KR100191075B1 - Apparatus and process for waste vinyl into gasoline and diesel oil - Google Patents

Abstract

The present invention relates to a method for producing gasoline and diesel oil using waste vinyl to produce gasoline and diesel oil that is currently used as main energy from waste vinyl that is almost impossible to recycle, and a dissolution tank. Distilled purified mixture obtained by dissolving the mixed vinyl system obtained by dissolving and cranking the waste vinyl raw material in a low pressure gas separation column into a mixed oil and a gas, and extracting and washing the mixed oil by applying a reagent in an extraction column. Diesel and gasoline are produced through the process of rectifying and rectifying. As a result, it is possible to produce pure gasoline and diesel oil with high yield, and there is no sulfur component, high octane number, and no energy pollution due to manufacturing.

Description

Method for producing gasoline and diesel oil using waste vinyl and its apparatus

The present invention relates to a method for producing gasoline and diesel oil using waste vinyl and a device for producing gasoline and diesel oil from waste vinyl that is almost impossible to recycle.

In today's world, energy resources are gradually being depleted due to limited resources, increased population, and accelerated consumption. Also, a large amount of waste is generated through various production and consumption activities, causing serious environmental pollution.

In particular, waste vinyl is less recycled and most of it is disposed of as trash, so it takes a long time to decay into a natural state. Therefore, countermeasures are required, and at the same time, development of new energy to replace limited petroleum energy is required. It is becoming.

Accordingly, the present invention has been made in response to the above requirements, and an object of the present invention is to produce waste gas, styropol, and the like (hereinafter referred to as waste vinyl) through a predetermined chemical reaction process to produce gasoline and diesel oil with high yields. The present invention provides a method and apparatus for producing gasoline and diesel oil using waste vinyl to prevent environmental pollution due to waste vinyl and to obtain and utilize energy.

1 is a block diagram of a manufacturing apparatus of the present invention.

2 is a manufacturing process block diagram of the present invention.

* Explanation of symbols for main parts of the drawings

11: melting tank 12, 19: cooler

13: low pressure gas separation tower 14: extraction tower

15: reagent injection unit 16: circulation pump

17: distillation tank 18: rectification tower

20: gasoline flow tower 21: flow pump

22, 23: diesel storage tank 24: gasoline storage tank

25: water seal 26: net safety device

27: diesel oil feed pump C1 ~ C3: coke

In order to achieve the above object, the present invention comprises a pre-treatment process step of pulverizing the prepared waste vinyl and removing the water contained in the pulverized waste vinyl raw material; A dissolution process step of dissolving the spent vinyl raw material in a state in which the heavy oil serving as the solvent is preheated in the dissolution tank 11; A cracking process step of generating a mixed gas in a gas state while gradually cracking and cracking the temperature of the waste vinyl solution obtained in the dissolution tank 11; A mixed oil separation process step of cooling the mixed gas in a gas state through a cooler (12) and passing the cooled mixed oil through a low pressure gas separation tower (13) to separate the mixed oil and a gas; In order to increase the effective ingredient of the separated mixed oil and obtain purified mixed oil, the mixed oil is fed to the extraction tower 14 and 98% of the concentrated acid (H ₂ SO ₄ ), which is about 1% of the mixed oil, to discharge the precipitate. After the addition of water, the mixture of water and sodium hydroxide (NaOH) diluted 1: 9 in the amount of about 10% of the mixed oil was added to the mixed oil of the active ingredient so that the precipitate could be discharged by washing water. An extraction process step of allowing purified water to be obtained by circulating and waiting for time and then adding washing water to discharge the washing water as a precipitate; The refined mixed oil is distilled by applying heat in a distillation tank, and then rectified by cooling to the rectification tower 18 to cool the diesel mixture and gasoline to obtain diesel oil and gasoline. It provides a method for producing gasoline and diesel oil.

