KR20070096823A - Processing device for waste cooking oil - Google Patents

Abstract

A processing device for waste cooking oil is provided to dispose the waste cooking oil continuously. A processing device for waste cooking oil performs transesterification of the waste cooking oil to produce glycerin and ester, wherein after mixing the waste cooking oil and an ester exchanging agent by an in-line mixer(20), the processing liquid produced by transesterification is introduced into a pair of glycerol separation baths(27a,27b) by turns to be separated into glycerin and ester, the separated glycerin is burned in a boiler(70), and the heat generated in the boiler is employed in heating or transesterification of the waste cooking oil, and in removal of moisture in oil regenerated from the ester.

Description

Processing Device for Waste Cooking Oil

1 is a view showing an embodiment of the present invention.

2 is a flow chart (flow chart) showing another embodiment of the present invention.

Description of the main symbols in the drawings

10: import nozzle for tank cars 11: transport drum

12: import line 13: strainer

14: import pump 15a: discharge side line

15b: Return line 16: Import tank

17: raw material supply tank 18: double strainer

19: fixed-supply pump 20: first in-line mixer

21: transesterification tank 24: stirrer

25: strainer pump 26: first three-way solenoid valve

27a: first glycerin separation tank 27b: second glycerin separation tank

28a, 28b: optical liquid level gauges 29a, 29b: switching valve

30: reservoir 31a, 31b: switching valve

32: intermediate tank 33: strainer

34: pump 35: second in-line mixer

36: second three-way switching valve 37a, 37b: neutralized washing water separation tank

38a, 38b: Optical liquid level meter 39a, 39b: Switching valve

40: neutralized washing water tank 44: stirrer

45: strainer 46: fixed-supply pump

47a, 47b: switching valve 48: regeneration oil tank

50: double strainer 51: pump

52: third in-line mixer 53: line

55: fresh water tank 56: pump

57a, 57b: oil-water separator 58a, 58b: optical liquid level meter

59a, 59b: selector valve 60: line

61: jacket type evaporator 63a, 63b: switching valve

66: steam heater 70: boiler

71: double strainer 72: pump

73: burner 74: separator

75: line 76: product tank

77: wastewater port 78: water tank

79: plural water pump 80: on-off valve

82: line

Field of invention

The present invention relates to a waste cooking oil processing apparatus capable of continuously processing waste cooking oil.

Background of the Invention

In the treatment of the spent cooking oil after the use of cooking oil such as frying oil, caustic soda is used as a catalyst, mixed with methanol and subjected to a transesterification reaction, and the reaction product is separated into glycerin and methyl ester with a separator (methyl separator), and methyl It has been tried to use ester as a fuel of a diesel engine (Japanese Patent Laid-Open Nos. 10-182518, 2000-219886, and 2004-67937).

Cooking oil constitutes a fat or oil which is a glycerin ester, and by transesterification, methanol and glycerin having high viscosity are replaced by reaction with methanol to produce methyl ester and glycerin.

Unlike the new oil that is squeezed out, the waste cooking oil is mixed with various impurities (fried waste, water, etc.) used for cooking, and is oxidized by heat cooking. It is necessary to carry out the transesterification reaction after removing impurities such as impurities and impurities.

However, even if a pretreatment step is performed, the transesterification reaction is a batch operation, and no device for continuously treating waste cooking oil has been developed.

An object of the present invention is to solve the above problems and to provide a waste cooking oil processing apparatus capable of continuously treating waste cooking oil.

The above and other objects of the present invention can be achieved by the present invention described below.

Summary of the Invention

In order to achieve the above object, the present invention provides a treatment apparatus for waste cooking oil which produces glycerine and ester by transesterification of waste cooking oil, and after mixing the waste cooking oil and the transesterification agent in an in-line mixer, The treatment liquid is alternately introduced into a pair of glycerin separation tanks, separated into glycerin and esters, and the separated glycerin is combusted in a boiler, and the heat generated from the boiler is composed of heating, transesterification reactions, and esters of waste cooking oil. It is a treatment apparatus for waste cooking oil used for removing water in recycled oil.

