuration, the vacuum fruit fermentation dryer can be used to reliably ferment empty fruit bunches, mesocarp fibers or palm palm shells, and all of the palm oil factory residue (empty bunches, mesocarp fibers). , Palm palm shells and sludge and sludge) are treated with a vacuum fermentation dryer, which has the advantage of producing almost no waste.

In the present invention, a part of the heat source generated by the heat source device is preferably used at least in the reduced pressure fermentation dryer. According to this configuration, for example, a dedicated steam boiler or the like provided in the vacuum fermentation dryer is not required, the facility configuration is simple, and running costs can be suppressed.

In the present invention, it is preferable to include a generator that is connected to the heat source device and receives a part of the generated heat source to generate electricity. With this configuration, it is possible to convert the generated heat source into electricity.

In the present invention, the electricity obtained by the generator is preferably used in the reduced pressure fermentation dryer. According to this configuration, a part of the electric power consumed by the reduced pressure fermentation dryer can be covered by the power generation of the generator, and the running cost can be suppressed.

Further, the present invention stores the residue produced in the palm oil factory in a closed container and stirs it under reduced pressure while heating it to a predetermined temperature range, and decomposes and reduces organic components of organic matter by utilizing microorganisms. A reduced pressure fermentation drying step for obtaining a dried product contained, and a heat source generation step for burning the dried product obtained in the reduced pressure fermentation drying step to generate a heat source, and a palm oil factory residue Since it is a treatment method, the same effect as that of the treatment device for the palm oil plant residue can be expected.

According to the palm oil factory residue treatment apparatus and the method for treating the same according to the present invention, it is possible to significantly reduce the processing cost of the palm oil factory residue. Further, by effectively utilizing the dried product discharged from the reduced pressure fermentation dryer, it is possible to generate a heat source with almost no waste generated.

FIG. 1 is a diagram schematically showing an oil production process in a palm oil factory and a palm oil factory residue treatment system according to an embodiment of the present invention. FIG. 2 is a diagram schematically showing a schematic configuration of a reduced pressure fermentation dryer provided in the processing system. FIG. 3: is a figure which shows schematic structure of the biomass boiler with which the same processing apparatus is equipped.

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

FIG. 1 is a diagram schematically showing an oil production process in a palm oil factory and a palm oil factory residue treatment system according to an embodiment of the present invention.

In FIG. 1, A is an oil refining process of palm oil in the palm oil factory, and a palm oil factory residue B is generated as a waste by this oil refining process. C is the palm oil residue treatment system of the present embodiment for treating the palm oil factory residue B.

First, palm oil refining process A will be described. In this oil refining step A, palm palm fruits (FFB: Fresh Fruit Bunch) are harvested in step 90, and in step 91, the harvested palm palm fruits are steamed and then defruited by a stripper to remove fruit 92 and empty fruit. It separates into a fruit bunch (EFB: Empty Fruit Bunch) 93. Empty fruit bunch EFB93 becomes the palm oil factory residue B.

In step 94, the separated fruit 92 is squeezed by a squeezing machine to obtain juice, and crude oil 95, that is, crude palm oil is extracted from this juice. By the pressing process in the step 94, the pressing residue 96 is separated from the fruit 92.

In step 97, the extracted crude palm oil is refined (refined) by a refiner including a centrifuge, a vacuum dryer, etc. to become palm oil (CPO: Crude Palm Oil) 98. By the centrifugal separation process in the step 97, sludge (POME: Palm Oil Mill Effluent) 99 as a waste oil of the palm oil refinery process is separated from the crude palm oil to be a palm oil factory residue B. The refined palm oil (CPO) 98 is a raw material for detergents such as soap and cosmetics.

The pressing residue 96 separated in the step 96 is passed through the wind separation tube in step 100, and is separated into seeds (seed or endosperm) and mesocarp fiber in step 101, and seeds 102 are The mesocarp fiber (MF) 103 is separated from the mesocarp fiber (MF) 103, and the mesocarp fiber (MF) 103 is a palm oil factory residue B.

On the other hand, in step 104, the separated seeds are dried and then coarsely crushed using a coarse crusher to be separated into a core 105 and a palm kernel shell (PKS) 106. Palm palm shell PKS is Palm Oil Factory Residue B.

