KR101493966B1 - a method and system for purify in waste oil - Google Patents

Abstract

The present invention makes it possible to increase the oil production efficiency of light oil, kerosene and gasoline by pre-heating in a pyrolysis oil preheating reactor in a pyrolytic oil preheating reactor. The oil of the light oil, kerosene, The oil is separated from the oil by distillation to obtain high-quality gas oil, kerosene and gasoline oil. The waste oil is pyrolyzed in a vapor state to increase the production amount of oil. Finally, the condensable oil The present invention relates to a refining system for refining waste oil and a refining method for refining and re-pyrolyzing oil by removing mist, tar and other impurities, thereby maximizing treatment efficiency while increasing oil production efficiency.
The technical constitution is as follows: a) The oil and the pyrolysis oil are introduced through the injection pipe of the pyrolysis oil preheating reactor and preheated at a temperature of 250 to 350 ° C to convert the diesel, kerosene and gasoline oil contained in the waste oil and pyrolysis oil into vapor ;
b) The vaporized oil, kerosene and gasoline vapor of the pyrolysis oil preheating reactor in step a) are discharged through a pipe and sequentially introduced into a wax / dust remover and a diesel oil rapid condenser. The waste oil and pyrolysis oil crude oil are introduced into a pyrolysis oil purification reactor And pyrolysis;
c) The diesel oil, kerosene, and petroleum oil phase which are pyrolyzed and discharged in the pyrolysis oil refining reactor of the step b) are introduced into the wax / dust remover, and the temperature is controlled at 350 to 400 ° C to produce a wax having a higher boiling point, And then pyrolyzing by reheating after re-entering the lower oil purification reactor;
d) The vapor of the pyrolysis oil preheating reactor, the pyrolysis oil refining reactor and the vapor of the wax / dust remover are introduced into the diesel oil rapid condenser and rapidly cooled to liquefy the vaporized pyrolysis oil vapor having the boiling point of 330 to 380 ° C To a diesel oil condenser lower hopper through a drain line communicated on one side thereof;
e) The diesel oil condensate of step d), which has a boiling point of 380 ° C. or lower, flows into the diesel oil condenser, and the oil vapor of the diesel oil having a boiling point of about 280 to 330 ° C. is liquefied and flows into the spiral cooler ;
f) The liquid phase of the diesel oil introduced into the spiral cooler in step e) is cooled to room temperature, and then flows into the diesel primary and secondary oil water separators through the water level automatic regulating unit, Second separation;
g) the oil vapor of the kerosene phase in step e) is introduced into the kerosene oil rapid condenser and rapidly cooled to pyrolysis oil vapor of kerosene phase having a boiling point of 180 to 230 ° C. and then transferred to the kerosene oil condenser bottom hopper ;
h) In the step g), the oil vapor having a boiling point of less than or equal to 230 ° C flows through the kerosene oil condenser and the kerosine oil vapor having a boiling point of 180 to 230 ° C is liquefied and introduced into the gas oil spiral cooler.
i) The liquid phase of the kerosene phase introduced into the kerosene spiral cooler of step h) is cooled to room temperature and then flows into the primary and secondary oil water separator through the water level automatic regulating unit so that the oil and kerosene- So as to be separated;
j) The oil vapor of the gasoline phase in step h) is introduced into the gasoline oil rapid condenser and rapidly cooled to liquefy the vaporized pyrolysis oil vapor having a boiling point of 110 to 180 DEG C and then transferred to the lower hopper of the gasoline oil condenser step;
k) the non-condensable gas in step j) is discharged through the upper pipe, and the oil vapor of the gasoline phase having a boiling point of 30-180 캜 is liquefied and introduced into the gasoline spiral cooler; And
l) The liquid phase of the gasoline phase introduced into the gasoline spiral cooler of step k) is cooled to room temperature and then flows into the primary and secondary oil water separator through the water level automatic regulating unit so that the oil of the gasoline- And separating the waste water from the waste water. As shown in FIG.

Description

BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a method for purifying waste oil,

The present invention relates to a refining system for refining waste oil and a refining method thereof, and more particularly, it relates to a refining system for refining waste oil and pyrolysis oil in a pyrolysis oil preheating reactor so as to increase the oil production efficiency of diesel, kerosene and gasoline by pre- Kerosene and gasoline oil can be obtained by primary and secondary oil-water separation by high-quality light oil, kerosene and gasoline oil, and the waste oil is pyrolyzed in a vapor state to increase the production amount of oil, and finally, Condensed oil mist, tar and other impurities in the non-condensable gas discharged after refining the oil, and recirculates and re-pyrolyzes the oil, thereby improving the efficiency of the oil production and improving the efficiency of the waste oil The present invention relates to a purification system and a purification method thereof.

Methods of purifying waste oil generally known are roughly divided into a chemical treatment method and a physical treatment method, wherein the chemical treatment method has a disadvantage in that the quality level of the purified product is low and contains a large amount of environmental pollutants.