In addition, the present invention provides a raw material supply tank for storing two or more import tanks for receiving waste cooking oil, mixing means for mixing the waste cooking oil in each of the imported tanks, and storing the mixed waste cooking oil. And a first in-line mixer which continuously mixes an ester exchange agent composed of an alcohol such as methanol and a catalyst such as caustic soda and waste cooking oil from the raw material supply tank, and a treatment liquid after the transesterification reaction from the first in-line mixer. A pair of glycerin separation tanks for separating crude regenerated oils formed by introducing glycerin and esters, a boiler using glycerin precipitated in a glycerin separation tank as a fuel, and fresh water and dilute sulfuric acid. Iii) a second inline mixer for continuously mixing neutralized wash water mixed with magnesium and crude regenerated oil separated in a glycerin separation tank, and a second inline From a pair of neutralized washing water separation tanks, which alternately introduce the washing tank recycled oil from the waste water and separates the washing water and the recycled oil, a third inline mixer for continuously mixing the separated recycled oil with fresh water, and a third inline mixer. The oil-water separation tank which alternately introduces regeneration oil mixed with fresh water and recovers the regeneration oil by separating the oil-water, and introduces the regeneration oil separated in the oil-water separation tank and heats it with steam from the boiler to separate the water in the regeneration oil. It is a processing apparatus of waste cooking oil provided with a steam heater.

In the present invention, the import tank, the raw material supply tank, the first to third inline mixers, and each separation tank may be accommodated in a cabinet surrounding the boiler.

In the present invention, an optical liquid level gauge is provided in the glycerin separation tank and the neutralized washing water separation tank, and the liquid level gauge may be monitored to separate the lower and upper liquids.

According to the present invention, the waste cooking oil can be treated continuously, and at the same time, glycerin is burned in a boiler to exhibit an excellent effect of using the heat source.

Detailed Description of the Invention

The "apparatus for treating waste cooking oil" described and described in the present specification and claims and drawings is described in Japanese Patent Application No. 2006-083473.

EMBODIMENT OF THE INVENTION Hereinafter, one suitable embodiment of this invention is described in detail based on an accompanying drawing.

In Fig. 1, the raw material (waste oil) is taken as a transport drum 11 by a tank car import nozzle 10, and an import line (which can be directly from a tank car). Through 12), solid matter etc. are removed from the strainer 13, and it is taken in by the import pump 14 to two or more import tanks 16 in the discharge side line 15a.

The waste cooking oil accepted by the import tank 16 has various qualities, and the extremely poor quality does not easily cause transesterification, which will be described later. By storing the high quality waste cooking oil and the low quality waste cooking oil from the return line 15b to the strainer 13 and the import pump 14, and supplying to the raw material supply tank 17 from the discharge side line 15a. Use waste oil with stable quality. This raw material supply tank 17 is made into the capacity of about 800L which can hold the throughput for one day.

The raw material from the raw material supply tank 17 is sent to the 1st in-line mixer 20 after filtration by the double strainer 18, for example at 34 L / h by the fixed quantity supply pump 19. As shown in FIG.

On the other hand, alcohol 22, such as methanol, and catalyst 23, such as caustic soda, are supplied to the transesterification tank 21, and are stirred in the stirrer 24 to form a transesterification agent. The transesterification agent is made by adding 0.05 kg of caustic soda to 1 L of methanol, which is sent to the first in-line mixer 20 via a constant amount (6.8 L / H) strainer pump 25.

The raw material and the transesterification agent are mixed while flowing in the first in-line mixer 20 to cause the transesterification reaction. As described later, the inline mixer 20 is accommodated in the cabinet C, the ambient temperature is maintained at 40 to 60 ° C, and continuous transesterification reaction is carried out by mixing the raw material and the transesterification agent in the inline mixer 20. It becomes possible.

The fluid after the transesterification reaction alternately flows into the first glycerin separation tank 27a and the second glycerin separation tank 27b every 30 minutes by switching between the first three-way solenoid valves 26. Enter

After receiving, the sedimentary separation is alternately settled in the glycerin separation tanks 27a and 27b, and the separation tanks 27a and 27b are monitored by the optical liquid level gauges 28a and 28b to monitor the interface between the crude crude oil at the top and the glycerin at the bottom. Then, the sedimentation separation separates the glycerin stayed in the lower portion, and sends to the glycerin storage tank (30) through the switching valve (29a, 29b).

Thereafter, the switching valves 29a and 29b are closed, and the crude regeneration oil made of the ester retained thereon is taken into the intermediate tank 32 via the switching valves 31a and 31b. By repeating the above operations alternately, continuous processing becomes possible.

Although described later, the glycerin stayed in the glycerin storage tank 30 is supplied to the boiler 70 by the double strainer 71 and the pump 72.

The crude regeneration oil is again sent to the second in-line mixer 35 via the strainer 33 and the pump 34.

In the neutralized washing water tank 40, the fresh water 41, the dilute sulfuric acid 42, and the magnesium 43 are mixed in the stirrer 44 to be neutralized washing water. This neutralized washing water is mixed with 0.02 L of dilute sulfuric acid and 0.25 kg of magnesium with respect to 1 L of fresh water to obtain neutralized washing water.