The separated core 105 is subjected to an oil extraction process in step 107 to extract palm kernel oil 108, and a residue (squeezed residue) 106 other than the palm kernel oil 108 becomes a palm oil factory residue B. The extracted palm kernel oil 108 is used for food, or for frying oil, spray oil, or the like.
Here, in a palm oil plant, when the palm FUB fruit FFB harvested at the time of producing palm oil CPO and palm kernel oil is, for example, 1000 tons per day, the resulting plant residue B per day is the empty fruit cluster EFB. 240 tons, mesocarp fiber MF 130 tons, palm palm shell PKS etc. (palm palm shell and core squeeze residue) 70 tons, sludge and sludge POME 700 tons, and residue B as a whole 1140 tons. The amount of palm FFB fruit FFB harvested and the amount of factory residue B such as empty fruit bunch EFB generated are examples and are not particularly limited.

The residue B generated in the palm oil factory, that is, empty fruit bunch EFB, mesocarp fiber MF, palm palm shell PKS, etc., and sludge and sludge POME are all objects to be treated in the palm oil residue treatment system C. Becomes Specifically, all of the residue B produced in the palm oil factory is introduced into the inlet 30a (see FIG. 2) of the reduced pressure fermentation dryer 3.

The reduced-pressure fermentation dryer 3 is a known one as described in, for example, Patent Document 1 and the like, while stirring the residue B to be treated under reduced pressure while heating it to a predetermined temperature range, and utilizing microorganisms. Then, the organic component of the residue B is decomposed to obtain a dried product having a reduced volume.

The reduced-pressure fermentation dryer 3 is, as schematically shown in FIG. 2, a substantially cylindrical shape that is hermetically formed so as to keep the inside at atmospheric pressure or below, as a closed container for containing the introduced factory residue B. A tank (pressure resistant tank) 30 is provided. A heating jacket 31 is provided on the peripheral wall of the tank 30, and heating steam is supplied from the biomass boiler 7 to the heating jacket 31. The temperature of the steam supplied from the biomass boiler 7 is preferably about 140°C, for example.

Also, a stirring shaft 32 extending in the longitudinal direction (left and right direction in FIG. 2) is provided inside the tank 30 so as to be surrounded by the heating jacket 31. The stirring shaft 32 is rotated at a predetermined rotation speed by the electric motor 32a. The agitation shaft 32 is provided with a plurality of agitation plates 32b spaced apart from each other in the axial direction. The agitation plates 32b agitate the factory residue B and perform fermentation drying treatment from the factory residue B. The dried product is sent in the longitudinal direction of the tank 30.

An input port 30a for the residue B generated in the palm oil factory is provided on the upper side of the longitudinal side of the tank 30, and the residue B input from the input port 30a is heated by the heating jacket 31. Meanwhile, the stirring shaft 32 is rotated to stir. Then, after a lapse of a predetermined time, the processed dried product is discharged from a discharge port 30b provided in the lower portion of the tank 30. A hydraulic motor may be used instead of the electric motor 32a.

A guide part 30c for guiding the vapor generated from the heated residue B to the condensing part 33 is provided on the upper part of the tank 30. In the present embodiment, two guide portions 30c are provided, and each guide portion 30c is arranged at a predetermined distance in the longitudinal direction of the tank 30. A plurality of cooling pipes 33b supported by a pair of heads 33a are provided inside the condensing part 33 supported by the communication passage 34 via the guide part 30c. The cooling pipes 33b and the cooling tower 33b are provided. A cooling water passage 80 is provided between the cooling water passage 80 and the cooling water passage 8. In the present embodiment, the condensing part 33 extends parallel to the longitudinal direction of the tank 30 and is arranged on the rear side of the guide part 30c.

Then, the cooling water that has flowed through the cooling pipe 33b in the condensing unit 33 and has increased in temperature due to heat exchange with the high-temperature steam flows through the cooling water passage 80 as schematically indicated by an arrow in FIG. 8 into the water receiving tank 81. The cooling tower 8 is provided with a pump 82 for pumping the cooling water from the water receiving tank 81 and a nozzle 83 for injecting the pumped cooling water. The cooling water jetted from the nozzle 83 receives the air blown from the fan 85 while flowing down the lower part 84, the temperature of the cooling water decreases, and the cooling water flows into the water receiving tank 81 again.