In another aspect, the present invention is a device for realizing the above-described method for producing diesel oil and gasoline from waste vinyl, a dissolution tank (11) formed so as to be heatable to perform the heat dissolution and cracking decomposition reaction by inputting the crushed and washed waste vinyl raw material (11) ); A cooler (12) connected to the dissolution tank (11) in a pipe and cooling the mixed gas; A low pressure gas separation tower (13) for separating the mixed oil and the gas from the mixed liquid cooled by the cooler (12); An extraction tower 14 connected to the low pressure gas separation tower 13 to perform reagent treatment and water washing of the mixed oil; A distillation tank 17 connected to the extraction tower 14 and distilling purified mixed oil; A rectification tower 18 connected to the distillation tank 17 to separate the vaporized mixed gas into gasoline and diesel oil; A gasoline bunker tower 20 for returning a portion of the gasoline passing through the cooler 19 connected to the rectifier tower 18 to the rectifier tower 18; Diesel flow pump (27) and the low pressure gas to transfer the return gas 21 and the separated diesel oil to the diesel storage tank (22) 23 to flow the gasoline to the gasoline tower (20) Using waste vinyl, characterized in that it comprises a water column 25 and the net safety device 26 for collecting the gas generated in the separation tower 13, the extraction tower 14 and the gasoline flow tower 20 It provides a gasoline and diesel oil production apparatus.

Prior to the detailed description of the present invention will be described the principle of extracting gasoline and diesel oil from the waste vinyl which is the object of the present invention to achieve.

Waste vinyl is petroleum, and the gasoline, diesel and liquefied gas we use in our daily lives are also extracted from petroleum. The waste vinyl raw material is composed of a polymer having a large molecular weight, and its composition is composed of carbon and hydrogen, and gasoline and diesel oil produced by a refinery are relatively small in molecular weight, and its composition is also composed of carbon and hydrogen. Both of them have a common point that the molecules are all composed of carbon and hydrogen, the difference is that the waste vinyl material is a high molecular weight polymer compound and the molecular weight of gasoline and diesel oil is relatively small.

Accordingly, the waste vinyl raw material can be converted into gasoline, diesel oil, gas, etc. by changing the composition of the molecular weight. As a theoretical basis, the waste vinyl raw material can be regarded as solid petroleum having a very high molecular weight. It can be converted into oil composed of and gas.

Thermal cracking of alkane-based hydrocarbons leads to two types of basic reactions, one of which leaves the hydrogen and the other of which breaks the chain between carbon and carbon. Indicated.

◎ The equation of the reaction from which hydrogen is released

(상기 식에서 n=L+m)◎ The chemical equation that the chain between carbon is broken,

Where n = L + m

이 식에서 n은 알칸계 탄화수소의 탄소원자 갯수를 뜻한다.◎ The switching temperature (T1) when the hydrogen is released,

Where n is the number of carbon atoms in the alkane hydrocarbon.

The minimum value of T1 when n = 20 is T1 = 892K (about 620 ° C.).

이 식에서 m은 알켄계 탄화수소의 탄소원자 갯수를 뜻한다.When the chain between carbon and carbon is broken, the conversion temperature (T2) is

Where m is the number of carbon atoms in the alkene hydrocarbon.

if m = 19 then T2 = 512K (about 240 ° C.).

The above-described conversion point is described in detail. From the influence of temperature and the principle on the length hard function and the chemical reaction equilibrium constant, the following function can be obtained.

According to the above formula, when the temperature T is low, both ΔZ ₁ ⁰ and ΔZ ₂ ⁰ become integers, and when the temperature is constantly raised, the point where ΔZ ₁ ⁰ and ΔZ ₂ ⁰ become 0 (zero) is elapsed. Negative). In this case, the point where ΔZ ₁ ⁰ and ΔZ ₂ ⁰ become 0 is called a switching point, and the temperature at this time is called a conversion temperature of a chemical reaction.

As shown in the above two functional formulas, the larger the carbon number n and m of the hydrocarbon, the larger the values of ΔZ ₁ ⁰ and ΔZ ₂ ⁰ are passed to the larger absolute value, that is, the number of copies.

The larger the molecule of the hydrocarbon, the easier the reaction will proceed, even at relatively low temperatures. Accordingly, the molecular composition of the waste vinyl material is a polymer having a very high molecular weight composed of carbon and hydrogen elements, so that even when the waste vinyl raw material melts, the reaction of hydrogen is released and the reaction of breaking the chain between carbon and carbon is weak. The higher the temperature, the faster the two reaction rates described above.

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

1 is a block diagram of the manufacturing apparatus of the present invention, Figure 2 is a block diagram of the manufacturing process of the present invention.

EXAMPLE

Pretreatment Process Step

Firstly, the soil, cloth, and pieces of paper contained in the waste vinyl material. Various miscellaneous materials such as wire are removed by manual or semi-mechanical work. Next, the waste vinyl raw material is pulverized to form a small size. At this time, when the waste vinyl raw material has a circular shape, it is preferable to grind it to a size of 3-5 cm in diameter and a length and width of 3-5 cm in spherical shape. This is because the pulverization of waste vinyl raw materials is to facilitate the removal of fine miscellaneous materials such as sand or dust, and is easily dissolved in the dissolution tank because it is easy to transport and input and has a high heat absorption ability. The pulverized waste vinyl raw material is removed by sand or soil fine impurities by a non-limiting method such as centrifugation and washed with water.