The neutralized washing water is supplied to the second in-line mixer 35 at 35 mL / H from the strainer 45 and the fixed-quantity supply pump 46, mixed with the crude regeneration oil, and then the second three-way switching valve 36. Through this, it is alternately sent to a pair of neutralization wash water separation tanks 37a and 37b. There, by the same operation as that of glycerin separation, that is, the boundary surfaces are monitored by the optical liquid level gauges 38a and 38b with the separation tanks 37a and 37b, and the water retained at the bottom by sedimentation separation is switched valves 39a and 39b. Via the on-off valve 80 to return to the neutralized washing water tank 40 by gravity flow, or via the on-off valve 81 to the gravity flow from the line 82 to be described later. Supply to the jacket type evaporator (61).

The neutralized washing water tank 40 and the jacket-type evaporator 61 are installed in the cabinet C lower than the neutralizing washing water separation tanks 37a and 37b, and are separated from the separation tanks 37a and 37b. The neutralized washing water flows in the gravity flow in the lines 53 and 82 to the neutralizing washing water tank 40 or the jacketed evaporator 61, respectively.

The neutralized washing water sees the concentration of the neutralized material, and when the concentration is low, the on / off valve 80 is opened to return to the neutralized washing water tank 40 from the line 53. When the concentration is high, the on / off valve 81 is opened. It is opened and supplied to the jacketed evaporator 61 in the line 82.

Thereafter, the switching valves 39a and 39b are closed, and the crude regeneration oil stayed in the upper portion is taken into the regeneration oil tank 48 through the switching valves 47a and 47b.

The regeneration oil is supplied from the regeneration oil tank 48 to the third inline mixer 52 by the double strainer 50 and the pump 51, and the fresh water tank which stores the fresh water 54 in the inline mixer 52. Fresh water is supplied from the 55 to the pump 56, continuously mixed in the third in-line mixer 52, and through the third three-way valve 56 to a pair of oil / water separation tanks 57a and 57b. It is sent alternately.

In the oil / water separation tanks 57a and 57b, water is similarly separated, and the liquid level gauges 58a and 58b monitor the interface and settle and separate the water retained in the lower portion through the switching valves 59a and 59b. , To the jacketed evaporator 61 in line 60.

Thereafter, the switching valves 59a and 59b are closed to supply the regenerated oil retained on the upper portion to the steam heater 66 via the switching valves 63a and 63b.

The steam generated by the boiler 70 is supplied to the steam heater 66, and the regeneration oil is indirectly heated by the steam and heated to about 100 ° C. Thereafter, the regenerated oil is supplied to the separator 74, the steam in the regenerated oil is separated, the water concentration is kept within a predetermined value, and stored in the product tank 76 as a final product.

In the boiler 70, glycerin is sent to the burner 73 and combusted, and it is provided for saturated steam generation of 1.1 kg / cm <2> h.

The waste water separated by the oil-water separation tanks 57a and 57b and the washing water from the line 82 are supplied to the jacket-type evaporator 61, and steam from the steam heater 66 is supplied to the jacket of the evaporator 61. The wastewater is supplied, heated in the jacketed evaporator 61, steam is exhausted in line 75, and the reduced wastewater is drained to wastewater port 77 and then drained out of the apparatus.

In addition, the condensed water from the jacket stays in the water tank 78 and is circulated and supplied from the plurality of pumps 79 to the boiler 70.

As described above, the cabinet C surrounds the boiler 70 and excludes the transport drum 11, the import tank 16, the raw material supply tank 17, and the fixed-quantity supply pump 19 in the cabinet C. Since almost all the apparatuses are accommodated and the cabinet C is maintained in an atmosphere of 40 to 60 ° C., it is not necessary to heat the raw materials or separately heat the first in-line mixer 20 in the transesterification reaction. In addition, since the second and third in-line mixers 35 and 52 and the separators 27, 37 and 57 are also maintained in the range of 40 to 60 ° C, good mixing and separation can be performed.

2 shows another embodiment of the present invention.

In the embodiment of Fig. 1, after the transesterification of the waste cooking oil, it was described as an example in which the ester and glycerin were separated, the separated ester was neutralized with sulfuric acid and magnesium, and the ester separated from the neutralized water was washed with fresh water. In the present embodiment, as a pretreatment for neutralizing the ester with sulfuric acid and magnesium, after neutralizing with hydrochloric acid, the ester is neutralized with sulfuric acid and magnesium, and washed with fresh water twice.