As a physical method for purifying wasted oil, a high-temperature pyrolysis method is known, but the high-temperature pyrolysis method is a refining method having a high level of refined oil and low content of environmental pollutants and a high value-added purification method.

However, the pyrolysis method of waste oil is disadvantageous in that the product is unstable, tar is generated, and the odor is severe because pyrolysis is performed by heating at a high temperature under normal pressure. In addition, after a certain time has elapsed, sediments are generated, and tar is used to cause clogging in combustion nozzles and piping when burners are used. Also, because of operation at a high temperature, the durability of the equipment is short and the risk of fire and explosion is relatively high It is.

On the other hand, in the method for producing ionic refining oil by chemical treatment of waste oil, a chemical agent is reacted with a metal ion floating in a waste oil without precipitation in a waste oil to make a metal ion insoluble metal salt, And then separated.

The ion purification method has a simple process and all the processes are performed at 120 to 150 ° C. Therefore, there is little risk of fire and explosion, and a facility investment cost is low. However, an agitation device for reacting with ammonium phos- phate, The reaction time of a certain time is required, and since the amount of the chemical introduced each time and the reaction time are difficult to control, the waste oil is not completely purified, and the unreacted chemical and heavy metal ions react with the purified ionized oil So that refined oil having low purity is produced.

In recent years, metal ions suspended in waste oil are eluted into crystalline metal molecules by using resonance and resonance devices, and the tensile strength and viscosity of the pulp particles are lowered so that they can be easily precipitated, and the moisture content of the clusters in the waste oil A waste oil purification method capable of producing an ionic purified oil that can be easily evaporated by converting it into an active water releasing energy and shortening a process time is known in Korean Patent Registration No. 10-0880387.

The purification method includes a multistage filtration step for removing solids such as sludge in the waste oil, and a step for storing the filtered waste oil and a radiation wavelength of 6 to 11 μm wavelength band, which is a resonance absorption wavelength of water molecules, through a far- And converting the dissolved mineral or metal ions dispersed in the waste oil into crystalline mineral or metal water through a resonance or resonance device to purify the mineral oil or metal water, An active waste oil conversion step of lowering the tension and viscosity of the waste oil particles, a flow rate distribution stage for distributing and supplying the converted active waste oil to the fractional distillation apparatus and preheating the active waste oil by using waste gas, A step of fractionally distilling water and light oil to produce water-refined oil; and a step of solidifying the crystalline mineral or metallic substance in the water- To remove the fine particles, and removing impurities through yusubun separation stage and a rectifying the separated fractions after fine impurity removal module for removing the residual water in the water layer to separate refined oil and commercialized.

Accordingly, it is possible to easily convert metal ions suspended in waste oil into metal by using a resonance or resonance device while easily removing sludge and solids from the waste oil, The oil is purified by filtration using the above-mentioned filtration apparatus, resulting in a large installation area of the waste oil refining apparatus, resulting in a reduction in treatment efficiency and inability to obtain a high-quality oil.

1. Korean Patent Registration No. 10-0880387

SUMMARY OF THE INVENTION The present invention has been made in order to solve the above-mentioned problems, and it is an object of the present invention to provide a method for preheating waste oil and pyrolysis oil in a pyrolysis oil preheating reactor so as to increase oil production efficiency of diesel, kerosene and gasoline Kerosene and petroleum oil can be obtained by primary and secondary oil-water separation of the diesel oil, kerosene oil and gasoline oil phase, and the high-quality diesel oil, kerosene oil and gasoline oil can be obtained by pyrolyzing the waste oil in a vapor state, Which is capable of increasing the oil production efficiency even further by recycling and re-pyrolyzing condensate oil mist, tar and other impurities in non-condensable gas discharged after refining the oil of the gasoline phase, .

It is another object of the present invention to provide a waste oil refining system capable of maximizing the treatment efficiency while minimizing the installation area of the waste oil refining apparatus.

As a technical means for achieving the above object, the present invention provides a method for purifying waste oil,

a) Thermal cracking oil Waste oil and pyrolysis oil are introduced through an injection pipe connected to the upper side of the preheating reactor and preheated at a temperature of 250 to 350 ° C to convert diesel, kerosene and gasoline oil contained in waste oil and pyrolysis oil into vapor ;

b) The vaporized oil, kerosene and gasoline oil vapor generated in the pyrolysis oil preheating reactor in step a) are discharged through a pipe and sequentially introduced into a wax / dust remover and a diesel oil quick condenser, and the wax / And the pyrolysis oil in the vapor phase of the gas oil, the kerosene and the gasoline phase is introduced into the pyrolysis oil purification reactor at the lower side through the pipe and pyrolyzed;