The cooling water cooled by the cooling tower 8 is sent by the cooling water pump 86, sent to the condensing unit 33 by the cooling water path 80, and flows through the plurality of cooling pipes 33b again. Then, after the temperature rises due to the heat exchange with the steam generated inside the tank 30 as described above, it flows through the cooling water path 80 again and flows into the water receiving tank 81 of the cooling tower 8. That is, the cooling water circulates in the cooling water passage 80 between the condenser 33 and the cooling tower 8.

In addition to the cooling water that circulates as described above, in the cooling tower 8, condensed water obtained by condensing the steam generated from the heated residue B in the condensing unit 33 is also injected. Although not shown, condensed water generated by exchanging heat with high-temperature steam is collected below the condenser 33.

Further, a vacuum pump 36 is connected to the condensing unit 33 via a communication passage 35 to reduce the pressure in the tank 30. That is, by the operation of the vacuum pump 36, the air and the condensed water are sucked out from the condenser 33 through the communication passage 35, and the air and the steam in the tank 30 are further sucked through the communication passage 34 and the guide portion 30c. .. In this way, the condensed water is sucked from the condenser 33 to the vacuum pump 36, and is guided from the vacuum pump 36 to the water receiving tank 81 of the cooling tower 8 by the water guiding pipe. An open/close valve 30d is provided in the communication passage 34 so that air or the like is not sucked from the inside thereof when the reduced pressure fermentation dryer 3 is stopped. Although not shown, an atmosphere opening valve that opens the inside of the tank 30 to the atmosphere is arranged near the vacuum pump 36.

In this way, the condensed water guided to the water receiving tank 81 of the cooling tower 8 mixes with the cooling water, is pumped up by the pumping pump 82 as described above, is jetted from the nozzle 83, and is then cooled while flowing down the lower stream portion 84. .. The condensed water contains the same microorganisms as those added to the residue B in the tank 30, and the odorous components contained in the condensed water are decomposed. It does not diverge into.

Explaining the operation of the reduced pressure fermentation dryer 3 having the above structure, the residue B contained in the tank 30 is stirred by the rotation of the stirring shaft 32 while being heated by the heating steam supplied to the heating jacket 31. It Then, the residue B contained in the tank 30 is effectively heated by being heated from the outside by the heating jacket 31 surrounding the inside of the tank 30 and being heated from the inside by the stirring shaft 32 and the like. The residue B is stirred by the stirring shaft 32. In addition, since the pressure is reduced by the operation of the vacuum pump 36, the boiling point is lowered in the tank 30, the evaporation of water is accelerated, and the water is evaporated in a temperature range in which the decomposition of the organic component of the residue B is promoted by the microorganisms. To do.

In the vacuum fermentation and drying process using the vacuum fermentation dryer 3, one step (1 cycle) is preferably, for example, 24 hours. First, the residue B is charged over 30 minutes and the residue B is removed over 23 hours. At the same time as the fermentation step of decomposing the organic component, a drying step of drying the residue B is provided, and the dried material (water content of about 10%) is discharged over 30 minutes. Meanwhile, if the pressure inside the tank 30 is reduced to -0.06 to -0.07 MPa (gauge pressure; hereinafter, gauge pressure is omitted), the water temperature in the tank 30 is maintained at 76 to 69°C (saturated steam temperature). It As a result, fermentation, decomposition and drying of the residue B are promoted by the microorganisms described below. Then, as a microorganism to be added to the residue B in the tank 30 when performing such a drying treatment, as described in, for example, Patent Document 2, a plurality of types of indigenous bacteria are used as a base, and Cultured complex effective microorganism groups are preferred, and the common name is SHIMOSE 1/2/3 group, which is the center of the colony.

SHIMOSE 1 was sent to FERM BP-7504 (Ministry of Economy, Trade and Industry, National Institute of Advanced Industrial Science and Technology, Institute of Biotechnology and Industrial Technology, Patent Microorganism Depositary Center (1-3, East 1-3, Tsukuba, Ibaraki, Japan) on March 14, 2003. Internationally deposited). SHIMOSE 2 is a microorganism belonging to FERM BP-7505 (an international deposit similar to SHIMOSE 1) and Pichiafarinosa, which is resistant to salt, and SHIMOSE 3 is called FERM BP-7506 (SHIMOSE 1). It is a microorganism belonging to Staphylococcus).