Drying and Transfer Process Steps

Next, the waste vinyl raw material that has undergone the above process is dried, which can be performed by supplying hot air using a blower, but is not limited thereto and may be performed by other methods. After drying, the waste vinyl raw material is introduced into the dissolution tank 11 using a non-limiting apparatus capable of moving and injecting the waste vinyl raw material.

Dissolution and Cracking Reaction Process Step

Meanwhile, before the waste vinyl raw material is introduced into the melting tank 11, the heavy oil is first filled in an amount of 1/3 to 1/4 height so that the heat dissolution rate of the waste vinyl raw material is accelerated by the heat conduction action of the heavy oil. For sake.

In addition, all of the coke from the dissolution tank 11 to the export port of the water sealing pipe 25 should be opened before the heat is applied to the dissolution tank 11 after the input of the waste vinyl raw material. This is to prevent the generation of gas and gaseous mixed oils (hereinafter referred to as mixed oils) while the waste vinyl material is dissolved in the dissolution tank 11 while the (vinyl) waste vinyl material is decomposed. In other words, if each coke is not opened, the pressure of the dissolution tank 11 is increased, and there is a fear that the gas and the mixed organic gas flow out through the inlet through which the waste vinyl raw material is introduced and ignite.

When the heat is always added to the dissolution tank 11 and the temperature reaches 170 ° C. to 190 ° C., when the waste vinyl material is slowly added in an appropriate amount, the stirrer (not shown) is operated. At this time, due to the low liquid level of the heavy oil filled in the dissolution tank 11 and the difference in dissolution conditions, an appropriate amount of waste vinyl raw material should be initially introduced. Gradually, as the temperature of the dissolution tank 11 rises, the dissolution rate of the waste vinyl raw material is increased, and the level of the liquid is increased. When the liquid level of the waste vinyl material dissolved in the dissolution tank 11 reaches about 3/5 to 4/5, the input of the waste vinyl raw material is stopped, the inlet is sealed, and the temperature is slowly raised. In this waste vinyl raw material dissolution process, the dissolution temperature should not exceed 250 ℃.

When the cracking decomposition reaction of the waste vinyl raw material by slowly raising the temperature of the dissolution tank 11 as described above, the dissolution temperature must be controlled at a temperature between 260 ℃ and 360 ℃, if the temperature is too low decomposition target Cannot be reached or the reaction rate is too slow. In addition, if the dissolution temperature is too high, the product is polymerized again to form new large molecules, and the cracking reaction rate is very important and must be strictly deducted because the extraction speed does not increase even if the dissolution temperature is increased. After the reaction, the discharge coke at the bottom of the dissolution tank 11 is opened to discharge the residue.

Separation Process Step

After the cracking reaction, a mixed gas of the waste vinyl raw material contains a large amount of gas, and thus, it is necessary to separate it. For this purpose, the mixed fluid is formed by passing through the cooler 12 and mixed in the low pressure gas separation tower 13. Separate oil and gas. The double gas is introduced into the water sealing pipe 25 through a pipe drawing drawn out from the low pressure gas separation tower 13 in the drawing.

Extraction and processing

In addition, the mixed oil is introduced into the extraction tower 14 through another pipeline to perform the extraction process, which is to discard the invalid and unstable components of the mixed oil and to extract only the active ingredient to improve the quality of the product. to be. At this time, the two reagents are introduced into the extraction tower 14 from the reagent input unit 15 formed in the predetermined portion of the extraction tower 14, and the extraction process is performed in the extraction tower 14 in the level of the mixed oil in the extraction tower 14 When it is half the height, the mixed oil must be off the tubing and stored in another extraction column.

One of the two reagents used in the extraction process (hereinafter referred to as A reagent) is 98% concentrated acid (H ₂ SO ₄ ) using about 1% of mixed oil, and the other (hereinafter referred to as B reagent) Sodium hydroxide (NaOH) diluted with water and sodium hydroxide (NaOH) is 1: 9 ratio of sodium hydroxide (NaOH) and water, the B reagent is about 10% of the mixed oil.

Put the reagent A into the mixed oil filled in 1/2 to the extraction column 14, and open each coke of the circulation pipe, and stop the circulating pump 16 after operating for a predetermined time (about 4 hours) Wait for a while. And the discharge coke is installed in the bottom of the extraction tower 14 to discharge the precipitate.