c) The diesel oil, kerosene and gasoline phase oil which is pyrolyzed and discharged in the pyrolysis oil refining reactor of step b) is introduced into the upper wax / dust remover, and the temperature is adjusted to 350 to 400 ° C to adjust the wax And after the heavy oil is condensed, re-entering the lower oil purification reactor and pyrolyzing by reheating;

d) The vapor of the pyrolysis oil preheating reactor, the pyrolysis oil refining reactor, and the vapor of the wax / dust remover are introduced into the diesel oil rapid condenser through piping and rapidly cooled to produce a diesel oil vapor having a boiling point of 330 to 380 ° C To a diesel oil condenser lower hopper through a drain line communicated on one side thereof;

e) The diesel oil of the step d), which has a boiling point of 380 ° C. or lower, flows into the diesel oil condenser, and the diesel oil vapor having a boiling point of about 280 to 330 ° C. passes through the diesel oil condenser, Into the spiral cooler;

f) The liquid phase of the diesel oil introduced into the spiral cooler in step e) is cooled to room temperature and then flows into the diesel oil primary water separator through the level automatic regulating unit composed of an inverted U-shaped pipe, The oil and water are firstly separated by an oil separator, and the oil of the oil phase separated from the first water is introduced into the oil secondary oil water separator, and the oil and the oil of the oil phase are separated and separated by the precipitation / ;

g) The oil vapor of the kerosene phase discharged from the diesel oil condenser in the step e) is introduced into the kerosene oil rapid condenser through the upper pipe and rapidly cooled to obtain a pyrolysis oil having a boiling point of 180 to 230 ° C Liquefying the vaporized vapor and then transferring the vaporized liquid to the lower hopper of the kerosene oil condenser through the drain pipe adjoined to the one side;

 h) The vapor, which has a boiling point of 230 ° C or less and has flowed into the kerosene oil condenser of step g), passes through the kerosene oil condenser and liquefies the oil vapor of the kerosene phase having a boiling point of 180 to 230 ° C, Entering the spiral cooler;

i) The liquid phase of the kerosene phase introduced into the kerosene spiral cooler of step h) is cooled to room temperature and then flows into the diesel primary oil water separator via the level automatic regulating unit composed of an inverted U-shaped pipe, The oil and water are firstly separated by an oil separator. The oil of the kerosene phase separated from the first water is introduced into the lower kerosene secondary oil water separator, and the oil and kerosene oil are separated by the precipitation / separation method by gravity. So as to be separated;

j) The oil vapor of the gasoline state discharged in a vapor state in the kerosene oil condenser of the step h) is transferred through the pipe and flows into the gasoline oil rapid condenser and rapidly cooled to produce a pyrolysis oil having a boiling point of 110 to 180 ° C Causing the vapor to liquefy and then to be delivered to the bottom hopper of the gasoline oil condenser through the drain line communicated to the one side;

k) The non-condensable gas is discharged through the upper pipe while passing through the gasoline oil condenser of the step j), and the oil vapor of the gasoline phase having a boiling point of 30 to 180 ° C. is liquefied and flows into the gasoline spiral cooler through the lower hopper ; And

l) The liquid phase of the gasoline phase introduced into the gasoline spiral cooler of step k) is cooled to room temperature and then flows into the first oil-water separator through the water level automatic regulating unit composed of an inverted U- The oil and water are firstly separated by a multi-stage oil-water separator. The oil of the gasoline phase separated from the first water is introduced into the second oil-water separator of the gasoline, so that the oil and oil of the gasoline- And separating the waste oil from the waste oil.

In addition, the present invention is characterized in that the waste oil and the pyrolysis oil preheated in the pyrolysis oil preheating reactor of step a) are preheated for 2 to 3 hours.

The wasted oil and the pyrolysis oil crude oil in the gas oil, the kerosene and the gasoline oil flowing into the pyrolysis oil refining reactor of the step b) are heated to 450 to 500 ° C to pyrolyze the wax / And water vapor is injected from the lower side to induce the hydrogenation reaction.

In addition, the diesel oil pyrolysis oil at room temperature is injected into the upper part of the diesel oil rapid condenser in step d) to rapidly cool the vapor introduced into the diesel oil rapid condenser, and the kerosene oil quick condenser of step g) The pyrolysis oil on the kerosene phase at the room temperature is injected into the upper portion of the gasifier so that the vapor of the kerosine phase flowing through the pipe is rapidly cooled and the gasoline oil rapid condenser of the step j) So that the vapor of the gasoline phase flowing through the pipe is rapidly cooled.

Meanwhile, the non-condensable gas discharged upward from the gasoline oil condenser in step k) is transferred to a non-condensable gas scrubber on one side thereof through a pipe, scrubbed with cleaning water, and condensable The oil mist, tar and other impurities are removed, and a gas scrubber oil separator is disposed below the non-condensable gas scrubber to separate the condensable oil mist, tar and other impurities in the washing water from the oil, Recycle to the reactor and pyrolysis again.

