KR20140098953A - Method for Purifying Pyrolysis Oil from Waste Comprising Hydrocarbon - Google Patents

Method for Purifying Pyrolysis Oil from Waste Comprising Hydrocarbon Download PDF

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Publication number
KR20140098953A
KR20140098953A KR1020130011426A KR20130011426A KR20140098953A KR 20140098953 A KR20140098953 A KR 20140098953A KR 1020130011426 A KR1020130011426 A KR 1020130011426A KR 20130011426 A KR20130011426 A KR 20130011426A KR 20140098953 A KR20140098953 A KR 20140098953A
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South Korea
Prior art keywords
hydrocracking
oil fraction
catalyst
heavy oil
hydrocarbon
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KR1020130011426A
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Korean (ko)
Inventor
이용걸
윤광남
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단국대학교 산학협력단
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Priority to KR1020130011426A priority Critical patent/KR20140098953A/en
Publication of KR20140098953A publication Critical patent/KR20140098953A/en

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    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
    • C10G1/10—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal from rubber or rubber waste
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G45/00—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds
    • C10G45/02—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing
    • C10G45/04—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing characterised by the catalyst used
    • C10G45/06—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing characterised by the catalyst used containing nickel or cobalt metal, or compounds thereof
    • C10G45/08—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing characterised by the catalyst used containing nickel or cobalt metal, or compounds thereof in combination with chromium, molybdenum, or tungsten metals, or compounds thereof
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G65/00—Treatment of hydrocarbon oils by two or more hydrotreatment processes only
    • C10G65/02—Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only
    • C10G65/12—Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only including cracking steps and other hydrotreatment steps
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/10—Feedstock materials
    • C10G2300/1003—Waste materials

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  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Wood Science & Technology (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)

Abstract

A method for pyrolysis and purification of hydrocarbon-containing wastes is provided. Separate the pyrolysis oil of hydrocarbon-containing waste into a light oil fraction and a heavy oil fraction. The light oil fraction is hydrolyzed using a first hydrocracking catalyst. The heavy oil fraction is hydrocracked using a second hydrocracking catalyst at a lower liquid space velocity than the hydrocracking process of the light oil fraction.

Description

FIELD OF THE INVENTION [0001] The present invention relates to a method for purifying pyrolysis oil,

The present invention relates to an oil refining method, and more particularly, to a hydrocarbon refining waste pyrolysis oil refining method.

Recent interest in recycling resources has increased the importance of technology for recovering usable materials from waste. As an example of waste containing hydrocarbons, waste tires are a typical source of pollution of air, soil and water by about 1.6 billion pieces per year worldwide.

These waste tires are mainly used as landfill or asphalt substitutes after crushing, but this also causes secondary environmental pollution. To solve this problem, Korean Patent Publication No. 2002-0010633 discloses a method for recovering oil from waste tires. However, the oil recovered from the waste tire contains significant amounts of sulfur (1-3 wt%) and a certain amount of nitrogen (<0.5 wt%), which can cause corrosion or erosion of equipment in addition to environmental pollution. Therefore, utilization of the oil recovered from the waste tire as fuel is extremely limited.

DISCLOSURE Technical Problem The present invention provides a method for purifying hydrocarbon-containing waste thermal cracking oil in which the content of sulfur and nitrogen is greatly reduced.

According to an aspect of the present invention, there is provided an apparatus for pyrolysis and hydrocracking of a hydrocarbon-containing waste. Separate the pyrolysis oil of hydrocarbon-containing waste into a light oil fraction and a heavy oil fraction. The light oil fraction is hydrolyzed using a first hydrocracking catalyst. The heavy oil fraction is hydrocracked using a second hydrocracking catalyst at a lower liquid space velocity than the hydrocracking process of the light oil fraction.