Here, the procedure of the vacuum fermentation drying process of organic substances by the vacuum fermentation dryer 3 will be described. First, the residue B (empty fruit bunch EFB, mesocarp fiber MF, palm palm shell PKS, etc., and sludge and sludge POME) is charged into the charging port 30 a of the tank 30 of the reduced pressure fermentation dryer 3. Then, the inside of the tank 30 is closed under atmospheric pressure.

After that, after adding a predetermined microorganism to the residue B in the tank 30, the atmosphere opening valve provided near the vacuum pump 36 is closed to close the inside of the tank 30. Then, the inside of the tank 30 is heated under reduced pressure, and the organic component of the residue B contained therein is fermented and dried. That is, heating steam is supplied from the biomass boiler 7 to be described later to heat the inside of the tank 30.

Then, the inside of the tank 30 is heated by the heating steam, the stirring shaft 32 is rotated at a predetermined rotation speed (for example, about 8 rpm), and the inside of the tank 30 is depressurized by the operation of the vacuum pump 36. As a result, the temperature in the tank 30 becomes an environment in which the activity of the microorganisms is optimal, and the decomposition of organic components of organic substances by the microorganisms is suitably promoted. The rotation speed (8 rpm) of the stirring shaft 32 is an example, and may be another value as long as the organic component of the organic matter can be decomposed.

In this way, while maintaining the temperature and pressure in the tank 30, when the predetermined time has elapsed, the supply of heating steam from the vacuum pump 36 and the biomass boiler 7 is stopped, and the atmosphere opening valve is opened to a large level. Set to atmospheric pressure. On the other hand, the stirring shaft 32 is rotated in the reverse direction, the lid of the discharge port 30b of the tank 30 is opened, and the dried material having a predetermined water content (for example, about 10%) is discharged from the tank 30. At this time, the dry matter discharged from the tank 30 is reduced in volume.

As described above, the dried product after the reduced pressure fermentation drying process by the reduced pressure fermentation dryer 3 is discharged from the discharge port 30b at the bottom of the tank 30 of the reduced pressure fermentation dryer 3. The dry matter having a predetermined water content (for example, about 10%) discharged from the discharge port 30b is about 1140 tons per day of the total amount of the factory residue B input to the vacuum fermentation dryer 3 per day. It is 280 tons. The amount of the obtained dried product is an example, and the entire amount of the factory residue B fed into the vacuum fermentation dryer 3 per day is defined as a dried product having a predetermined water content (for example, about 10%). The number of installed bases of the reduced pressure fermentation dryer 3 may be appropriately selected so as to ensure discharge.

As shown in FIG. 1, the dried product obtained by the reduced pressure fermentation dryer 3 is separated by a separator 39 into a suitable product suitable for the fuel used in the biomass boiler 7 and an unsuitable product other than the suitable one. It This compatible product is a small particle of a predetermined size or less among the obtained dried products, and since the small particle is fermented to homogenize the particle size, particle shape and components, The thermal energy generated during combustion is stable. Therefore, the small particles are supplied to the biomass boiler 7 as the biomass fuel 40. On the other hand, unsuitable materials (large particles exceeding a predetermined size) are re-introduced into the vacuum fermentation dryer 3 to further accelerate the fermentation, molded into small particles, and discharged again from the discharge port 30b, or fertilizer. And used as animal feed. In particular, when it is used as a fertilizer, this fertilizer contains a large amount of potassium (K) and is treated locally as a high-quality fertilizer.

Most of the water contained in this residue B (water other than the water contained in the obtained dried product) of the factory residue B fed into the reduced pressure fermentation dryer 3 is as shown in FIG. Evaporates in the tank 30 of the reduced pressure fermentation dryer 3, and the amount of waste water is completely eliminated. The evaporated water content is, for example, 970 tons with respect to the total amount of the factory residue B (1140 tons) per day that is input. The amount of evaporated water is also an example.

The biomass boiler 7 burns small particles in the dried material having a predetermined water content (about 10%) obtained by the vacuum fermentation dryer 3 to generate high temperature steam. Therefore, in this biomass boiler 7, a small-sized material in the dried material obtained in the reduced pressure fermentation drying step by the reduced pressure fermentation dryer 3 is burned as a biomass fuel to perform a heat source generation step of generating steam (heat source).