In addition, the present invention relates to a purification system for waste oil,

A pyrolysis oil preheating reactor in which waste oil and pyrolysis oil are introduced through an injection pipe installed at an upper side and preheated to a predetermined temperature;

A wax / dust remover connected to the pyrolysis oil preheating reactor via a pipe through which oil vapor of kerosene, kerosene and gasoline is transferred to remove the wax / dust;

A pyrolysis oil purification reactor communicating with the lower side of the wax / dust remover, wherein the wax and the heavy oil having a boiling point higher than a predetermined temperature in the oil vapor of the wax / dust remover are condensed and liquefied;

A diesel oil rapid condenser for rapidly cooling the oil vapor in the vapor state of the vapor state in which the vapor of the vaporized pyrolysis oil preheating reactor and the vapor of the pyrolysis oil purifying reactor are introduced through the wax / dust remover through the pipe;

 An oil-in-oil condenser connected to one side of the diesel oil rapid condenser through a drain pipe and communicating with the lower hopper;

A water level automatic regulating unit having a spiral cooler for cooling the oil on the diesel oil condition and a downwardly U-shaped piping arranged below the diesel oil condenser;

A primary oil water separator which is connected to the lower side of the water level automatic regulating unit in order to separate the oil and water from each other and a secondary oil water separator which separates the oil on the oil phase by precipitation /

A kerosene oil rapid condenser which is interposed between the diesel oil condenser and the piping to rapidly cool the oil vapor in the vapor phase kerosene phase;

A kerosene oil condenser which is connected to one side of the kerosene oil rapid condenser through a drain pipe and communicates with the lower hopper;

A water level automatic regulating unit which is arranged below the kerosene oil condenser and comprises a spiral cooler for cooling the oil in kerosene phase and an inverted U-shaped pipe spouted below the spiral cooler;

A first oil-water separator for firstly separating the oil and the water, and a second oil-water separator for separating oil from the kerosene oil by the precipitation / separation;

A gasoline oil rapid condenser which is interposed between the kerosene oil condenser and the piping to rapidly cool the oil vapor in the vapor state of the flowing vapor;

A gasoline oil condenser connected to the one side of the gasoline oil rapid condenser through a drain pipe and communicating with the lower hopper;

A water level automatic regulating unit disposed below the gasoline oil condenser and including a spiral cooler for cooling the oil of the gasoline phase and an inverted U-

A primary oil-water separator which is connected to the lower side of the water level automatic regulating unit in order to separate oil and moisture from each other and a secondary oil-water separator which separates the oil on the oil- And a purification system for waste oil is provided.

A non-condensing gas scrubber is communicated with one side of the gasoline oil condenser through a pipe to introduce condensable oil mist, tar, and impurities into the clean water into the non-condensable gas scrubber, And the gas scrubber oil water separator is connected to the pyrolysis oil preheating reactor so that condensable oil mist, tar and other impurities are recirculated.

According to the refining system and the refining method of waste oil of the present invention, it is possible to increase the oil production efficiency of light oil, kerosene and gasoline by preheating the waste oil and pyrolysis oil in the pyrolysis oil preheating reactor, Kerosene and gasoline oil can be obtained by primary and secondary oil separation of the oil of the gasoline phase, and the production amount of the oil is increased by pyrolyzing the waste oil in a vapor state, and finally, after the oil purification of the gasoline phase There is an excellent effect that the oil production efficiency can be further improved due to recycling and re-pyrolysis by removing condensable oil mist, tar and other impurities in the discharged non-condensable gas.

While the present invention has been particularly shown and described with reference to specific embodiments thereof, it will be understood by those skilled in the art that various changes and modifications may be made therein without departing from the spirit and scope of the invention as defined by the following claims It will be understood by those skilled in the art that it is easy to know.

BRIEF DESCRIPTION OF THE DRAWINGS FIG. 1 is a schematic block diagram of a waste oil purification system according to the present invention; FIG.
2 is a flow chart for purifying waste oil according to the present invention.

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

FIG. 1 is a schematic diagram of a waste oil refining system according to the present invention. FIG. 2 is a flow chart for purifying waste oil according to the present invention, in which waste oil and pyrolysis oil are introduced through an injection pipe 111 installed at one side A pyrolysis oil preheating to a predetermined temperature is provided on the upper side of the preheating reactor 110 through a pipe P to which oil vapor contained in waste oil and pyrolysis oil, kerosene oil and gasoline oil are transferred, The wax / dust remover 120 is connected to the lower side of the wax / dust remover 120 and the pyrolysis oil refining reactor 100 is communicated with the wax / The wax having a boiling point above a certain temperature of the pyrolysis oil refining reactor 100 and the heavy oil are condensed and liquefied and introduced into the pyrolysis oil purification reactor 100.