The liquid space velocity for hydrolyzing the heavy oil fraction may be 0.3 to 0.7 times the liquid space velocity for hydrolyzing the light oil fraction. As an example, the liquid space velocity for hydrolyzing the heavy oil fraction may be 0.5 to 1 hr &lt; -1 &gt;. The hydrogen flow rate for hydrocracking the heavy oil fraction may be slower than the hydrogen flow rate for hydrocracking the light oil fraction have. In particular, the hydrogen flow rate for hydrocracking the heavy oil fraction may be 0.1 to 0.6 times the hydrogen flow rate for hydrocracking the light fuel fraction. As an example, the hydrogen flow rate for hydrocracking the heavy oil fraction may be 100-500 ccm.

The second hydrocracking catalyst may contain more active phase than the first hydrocracking catalyst. The first hydrocracking catalyst and the second hydrocracking catalyst may be a transition metal sulfide catalyst or a transition metal phosphide catalyst regardless of each other. The transition metal sulfide catalyst may comprise at least one catalyst selected from the group consisting of MoS 2 , Ni-MoS 2 , Ni-WS 2 and Co-MoS 2 . The transition metal phosphide catalyst may comprise at least one catalyst selected from the group consisting of Ni2P, Co2P, Fe2P, MoP and WP.

In order to accomplish the above object, one aspect of the present invention provides another example of a method for pyrolysis and hydrocracking of a hydrocarbon-containing waste. Separate the pyrolysis oil of hydrocarbon-containing waste into a light oil fraction and a heavy oil fraction. The light oil fraction is hydrolyzed using a first hydrocracking catalyst. The heavy oil component is hydrocracked using a second hydrocracking catalyst containing more active phase than the first hydrocracking catalyst.

According to embodiments of the present invention, the heavy oil fraction containing a large amount of nitrogen and a polycyclic ring compound in addition to sulfur can be hydrolyzed at a low liquidus space velocity as compared with the hydrocracking process of the light oil fraction. In this case, various competing reactions such as hydrode- sulfation (HDS), hydrodenitrogenation (HDN), and poorly decomposable sulfide decomposition reaction such as polycyclic ring compound can be easily carried out all at once, The residual content can be effectively reduced.

FIG. 1 is a schematic view illustrating a method of pyrolysis and hydrocracking of a hydrocarbon-containing waste according to an embodiment of the present invention.
Fig. 2 is a graph showing the boiling point of the light oil fraction, and Fig. 3 is a graph showing the components of the light oil fraction.
FIG. 4 is a graph showing the boiling point of the heavy oil component, and FIG. 5 is a graph showing the components of the heavy oil component.
6 is a graph showing the sulfur content of the effluent discharged in Experimental Example 1 with respect to the reaction time. 7 is a graph showing the components of the effluent before the reaction and 19 hours after the reaction in Experimental Example 1. FIG.
8 is a graph showing the hydrogenation desulfurization conversion rate according to the change of the liquid phase space velocity and the hydrogen flow rate in Experimental Example 2. FIG.
FIG. 9 is a graph showing the components of the effluent after the reaction in the reaction conditions of Experimental Example 2, that is, the heavy hydrocarbon fraction before the reaction, the liquid phase space velocity is 0.5 hr -1, and the hydrogen flow rate is 100-500 ccm.

Hereinafter, preferred embodiments of the present invention will be described in detail with reference to the accompanying drawings. However, the present invention is not limited to the embodiments described herein but may be embodied in other forms. Like reference numerals designate like elements throughout the specification.

FIG. 1 is a schematic view illustrating a method of pyrolysis and hydrocracking of a hydrocarbon-containing waste according to an embodiment of the present invention.

1, a hydrocarbon-containing waste pyrolysis oil 11 may be provided. The hydrocarbon-containing waste may be pulverized waste rubber such as waste tires. Such hydrocarbon-containing waste can be pyrolyzed to obtain pyrolysis oil. Pyrolysis of the hydrocarbon-containing waste may be a hypoxic indirect heating process. In this case, pyrolysis is carried out at a temperature of about 400 to 600 ° C, so that combustion reaction hardly occurs and generation of secondary pollutants is small.