-Biomass boiler-
As schematically shown in FIG. 3, the biomass boiler 7 includes a biomass burner 71 capable of efficiently burning dry matter (small particles) and a heat medium such as water, which is heated by combustion heat of the biomass burner 71. And a steam generator 72 for generating steam. The heating steam generated in the steam generator 72 is supplied to the reduced pressure fermentation dryer 3 (the heating jacket 31 of the tank 30 and the like).

As an example, the biomass burner 71 uses, as fuel, a hopper 73 into which small particles of the dried material obtained by the reduced pressure fermentation dryer 3 are put, and a dried material (small particles) dropped from the hopper 73. A screw feeder 74 which is driven by an electric motor 74a, a primary combustion furnace 75 which thermally decomposes the small particles thus sent to generate a combustible gas, and a secondary combustion furnace which completely burns the combustible gas. And 76.

The screw feeder 74 is housed in a cylindrical chamber 74b, and a hopper 73 is connected above the rear end side (right side in FIG. 3). A rotary valve 73a is provided below the hopper 73. On the other hand, the front end portion (the left end portion in FIG. 3) of the screw feeder 74 faces the opening at the upstream end (the right end in FIG. 3) of the cylindrical primary combustion furnace 75 so that the small particles and the like are supplied thereto. Has become.

Further, an electric heating type ignition plug 75a is provided facing the opening at the upstream end of the primary combustion furnace 75 so that the small particles in the primary combustion furnace 75 are ignited when the operation of the biomass burner 71 is started. It has become. Small particles are supplied to the primary combustion furnace 75 from the screw feeder 74, and the air pushed by the fan 77 flows into the chamber 74b to combust the small particles.

Then, in addition to the air flowing in from the opening at the upstream end, the air also flows into the primary combustion furnace 75 through the plurality of holes provided in the peripheral wall thereof, but the amount of these air is small. Since the amount of the substance becomes insufficient with respect to the amount of the substance, in the primary combustion furnace 75, a part of the small grain is burned, while the rest is thermally decomposed at a high temperature to generate a combustible gas. The combustible gas thus generated combusts and flows out toward the secondary combustion furnace 76 on the downstream side.

That is, at the downstream end of the primary combustion furnace 75 (the left end in FIG. 3), a tapered nozzle portion 75b is provided so as to project into the secondary combustion furnace 76, and from this, the secondary combustion furnace 76 is provided. Combustible gas is blown into the interior while burning. The high temperature combustible gas blown in this way mixes with the secondary air sucked from the air suction passage 76b and burns in the burner portion 76a provided in the secondary combustion furnace 76, and this flame burns the combustion chamber on the downstream side. It comes out to 76c.

This flame entrains the air in the combustion chamber 76c and burns so that the unburned components are almost eliminated, and the high-temperature combustion gas (burned gas) generated thereby passes through the steam generating section 72 and the downstream side thereof. After passing through the exhaust pipe 78, a dust collector (not shown), etc., it is released into the atmosphere. Since the combustible gas generated from the small particles is burned in this way, the exhaust gas contains few harmful substances and can be cleaned by a general dust collector.

The steam generating section 72 has a general configuration, and a detailed description thereof will be omitted, but in a spiral shape (or in a zigzag manner in the combustion chamber 76c) so as to surround the combustion chamber 76c of the secondary combustion furnace 76 in which flame blows out. The pipe 72a is provided, and the steam or water flowing through the pipe 72a is heated by the flame or combustion gas in the combustion chamber 76c to generate high-temperature steam. As shown in FIG. 1, a part of the generated steam 79 is supplied to the reduced pressure fermentation dryer 3 through the pipe 72 a and the steam path 70 to heat the tank 30 of the reduced pressure fermentation dryer 3. The jacket 31 is circulated to heat the inside of the tank 30. Therefore, since the small particles of the dried material obtained by the reduced pressure fermentation dryer 3 can be used as the biomass fuel 40, the heating steam 79 required in the reduced pressure fermentation dryer 3 can be generated, and thus the palm oil of the present invention can be used. It is possible to reduce the running cost of the entire residue treatment system.

The rest of the steam 79 generated in the biomass boiler 7 is supplied to the steam turbine generator 9 via the pipe 72a and another steam passage 87.