The vapor in the pyrolysis oil preheating reactor 110 and the vapor in the pyrolysis oil refining reactor 100 are communicated to the diesel oil rapid condenser 130 through the piping P and communicated with the diesel oil rapid condenser 130, The oil vapor condenser 130 is connected to the diesel oil condenser 130 through a drain pipe 131. The diesel oil condenser 130 is connected to the diesel oil condenser 130 through a drain pipe 131. The diesel oil condenser 130, And a lower level hopper 141 of the diesel oil condenser 140. The lower side of the diesel oil condenser 140 is connected to a spiral cooler 142 for cooling the oil on the diesel oil condition, A primary oil water separator 144 for primarily separating the oil and water from the oil via the oil separator 143, and a diesel oil secondary oil separator 145 for separating the oil on the diesel oil from the oil for separation / separation.

The kerosene oil condenser 150 is disposed above the kerosene oil rapid condenser 150. The kerosene oil condenser 150 is connected to the kerosene oil condenser 150 through a pipe P, Oil kerosene condenser 160 is connected to one side of the kerosene oil rapid condenser 150 via a drain pipe 151. The kerosene oil condenser 160 is connected to the kerosene oil condenser 150 through a drain pipe 151. [ A spiral cooler 162 for cooling the kerosene oil, and a water level automatic regulating unit 163 having an inverted U-shaped pipe under the kerosene oil condenser 160. The water level automatic regulating unit 163 is connected to the lower hopper 161, A primary oil water separator 164 for primarily separating oil and moisture from the oil and a kerosene secondary oil water separator 165 for separating the oil from the kerosene oil by secondary precipitation / separation.

In addition, the kerosene oil condenser 160 is provided with a gasoline oil rapid condenser 170 through which the oil vapor in the form of a vaporous state flows into the gasoline oil rapid condenser 170 via the pipe P, And the pyrolysis oil of the gasoline phase at room temperature (30 ° C) is sprayed on the upper side to rapidly cool and liquefy the incoming vapor. The gasoline oil condenser (180) is connected to one side of the gasoline oil rapid condenser A spiral cooler 182 for cooling the oil of the gasoline phase and a water level automatic regulating unit 183 constituted by an inverted U-shaped pipe below the spiral cooler 182 are connected to the lower hopper 81 of the gasoline oil condenser 180, A primary oil water separator 184 for primarily separating oil and moisture from the oil and a secondary oil water separator 185 for separating the oil of the gasoline phase from the oil / It is addressed.

A non-condensable gas scrubber 190 through which a non-condensable gas flows is communicated through a pipe P to the one side of the gasoline oil condenser 810, and the non-condensable gas scrubber 190 Condensable oil mist, tar, and other impurities, which are scrubbed with washing water, are communicated with the gas scrubber oil-water separator 200 on the lower side of the incondensible gas scrubber 190, while the gas scrubber oil- And is connected to the pyrolysis oil preheating reactor 110 so that mist, tar, and other impurities are recirculated.

The waste oil purification method of the present invention having the above-described structure will be described in detail as follows.

1 and 2, waste oil and recycled pyrolysis oil are introduced into the oil preheating reactor 110 (FIG. 1) through an injection pipe 111 communicated to the upper side of the pyrolysis oil preheating reactor 110 in step a) ), And then preheated at a temperature of 250 ° C to 350 ° C for 2 to 3 hours to produce oil, kerosene and gasoline oil in the form of a vapor in the waste oil and pyrolysis oil.

The vaporized oil, kerosene and gasoline vapor of the pyrolysis oil preheater 110 of step a) in step b) are introduced into the wax / dust remover 120 and the diesel oil rapid condenser 130 The wasted oil and the pyrolysis oil crude oil contained in the vapor of the light oil, the kerosene and the petroleum oil introduced into the wax / dust remover 120 are introduced into the wax / dust remover 120 through the piping, After flowing into the reactor 100, the waste oil and the pyrolysis oil crude oil preheated in the pyrolysis oil refining reactor 100 are pyrolyzed by heating at 450 to 500 ° C.

Accordingly, it is possible to increase the oil production efficiency of diesel, kerosene and gasoline by preheating the waste oil and pyrolysis oil in the pyrolysis oil preheater 100.

In step c), the oil oil stream pyrolyzed and discharged in the pyrolysis oil refining reactor 100 of step b) is introduced into the upper wax / dust remover 120. At this time, the wax / The wax and the heavy oil having a higher boiling point are condensed by regulating the temperature to 350 to 400 ° C. and re-introduced into the oil refining reactor 100 to induce pyrolysis by reheating .

In step d), the vapor of the pyrolysis oil preheating reactor 110 and the vapor of the pyrolysis oil refining reactor 100 and the wax / dust remover 120 are introduced into the diesel oil quick condenser 130, The pyrolysis oil of the diesel oil phase at room temperature (30 ° C) is sprayed from the top of the rapid condenser 130 to quickly cool the incoming vapor, liquefying the oil-vapor phase pyrolysis oil vapor having a boiling point of 330 to 380 ° C, And then transferred to the lower hopper of the diesel oil condenser 140 via the drawn drain pipe 131 to realize a quenching effect and a rapid condensation effect.