The hydrocarbon-containing waste pyrolysis oil 11 may be introduced into the still. The hydrocarbon-containing waste pyrolysis oil (11) can be separated into the light oil fraction (13) and the heavy oil fraction (12) in the still apparatus (10). The bottom effluent 19 of the still 10 can be disposed of. The distiller 10 may be an atmospheric distillation unit. The light oil fraction (13) and the heavy oil fraction (12) mean oil fraction having a low boiling point and oil fraction having a high boiling point, respectively, based on the selected boiling point. The selected boiling point may be about 100 to 500 &lt; 0 &gt; C. The light oil fraction 13 may have a boiling point of about 100 to 330 캜 and the heavy oil fraction 12 may have a boiling point of about 330 to 500 캜.

Fig. 2 is a graph showing the boiling point of the light oil fraction, and Fig. 3 is a graph showing the components of the light oil fraction.

Referring to FIG. 2, it can be seen that the light oil fraction is mostly vaporized at 180 ° C or lower. Also, referring to FIG. 3, it can be seen that the component of the light oil component shows about 6,700 ppm S of sulfur, and the sulfide of the BT (BenzoThiophene) series occupies almost the majority.

FIG. 4 is a graph showing the boiling point of the heavy oil component, and FIG. 5 is a graph showing the components of the heavy oil component.

Referring to FIG. 4, it can be seen that most of the heavy oil component is vaporized at 350 ° C. or lower. Also, referring to FIG. 5, the components of the heavy oil component were found to be about 14,500 ppm S of sulfur and about 4070 ppm N of nitrogen. Also, polycyclic ring compounds having three or more rings such as DBT (DiBenzoThiophene), 4MDBT (4-MethylDiBenzoThiophene) and 46DMDBT (4,6-DiMethylDiBenzoThiophene)

Referring again to FIG. 1, light oil fraction 13 may be introduced into a first hydrocracking unit 30 having a first hydrocracking catalyst. The heavy oil fraction 12 may also be introduced into a second hydrocracking unit 20 having a second hydrocracking catalyst. As described above, since the heavy oil 12 contains a large amount of nitrogen and a polycyclic ring compound compared with the light oil fraction 13, the second hydrocracking apparatus 20 can not compete with the hydrodesulfurization (HDS) Decomposition sulfide decomposition reaction such as hydrodenitrogenation (HDN) and a polycyclic ring compound can proceed together.

 The first hydrocracking catalyst and the second hydrocracking catalyst may be a transition metal sulfide catalyst or a transition metal phosphide catalyst regardless of each other. However, the second hydrocracking catalyst contains more active phase than the first hydrocracking catalyst and can also have a high degree of dispersion. Thus, the first hydrocracking catalyst may be lower than the second hydrocracking catalyst. In this case, various competitive reactions in the second hydrocracking apparatus 20 can be easily conducted at once.

Here, the transition metal sulfide catalyst may comprise at least one catalyst selected from the group consisting of MoS 2 , Ni-MoS 2 , Ni-WS 2 and Co-MoS 2 . The transition metal phosphide catalyst may comprise one or more catalysts selected from the group consisting of Ni2P, Co2P, Fe2P, MoP and WP. The first hydrocracking catalyst and the second hydrocracking catalyst may be provided supported on the catalyst support. Catalyst support is silica-alumina (SiO 2 -Al 2 O 3) , alumina (Al 2 O 3) specifically γ- alumina, zinc oxide (ZnO), zirconia (ZrO 2), ceria (CeO2), silica (SiO 2) Zeolite, zeolite, mesoporous silica, clay, USY zeolite, saponite, and titania (TiO 2 ).