Then, the reagent B is placed in the extraction tower 14, and the circulating pump is operated for a predetermined time as in the reagent A treatment, and the process is performed after the precipitate is discharged.

Next, clean water that is 1/2 of the mixed oil treated with the reagent is added to the extraction tower 14, and the circulating pump 16 is operated to wash for 4 to 6 hours. Then, after stopping the circulation pump 16, the air is allowed to stand for a predetermined time (4 to 6 hours), and then the discharge coke at the bottom of the extraction tower 14 is opened to discharge the precipitate and the washing water again. This washing process is preferably performed about two times to obtain a mixed oil purified by such a process.

At this time, the residual gas in the extraction tower 14 that is not completely separated from the low pressure gas separation tower 13 is introduced into the water sealing pipe 25 again.

Distillation and Rectification Process Steps

After the extraction process as described above, the coke between the extraction tower 14 and the distillation tank 17 is opened and the circulation pump 16 is operated to allow the mixed oil to flow into the distillation tank 17.

When the mixed oil refined into the distillation tank 17 is introduced, the temperature is gradually increased by applying heat to the distillation tank 17, wherein the height of the mixed oil filled in the distillation tank 17 exceeds 4/5 of the height of the total distillation tank. Do not do it. If this is exceeded, the mixed oil is not vaporized and the mixed oil in the mixed state of the liquid boils into the rectifying tower 18 directly through a pipe (oil pipe).

On the other hand, the bottom temperature of the distillation tank 17 is adjusted to be carried out at 350 ℃ ~ 370 ℃.

Rectification of the mixed oil formed in the rectification tower 18 is a task to determine the quality of the production oil and gasoline and diesel oil are separated. The temperature should be strictly deducted from the highest point of the tower, but the deduction temperature should not exceed 150 ℃. Such a temperature deduction is not sufficient only by the method of lowering the temperature of the distillation tank 17, so it must be performed in parallel with the cooling flow method described below.

▷ Cooling flow method

The gasoline separated from the rectification tower 18 is cooled through the cooler 19 and flows into the gasoline flow tower 20. The gasoline level in the gasoline flow tower 20 reaches 1/3 to 1/2. When the export coke (C2) and the import coke (C1) of the circulating pump 21 is opened and the circulating pump 21 is operated, the temperature of the rectification tower 18 is deducted by the cooled gasoline of the gasoline circulating tower 20. Done.

When deducting the temperature as the gas flow of gasoline, it is necessary to operate the imported coke of the circulating pump 21. Initially, the import amount of the circulating pump 21 is reduced to observe the temperature state, and if the temperature is further lowered at 150 ° C. Reducing the amount of imported by turning the imported coke of the mask reflow pump 21, if the temperature exceeds 150 ℃ by increasing the imported amount of imported coke of the recirculation pump 21 to lower the temperature of the top of the rectification tower (18) The temperature at the top is maintained at 150 ° C.

If the gas level of the gasoline filled in the gasoline flow tower 20 exceeds 1/2, the import coke C3 of the gasoline storage tank 24 is properly opened under the condition of guaranteeing the gasoline cooling flow and the return pump 21 Open the imported coke in moderation. As a result, the gasoline flow level of the gasoline flow tower 20 is 1/2 and the imported coke C3 and the flow pump 21 of the gasoline storage tank 21 until the temperature of the rectification tower 18 reaches a normal value. The import coke of C1 should be adjusted repeatedly.

The gas generated again in the gasoline flow tower 20 enters the water sealing tube 25 through a pipe. In the gasoline flow tower 20, some gasoline is returned to the rectification tower 18, and the other gas enters the gasoline storage tank 21.

In addition, the diesel oil separated from the rectification tower 18 is also cooled and then enters the diesel storage tanks 22 and 23. After deducting the temperature of the rectification tower 18 to 165 ° C, the coke of the diesel oil pipeline is To open and transfer the diesel oil to the diesel oil storage tanks 22 and 23 as the diesel oil transfer pump 27. At this time, it should be noted that the diesel coke pump 27 does not largely open the cork, but slowly opens so that diesel oil remains in the imported pipeline at all times. This is because the mixed oil comes out of the pipe.

On the other hand, the water level inside the water sealing pipe 25 where the gas generated in the low pressure gas separation tower 13, the extraction tower 14 and the gasoline flow tower 20 is collected should be 1/2 of the total height, and the net safety device (26) consists of three to four layers of densely fabricated nets. The operation of the water sealing tube 25 and the net safety device 26 is the same bar, the fire is ignited in the gas to prevent the explosion explosion through the gas extraction tube.