In step e), the vapor flowing into the diesel oil condenser 140 and having a boiling point of 380 DEG C or lower passes through the diesel oil condenser 140 and flows through the diesel oil condenser 140, And flows into the light oil spiral cooler 142 through the lower hopper 141.

The liquid phase on the diesel oil flowing into the diesel spiral cooler 142 is cooled to a room temperature (30 ° C) state in step f), and then passed through a water level automatic regulating unit 143 composed of an inverted U- Oil separator 144 to separate the oil and moisture from the liquid phase liquid phase containing the water by the multi-stage oil phase separator, and the oil phase of the diesel phase from which the primary water phase is separated is the secondary oil phase Separator 145 so that water and oil on the diesel oil phase are separated by the sedimentation / separation method by gravity. The level-automatic regulating unit 143 composed of the inverted U-shaped pipe is formed of a transparent body, Visually check the production and quality of the diesel oil and visually check the water level by gravity through the reverse U-pipe.

Subsequently, in step g), the oil vapor in a kerosene phase on the diesel oil condenser 140 of the step e) is transferred to the kerosene oil oil-rich condenser 150 through the upper pipe P, , The kerosene oil quick condenser 150 injects pyrolysis oil on the kerosene phase at room temperature (30 ° C) from the upper part and rapidly boils the vapor on the kerosene phase introduced through the pipe P to obtain a boiling point of 180 to 230 ° C The oil vapor in the pyrolysis oil phase is transferred to the lower hopper 161 of the kerosene oil condenser 160 via the drain pipe 151 provided on one side thereof.

In step h), the vapor flowing into the kerosene oil condenser 160 of step g) and having a boiling point of 230 ° C or lower passes through the kerosene oil condenser 160, and the kerosene oil vapor having a boiling point of 180 to 230 ° C And then flows into the spiral cooler 162 through the lower hopper 161.

In step i), the kerosene-like liquid phase introduced into the kerosene spiral cooler 162 in step h) is cooled to room temperature (30 ° C), and then the water level automatic regulating unit 163 composed of an inverted U- And then flows into the kerosene primary oil water separator 164 to separate the oil and the water from the liquid phase of the oil-containing kerosene-containing liquid through the multi-stage oil water separator, and the kerosene- Is introduced into the secondary oil water separator 165 and is separated by the gravity-settling / separation method so that the oil of the water and the kerosene phase are separated by the secondary.

In step j), the oil vapor of the gasoline phase is transferred through the upper pipe P in a vapor state in the kerosene oil condenser 160 of the step h) to the gasoline oil rapid condenser 170 to be spouted, The oil quick condenser 170 injects pyrolysis oil of the gasoline phase at room temperature (30 ° C) from the upper part and rapidly cools the vapor of the gasoline phase flowing through the pipe P to form a gasoline- The liquefied oil vapor of the pyrolysis oil of the gasoline oil condenser 180 is transferred to the lower hopper 181 of the gasoline oil condenser 180 through the drain pipe 171 provided at one side thereof.

In step k), the vapor flowing into the gasoline oil condenser 180 in step j) and having a boiling point of 180 ° C or lower passes through the gasoline oil condenser 180, and flows through the oil vapor of the gasoline- And flows into the gasoline spiral cooler 182 through the lower hopper.

In step 1), the liquid phase of the gasoline phase introduced into the gasoline spiral cooler 182 in step k) is cooled to room temperature (30 ° C), and then the liquid level of the gasoline- 183 to the primary oil water separator 184 to separate the oil and moisture from the liquid phase of the gasoline phase containing water into primary oil and water through the multi-stage oil water separator, The oil of the constellation flows into the second oil water separator 185 of the gasoline oil so that the oil and the oil of the gasoline phase are separated by the precipitation / separation method by gravity.

On the other hand, in the gasoline oil condenser 180, the non-condensable gas is discharged to the upper side and is conveyed to the non-condensable gas scrubber 190 through the pipe P, and then scrubbed with the washing water The non-condensable oil mist separator 200 is disposed below the non-condensable gas scrubber 190 to remove the condensable oil mist, tar and other impurities in the non-condensable gas, Tar and other impurities are easily and easily oil-water separated, and the separated condensable oil mist, tar and other impurities are recycled to the pyrolysis oil preheater 110 via a separate circulation pipe or circulator, It is possible to further increase the oil production efficiency.