Referring to the flow of this treatment, the waste cooking oil 100 is converted into ester and glycerin 101 by transesterification reaction, and is separated (102) into ester (103) and glycerin (104), and ester (103) is used. Neutralize 105 with hydrochloric acid, separate 106 to obtain ester 107 and neutralized water 108, neutralize the ester 107 with sulfuric acid and magnesium 109, and separate it 110. The ester 111 and the neutralized water 112 were used, the ester 111 was washed 113 with fresh water, and the ester 115 from which the washed water 114 was separated was further washed with fresh water 116, and washed. The water 117 is separated and used as the regeneration oil 118.

For neutralization by hydrochloric acid, the mixture is mixed using the inline mixer shown in FIG. 1, and the separation is performed using a pair of sedimentation separation tanks, and the washing with a fresh water is also performed by the inline mixer and the pair of sedimentation separation types. Use a separation tank.

In this embodiment, it is possible to obtain a higher purity recycled oil by neutralizing twice with hydrochloric acid and sulfuric acid and washing twice with fresh water.

This invention has the effect of the invention which can process waste cooking oil continuously.

Simple modifications and variations of the present invention can be readily used by those skilled in the art, and all such variations or modifications can be considered to be included within the scope of the present invention.

Claims (8)

A waste cooking oil processing apparatus for producing glycerine and esters by transesterification of waste cooking oil, wherein the waste cooking oil and the transesterification agent are mixed in an in-line mixer, and then the treated solution after the transesterification reaction is fed to a pair of glycerin separation tanks. It is introduced alternately, and separated into glycerin and ester, and the separated glycerin is combusted in a boiler, and the heat generated in the boiler is used for heating or transesterification of waste cooking oil and removing water from regenerated oil formed from ester. Waste treatment oil processing device. The waste cooking oil processing apparatus according to claim 1, wherein the separated ester is neutralized with an aqueous magnesium sulfate solution to separate the ester, the ester is washed with fresh water, and the ester is separated from the fresh water to be a regenerated oil. The method of claim 1, wherein the ester is neutralized with hydrochloric acid to separate the ester, the ester is further neutralized with an aqueous magnesium sulfate solution to separate the ester, and the neutralized separated ester is washed twice with fresh water to obtain the ester. A waste cooking oil processing apparatus, characterized in that the regeneration oil. The method of claim 1, wherein the two or more import tanks for receiving waste cooking oil, mixing means for mixing the waste cooking oil in each of the import tanks, a raw material supply tank for storing the mixed waste cooking oil, alcohol and caustic such as methanol Glycerine and ester produced by alternately introducing a first in-line mixer for continuously mixing a transesterification agent consisting of a catalyst such as soda and waste cooking oil from the raw material supply tank, and a treatment solution after the transesterification reaction from the first in-line mixer. A pair of glycerin separation tanks for separating crude regenerated oil, a boiler using glycerine precipitated in a glycerin separation tank as a fuel, and neutralized washing water mixed with fresh water, dilute sulfuric acid and magnesium, and crude regeneration oil separated in a glycerin separation tank. Alternately mixing the second in-line mixer and the washing crude oil from the second in-line mixer A pair of neutralized washing water separation tanks separated into washing water and regeneration oil, a third inline mixer for continuously mixing the separated regeneration oil with fresh water, and a regeneration oil mixed with fresh water from the third inline mixer. It is characterized in that it comprises an oil-water separation tank for introducing and separating the oil-water and recovering the regenerated oil, and a steam heater for separating the water in the regenerated oil by introducing steam from the boiler while introducing the recycled oil separated in the oil-water separation tank. Apparatus for processing waste cooking oil. 5. The apparatus of claim 4, wherein an import tank, a raw material supply tank, first to third inline mixers, and each separation tank are accommodated in a cabinet surrounding the boiler. 5. The waste cooking oil according to claim 4, wherein an optical liquid level gauge is installed in the glycerin separation tank and the neutralization washing water separation tank, and the liquid level gauge is separated by monitoring the interface with the optical liquid level gauge. Processing unit. 5. The treatment apparatus for waste cooking oil according to claim 4, wherein the crude regenerated oil separated in the glycerin separation tank is neutralized with hydrochloric acid before being neutralized with neutralized washing water mixed with fresh water, dilute sulfuric acid and magnesium. The waste cooking oil according to claim 4, wherein the regeneration oil separated by the neutralized washing water separation tank is mixed with fresh water to separate the regeneration oil from the fresh water, and then mixed with the fresh water, and the regeneration oil is separated from the fresh water. Processing unit.

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