The second hydrocracking unit 20 may have a lower LHSV than the first hydrocracking unit 30. [ As an example, the liquid phase space velocity of the second hydrocracking apparatus 20 may be 0.3 to 0.7 times, specifically 0.5 times as much as that of the first hydrocracking apparatus 30. In addition, the second hydrocracking unit 20 may have a lower H2 flow rate than the first hydrocracking unit 30. [ As an example, the hydrogen flow rate in the second hydrocracking equipment 20 may be 0.1 to 0.6 times, specifically 0.2 times as high as that of the first hydrocracking equipment 30. [ In this case, various competitive reactions in the second hydrocracking equipment 20 can be easily performed at once, and the residual amount of sulfur in the effluent from the second hydrocracking equipment 20 can be effectively reduced.

The reaction conditions of the first hydrocracking apparatus 20 and the second hydrocracking apparatus 30 may be as follows.

catalyst Reaction temperature pressure LHSV H 2 flow rate The first hydrocracking equipment
(Light oil refining) Ni-MoS 2 series 350 ℃ 30 atm 1 to 2 hr -1 500ccm / min Second hydrocracking equipment
(Heavy oil refining) Ni-MoS 2 series 350 ℃ 30 atm 0.5 to 1 hr -1 50 to 500ccm / min

The effluent 34 of the first hydrocracking unit 30 and the effluent 24 of the second hydrocracking unit 20 may be introduced into the still 40. At this time, the effluents 34, 24 may be mixed 44 and introduced into the still 40. The effluents 34 and 24 introduced into the still 40 can be separated into an aromatic compound (BTX) 45 such as benzene, toluene and xylene and a fuel oil 47 such as gasoline and diesel. At this time, the aromatic compound 45 flowing out of the still 40 and the fuel oil 47 may contain not more than 1000 ppm of sulfur. On the other hand, the effluent 42 from the bottom of the still 40 can be recycled to the second hydrocracker 20. At this time, the effluent (42) may be mixed with the heavy oil fraction (12) exiting the distiller (10).

Hereinafter, exemplary embodiments of the present invention will be described in order to facilitate understanding of the present invention. It should be understood, however, that the following examples are intended to aid in the understanding of the present invention and are not intended to limit the scope of the present invention.

[Experimental Examples; Examples]

Experimental Example 1: Purification of light oil fraction

Ni-MoS 2, while the catalyst remains a hydrogenated separation device disposed in a 350 degrees and 30atm pressure, a light oil minutes and flowing at a space velocity of 0.5 hr -1 was also introduced hydrogen to 500 ccm / min, 4 hours, 10 hours, 15 hours, 19 hours, 21 hours and 24 hours, respectively, and the sulfur content in each effluent was measured.

6 is a graph showing the sulfur content of the effluent discharged in Experimental Example 1 with respect to the reaction time. 7 is a graph showing the components of the effluent before the reaction and 19 hours after the reaction in Experimental Example 1. FIG.

Referring to FIG. 6, after about 10 hours of reaction, the sulfur content of the effluent can be lowered to 1000 ppm or less, and the fuel oil meeting the standard can be obtained.

7, after the reaction, the sulfur-containing aromatic compounds such as BT (BenzoThiophene), DBT (DiBenzoThiophene), 4MDBT (4-MethylDiBenzoThiophene) and 46DMDBT (4,6-DiMethylDiBenzoThiophene) It can be seen that all can be removed.

Experimental Example 2: Purification of heavy oil fraction

The hydrogenolysis apparatus in which the Ni-MoS 2 catalyst was placed was fed at a space velocity of 0.5 hr -1 or 1 hr -1 while keeping the temperature of 350 ° C. and the pressure of 30 atm, and hydrogen was supplied at 100, 300, or 500 ccm / min. After reacting for 20 hours under each reaction condition, the sulfur content in the effluent was measured.

8 is a graph showing hydrogenation desulfurization conversion rates according to changes in liquid phase space velocity and hydrogen flow rate in Experimental Example 2. FIG.

Referring to FIG. 8, it can be seen that the lower the liquid phase space velocity and the lower the hydrogen flow rate, the greater the hydrogen desulfurization conversion rate and the lower the residual sulfur content in the effluent. In particular, it can be seen that when the liquid space velocity is 0.5 hr -1 and the hydrogen flow rate is 100 ccm, the residual sulfur content is reduced to less than 1000 ppm, which satisfies the standard.