100 ... Pyrolysis oil refining reactor
110 ... Oil preheat reactor 120 ... Wax / Dust remover
130 ... Diesel oil rapid condenser 140 ... Diesel oil condenser
142, 162, 182 ... spiral cooler
143, 163, 183 ... automatic level control unit
150 ... kerosene oil rapid condenser 160 .. kerosene oil condenser
170 ... Gasoline Oil Rapid Condenser 180 ... Gasoline Oil Condenser
190 ... non-condensing gas scrubber
200 ... Gas scrubber oil water separator

Claims (13)

In the method for purifying waste oil,
a) Thermal cracking oil Waste oil and pyrolysis oil are introduced through an injection pipe connected to the upper side of the preheating reactor and preheated at a temperature of 250 to 350 ° C to convert diesel, kerosene and gasoline oil contained in waste oil and pyrolysis oil into vapor ;
b) The vaporized oil, kerosene and gasoline oil vapor generated in the pyrolysis oil preheating reactor in step a) are discharged through a pipe and sequentially introduced into a wax / dust remover and a diesel oil quick condenser, and the wax / And the pyrolysis oil in the vapor phase of the gas oil, the kerosene and the gasoline phase is introduced into the pyrolysis oil purification reactor at the lower side through the pipe and pyrolyzed;
c) The diesel oil, kerosene and gasoline phase oil which is pyrolyzed and discharged in the pyrolysis oil refining reactor of step b) is introduced into the upper wax / dust remover, and the temperature is adjusted to 350 to 400 ° C to adjust the wax And after the heavy oil is condensed, re-entering the lower oil purification reactor and pyrolyzing by reheating;
d) The vapor of the pyrolysis oil preheating reactor, the pyrolysis oil refining reactor, and the vapor of the wax / dust remover are introduced into the diesel oil rapid condenser through piping and rapidly cooled to produce a diesel oil vapor having a boiling point of 330 to 380 ° C To a diesel oil condenser lower hopper through a drain line communicated on one side thereof;
e) The diesel oil of the step d), which has a boiling point of 380 ° C. or lower, flows into the diesel oil condenser, and the diesel oil vapor having a boiling point of about 280 to 330 ° C. passes through the diesel oil condenser, Into the spiral cooler;
f) The liquid phase of the diesel oil introduced into the spiral cooler in step e) is cooled to room temperature and then flows into the diesel oil primary water separator through the level automatic regulating unit composed of an inverted U-shaped pipe, The oil and water are firstly separated by an oil separator, and the oil of the oil phase separated from the first water is introduced into the oil secondary oil water separator, and the oil and the oil of the oil phase are separated and separated by the precipitation / ;
g) The oil vapor of the kerosene phase discharged from the diesel oil condenser in the step e) is introduced into the kerosene oil rapid condenser through the upper pipe and rapidly cooled to obtain a pyrolysis oil having a boiling point of 180 to 230 ° C Liquefying the vaporized vapor and then transferring the vaporized liquid to the lower hopper of the kerosene oil condenser through the drain pipe adjoined to the one side;
h) The vapor, which has a boiling point of 230 ° C or less and has flowed into the kerosene oil condenser of step g), passes through the kerosene oil condenser and liquefies the oil vapor of the kerosene phase having a boiling point of 180 to 230 ° C, Entering the spiral cooler;
i) The liquid phase of the kerosene phase introduced into the kerosene spiral cooler of step h) is cooled to room temperature and then flows into the diesel primary oil water separator via the level automatic regulating unit composed of an inverted U-shaped pipe, The oil and water are firstly separated by an oil separator. The oil of the kerosene phase separated from the first water is introduced into the lower kerosene secondary oil water separator, and the oil and kerosene oil are separated by the precipitation / separation method by gravity. So as to be separated;
j) The oil vapor of the gasoline state discharged in a vapor state in the kerosene oil condenser of the step h) is transferred through the pipe and flows into the gasoline oil rapid condenser and rapidly cooled to produce a pyrolysis oil having a boiling point of 110 to 180 ° C Causing the vapor to liquefy and then to be delivered to the bottom hopper of the gasoline oil condenser through a drain line communicated to the one side;
k) The non-condensable gas is discharged through the upper pipe while passing through the gasoline oil condenser of the step j), and the oil vapor of the gasoline phase having a boiling point of 30 to 180 ° C. is liquefied and flows into the gasoline spiral cooler through the lower hopper ; And
l) The liquid phase of the gasoline phase introduced into the gasoline spiral cooler of step k) is cooled to room temperature and then flows into the first oil-water separator through the water level automatic regulating unit composed of an inverted U- The oil and water are firstly separated by a multi-stage oil-water separator. The oil of the gasoline phase separated from the first water is introduced into the second oil-water separator of the gasoline, so that the oil and oil of the gasoline- And separating the waste water from the waste water.
The method for purifying waste oil according to claim 1, wherein the waste oil and pyrolysis oil preheated in the pyrolysis oil preheating reactor in step a) are preheated for 2 to 3 hours.
The method according to claim 1,