For reference, Table 1 and Table 2 show the experimental results of gasoline and diesel oil produced by the process of the present invention.

◇ Disassembly gasoline

◇ Decomposition diesel oil

As described above, in the present invention, the gasoline and diesel oils obtained from waste vinyl are 75% or more, and the remaining 25% of gas and carbon powder are extracted. Among the 75% of the mixed oils, gasoline is 45% and diesel oil is 55%. You can get it. Gasoline and diesel oil produced from the present invention has the advantage of not causing sulfur due to the sulfur content and is obtained by heating rather than combustion method, and has an effect of causing an increase in octane number due to the high content of explosive substances. .

Claims (6)

A pretreatment process step of pulverizing the prepared waste vinyl and removing moisture contained in the ground waste vinyl raw material; A dissolution process step of dissolving the spent vinyl raw material in a state in which the heavy oil serving as the solvent is preheated in the dissolution tank 11; A cracking process step of generating a mixed gas in a gaseous state by gradually cracking and cracking the temperature of the waste vinyl solution obtained in the dissolution tank 11; A mixed oil separation process step of cooling the mixed gas in the gas state through a cooler (12) and passing the cooled mixed oil through a low pressure gas separation tower (13) to separate the mixed oil and a gas; In order to increase the effective ingredient of the separated mixed oil and obtain a purified mixed oil, the mixed oil is fed to the extraction tower 14 and 98% of the concentrated acid (H ₂ SO ₄ ), which is about 1% of the mixed oil, to discharge the precipitate. After inputting the solution, a solution of dilute sodium hydroxide (NaOH) and water 1: 9 in a quantity of about 10% of the mixed oil is added to the mixed oil of the active ingredient so that the precipitate can be discharged by washing water. An extraction process step of allowing the purified mixed oil to be obtained by circulating the time and waiting and then inputting the washing water to discharge the washing water as a precipitate; The refined mixed oil is distilled by applying heat in a distillation tank, and then rectified by cooling to the rectification tower 18 to cool the diesel mixture and gasoline to obtain diesel oil and gasoline. Method of producing gasoline and diesel oil. According to claim 1, Dissolution in the dissolution process step is a waste oil in a state in which the heavy oil as a solvent is supplied to the height of 1/3 to 1/4 in the melting tank 11 and heated to a temperature of 170 ℃ ~ 180 ℃ Method for producing gasoline and diesel oil using waste vinyl, characterized in that the vinyl raw material was added and dissolved in the midstream. The cracking process step is characterized in that the cracking decomposition by gradually raising the temperature when the waste vinyl solution obtained in the dissolution step reaches a height of about 3/5 ~ 5/5 in the dissolution tank (11). Gasoline and diesel oil production method using waste vinyl. The gasoline and diesel oil production method using waste vinyl according to claim 1, wherein the temperature of the dissolution tank is adjusted at a temperature between 260 ° C and 360 ° C during the cracking process. The method of claim 1, wherein the bottom temperature of the distillation tank (17) during the distillation process step is carried out by adjusting between 350 ℃ ~ 370 ℃ gasoline and diesel oil production method using waste vinyl. Dissolving tank (11) formed so as to be heated so as to perform the thermal melting and cracking decomposition reaction by inputting the crushed and washed waste vinyl raw material; A cooler (12) connected to the dissolution tank (11) in a pipe and cooling the mixed gas; A low pressure gas separation tower (13) for separating the mixed oil and the gas from the mixed liquid cooled by the cooler (12); An extraction tower 14 connected to the low pressure gas separation tower 13 to perform reagent treatment and water washing of the mixed oil; A distillation tank 17 connected to the extraction tower 14 and distilling purified mixed oil; A rectification tower 18 connected to the distillation tank 17 to separate the vaporized mixed gas into gasoline and diesel oil; A gasoline bunker tower 20 for returning a portion of the gasoline passing through the cooler 19 connected to the rectifier tower 18 to the rectifier tower 18; Diesel flow pump (27) and the low pressure gas to transfer the return gas 21 and the separated diesel oil to the diesel storage tank (22) 23 to flow the gasoline to the gasoline tower (20) Using waste vinyl, characterized in that it comprises a water column 25 and the net safety device 26 for collecting the gas generated in the separation tower 13, the extraction tower 14 and the gasoline flow tower 20 Gasoline and diesel oil production equipment.

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