9 is a graph showing the components of the effluent after the reaction in the reaction conditions of Experimental Example 2, that is, the heavy hydrocarbon fraction before the reaction, the liquid phase space velocity is 0.5-1.0 hr -1 and the hydrogen flow rate is 100ccm-500ccm.

9, almost all of the sulfur-containing aromatic compounds such as BT (BenzoThiophene), DBT (DiBenzoThiophene), 4MDBT (4-MethylDiBenzoThiophene) and 46DMDBT (4,6-DiMethylDiBenzoThiophene) It can be seen that it has been removed.

While the present invention has been particularly shown and described with reference to exemplary embodiments thereof, it is to be understood that the invention is not limited to the disclosed exemplary embodiments, but, on the contrary, This is possible.

Claims (11)

Separating the pyrolysis oil of the hydrocarbon-containing waste into a light oil fraction and a heavy oil fraction;
Hydrolyzing the light oil fraction using a first hydrocracking catalyst; And
And hydrocracking the heavy oil fraction using a second hydrocracking catalyst at a lower liquid space velocity than the hydrocracking process of the light oil fraction. The method according to claim 1,
Wherein the liquid space velocity for hydrocracking the heavy oil fraction is 0.3 to 0.7 times the liquid space velocity for hydrocracking the light oil fraction. The method according to claim 1 or 2,
Wherein the liquid phase space velocity for hydrocracking the heavy oil is 0.5 to 1 hr &lt; -1 &gt;. The method according to claim 1,
Wherein the hydrogen flow rate for hydrocracking the heavy oil fraction is slower than the hydrogen flow rate for hydrocracking the light oil fraction. The method of claim 4,
Wherein the hydrogen flow rate for hydrocracking the heavy oil fraction is 0.1 to 0.6 times the hydrogen flow rate for hydrocracking the light oil fraction. The method of claim 4,
Wherein the hydrogen flow rate for hydrocracking the heavy oil fraction is 100 to 500 ccm. The method according to claim 1,
Wherein the second hydrocracking catalyst contains more active phase than the first hydrocracking catalyst. The method of claim 7,
Wherein the first hydrocracking catalyst and the second hydrocracking catalyst are a transition metal sulfide catalyst or a transition metal phosphide catalyst regardless of each other. The method of claim 8,
The transition metal sulfide catalyst, MoS 2, Ni-MoS 2, Ni-WS 2 and MoS 2 Co-hydrocarbon-containing waste pyrolysis oil refining method comprising at least one catalyst selected from the group consisting of. The method of claim 8,
Wherein the transition metal phosphide catalyst comprises at least one catalyst selected from the group consisting of Ni2P, Co2P, Fe2P, MoP and WP. Separating the pyrolysis oil of the hydrocarbon-containing waste into a light oil fraction and a heavy oil fraction;
Hydrolyzing the light oil fraction using a first hydrocracking catalyst; And
And hydrocracking the heavy oil using a second hydrocracking catalyst containing more active phase than the first hydrocracking catalyst.
KR1020130011426A 2013-01-31 2013-01-31 Method for Purifying Pyrolysis Oil from Waste Comprising Hydrocarbon KR20140098953A (en)

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Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
KR20200070840A (en) 2018-12-10 2020-06-18 한화토탈 주식회사 Apparatus for processing condensate comprising installed side stripper on stabilizer column for condensate fractionator overhead processing
WO2023096379A1 (en) * 2021-11-26 2023-06-01 Sk Innovation Co., Ltd. Refining apparatus and refining method of waste plastic pyrolysis oil

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
KR20200070840A (en) 2018-12-10 2020-06-18 한화토탈 주식회사 Apparatus for processing condensate comprising installed side stripper on stabilizer column for condensate fractionator overhead processing
WO2023096379A1 (en) * 2021-11-26 2023-06-01 Sk Innovation Co., Ltd. Refining apparatus and refining method of waste plastic pyrolysis oil

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