Wherein the waste oil and the pyrolysis oil crude oil in the light oil, kerosene, and petroleum-derived oil vapor introduced into the pyrolysis oil purification reactor of the step b) are pyrolyzed by heating at 450 to 500 ° C.
The method for purifying waste oil according to claim 1, wherein the wax / dust remover of step (c) comprises injecting steam at a lower side thereof to induce hydrogenation reaction.
The method for purifying waste oil according to claim 1, wherein the diesel oil pyrolysis oil at room temperature is injected into the upper portion of the diesel oil rapid condenser in step (d) to rapidly cool the vapor introduced into the diesel oil rapid condenser .
The method according to claim 1, wherein the kerosene oil rapid condenser in step g) is sprayed with pyrolysis oil on a kerosene phase at room temperature to rapidly cool the vapor on the kerosene phase flowing through the pipe, Refining method.
The method for purifying waste oil according to claim 1, wherein the petroleum oil rapid condenser in step j) is sprayed with pyrolysis oil of gasoline phase at room temperature to rapidly cool the vapor phase of the gasoline phase flowing through the pipe .
The method of claim 1, wherein the non-condensable gas discharged upward from the gasoline oil condenser in step k) is transferred to a non-condensable gas scrubber on one side thereof through a pipe, scrubbed with cleaning water, And removing condensable oil mist, tar, and other impurities in the waste oil.
The method as claimed in claim 8, wherein a gas scrubber oil separator is disposed below the non-condensable gas scrubber, and the condensable oil mist, tar and other impurities in the rinse water are subjected to oil separation and recirculated to the pyrolysis oil pre- And then pyrolyzing the waste oil again.
In a waste oil purification system,
A pyrolysis oil preheater 110 for introducing waste oil and pyrolysis oil through an injection pipe 111 installed at one side of the pyrolysis furnace and preheating the pyrolysis oil to a predetermined temperature;
The oil vapor of the pyrolysis oil preheating reactor 110 is connected to the oil pipeline P through which the oil vapor of the gas oil, kerosene, and gasoline is transferred to remove wax / dust in the oil vapor of the gas oil, kerosene, A wax / dust remover 120;
A pyrolysis oil purification reactor 100 communicated with the lower side of the wax / dust remover 120 so as to condense and liquefy wax and heavy oil having a boiling point above a predetermined temperature in the oil vapor of the wax / );
The oil vapor in the vapor state of the vapor state in which the vapor of the pyrolysis oil preheating reactor 110 and the vapor of the pyrolysis oil refining reactor 100 are introduced via the pipe P through the wax / An oil-oil-quick condenser 130 for circulating the oil;
An oil-in-oil condenser 140 which is communicated with one side of the diesel oil rapid condenser 130 through a drain pipe 131 and communicates with the lower hopper 141;
A spiral cooler 142 for cooling the oil on the diesel oil condition and a water level automatic adjustment unit 143 formed below the diesel oil condenser 140 and composed of an inverted U-shaped pipe;
A primary oil water separator 144 communicating in sequence below the level automatic regulating unit 143 for primarily separating oil and water and a diesel oil secondary oil separator 144 separating the oil on the oil- (145);
A kerosene oil rapid condenser 150 which is interposed between the diesel oil condenser 140 and the piping P to rapidly cool the oil vapor on the kerosene phase in an incoming steam state;
A kerosene oil condenser 160 communicated with the lower hopper 161 via a drain pipe 151 at one side of the kerosene oil quick condenser 150;
A spiral cooler 162 for cooling the kerosene oil and a water level automatic control unit 163 disposed below the kerosene oil condenser 160 for cooling the kerosine oil and having an inverted U-shaped pipe;
A primary oil water separator 164 which is communicated sequentially below the water level automatic regulating unit 163 to primarily separate oil and water and a diesel oil secondary oil separator 164 in which oil on the kerosene phase is secondarily separated by precipitation / (165);
A gasoline oil rapid condenser 170 interposed between the kerosene oil condenser 160 and the pipe P for rapidly cooling the oil vapor in the vapor state of the flowing vapor;
A gasoline oil condenser 180 communicated with the lower hopper 181 through a drain pipe 171 at one side of the gasoline oil rapid condenser 170;
A spiral cooler 182 for cooling the oil of the gasoline phase and a water level automatic adjustment unit 183 disposed below the gasoline oil condenser 180 and having an inverted U-shaped pipe;
A first oil-water separator 184 communicating with the lower side of the water level automatic regulating unit 183 in order and separating the oil and moisture from the oil, and a second oil-water separator 184 separating oil from the oil- (185). ≪ / RTI >
The non-condensable gas scrubber (190) according to claim 10, wherein a non-condensable gas is introduced into the gasoline oil condenser (180) via a pipe (P) to scrub the condensable oil mist, tar, wherein a gas scrubber is communicated in communication.
12. The refining system for waste oil according to claim 11, wherein a gas scrubber oil water separator (200) is communicated under the non-condensable gas scrubber (190).
13. The refinery system of claim 12, wherein the gas scrubber oil water separator (200) is connected to the pyrolysis oil preheater (110) so that condensable oil mist, tar and other impurities are recirculated.

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