Although not shown, the steam turbine generator (generator) 9 has a steam turbine inside, and flows high-temperature and high-pressure steam 79 from the biomass boiler 7 toward the impeller of the steam turbine through the steam passage 87. Generates electric power by rotating the steam turbine at high speed. This generated electric power is supplied to the reduced pressure fermentation dryer 3 via an electric cable 88, as shown in FIG. Therefore, the electric power generated by the steam turbine generator 9 can be used as a part of the electric power used in the reduced pressure fermentation dryer 3, and the running cost of the entire palm oil residue treatment system C can be further reduced. Is. In addition, surplus electric power other than the electric power used for the power used in the reduced pressure fermentation dryer 3 is supplied to other devices, and if there is still surplus electric power, it is possible to sell the electric power to an electric power company.

As described above, in the present embodiment, all of the residue B at the palm oil factory can be fermented by the reduced pressure fermentation dryer 3 and processed into a greatly reduced volume dried product. Moreover, since this dried product is burned as the biomass fuel in the biomass boiler 7, almost no industrial waste is generated, and the processing cost thereof is reduced.

In the present embodiment, as the residue B at the palm oil factory, all of the empty fruit bunch EFB, Chinese fruit peel fiber MF, palm palm shell PKS, etc., sludge and sludge POME are put into the vacuum fermentation dryer 3. The present invention is not limited to this, but the present invention is not limited to this, and a part of the factory residue B, for example, empty fruit bun EFB only, or empty fruit bun EFB and two of sludge and sludge POME, and further empty fruit. The reduced pressure fermentation dryer 3 may be a combination of the three groups such as the bunch EFB, the mesocarp fiber MF, and the palm palm shell PKS, and other combinations.

Furthermore, most of the dried material (small particles) discharged from the reduced pressure fermentation dryer 3 is used as the biomass fuel 40 in the biomass boiler 7, and steam 79 is generated as a heat source for heating the tank 30 of the reduced pressure fermentation dryer 3. Therefore, it is possible to generate a heat source (steam) with almost no waste.

In addition, the steam generated by the biomass boiler 7 is used to drive the steam turbine generator 9, and the generated power is used as a part of the power used in the reduced pressure fermentation dryer 3 to reduce the running cost. If there is surplus power, it is possible to sell it to a power company.

The embodiment disclosed this time is an example in all respects, and is not a basis for a limited interpretation. The technical scope of the present invention should not be construed only by the embodiments described above, but should be defined based on the claims. Further, the technical scope of the present invention includes all modifications within the meaning equivalent to the scope of the claims.

The present invention can be used for a treatment apparatus for palm oil factory residue and a treatment method therefor.

A Palm oil refining process in palm oil factory B Palm oil factory residue C Palm oil residue processing system 3 Vacuum fermentation dryer 30 Tank (closed container)
7 Biomass boiler (heat source equipment)
9 Steam turbine generator (generator)
93 Empty Fruit Bunch (EFB)
99 Sludge and sludge (POME)
103 Mesocarp fiber (MF)
106 Palm palm shell (PKS), etc.

Claims

The residue produced at the palm oil factory is placed in a closed container and stirred under reduced pressure while heating to a specified temperature range, while using microorganisms to decompose the organic components of organic matter to obtain a reduced volume dried product. A vacuum fermentation dryer,
A heat source device that is disposed in a subsequent stage of the reduced pressure fermentation dryer and that burns the obtained dried material to generate a heat source.
The palm oil factory residue treatment apparatus according to claim 1,
The palm oil factory residue comprises at least one of empty fruit bunch, mesocarp fiber and palm palm shell.
The apparatus for treating the residue of a palm oil factory according to claim 2,
The palm oil plant residue treatment equipment further comprises sludge and sludge.
The palm oil factory residue treatment apparatus according to claim 1,
Part of the heat source generated by the heat source device is used in the reduced pressure fermentation dryer, and the palm oil factory residue treatment apparatus is characterized.
The palm oil factory residue treatment apparatus according to claim 1,
A palm oil plant residue treatment apparatus, comprising a generator connected to the heat source device and receiving a part of the generated heat source to generate electricity.
The apparatus for treating the residue of a palm oil factory according to claim 5,
Electricity obtained by the generator is used in the reduced pressure fermentation dryer, wherein the palm oil factory residue treatment apparatus is characterized.
The residue produced at the palm oil factory is placed in a closed container and stirred under reduced pressure while heating to a specified temperature range, while using microorganisms to decompose the organic components of organic matter to obtain a reduced volume dried product. A reduced pressure fermentation drying step,
A heat source generation step of burning the dried material obtained in the reduced pressure fermentation drying step to generate a heat source.