WO2010093135A2 - Stripping method using nitrogen - Google Patents

Stripping method using nitrogen Download PDF

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Publication number
WO2010093135A2
WO2010093135A2 PCT/KR2010/000565 KR2010000565W WO2010093135A2 WO 2010093135 A2 WO2010093135 A2 WO 2010093135A2 KR 2010000565 W KR2010000565 W KR 2010000565W WO 2010093135 A2 WO2010093135 A2 WO 2010093135A2
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Prior art keywords
nitrogen
oil
present
stripper
kgmole
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PCT/KR2010/000565
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French (fr)
Korean (ko)
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WO2010093135A3 (en
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백지우
유익상
남용원
김진의
송만규
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에스케이에너지 주식회사
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Priority to CN201080007260.1A priority Critical patent/CN102325862B/en
Publication of WO2010093135A2 publication Critical patent/WO2010093135A2/en
Publication of WO2010093135A3 publication Critical patent/WO2010093135A3/en

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    • A—HUMAN NECESSITIES
    • A47—FURNITURE; DOMESTIC ARTICLES OR APPLIANCES; COFFEE MILLS; SPICE MILLS; SUCTION CLEANERS IN GENERAL
    • A47K—SANITARY EQUIPMENT NOT OTHERWISE PROVIDED FOR; TOILET ACCESSORIES
    • A47K11/00—Closets without flushing; Urinals without flushing; Chamber pots; Chairs with toilet conveniences or specially adapted for use with toilets
    • 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
    • C10G11/00—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
    • C10G11/14—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts
    • C10G11/18—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts according to the "fluidised-bed" technique
    • A—HUMAN NECESSITIES
    • A47—FURNITURE; DOMESTIC ARTICLES OR APPLIANCES; COFFEE MILLS; SPICE MILLS; SUCTION CLEANERS IN GENERAL
    • A47K—SANITARY EQUIPMENT NOT OTHERWISE PROVIDED FOR; TOILET ACCESSORIES
    • A47K11/00—Closets without flushing; Urinals without flushing; Chamber pots; Chairs with toilet conveniences or specially adapted for use with toilets
    • A47K11/02—Dry closets, e.g. incinerator closets
    • A47K11/03—Dry closets, e.g. incinerator closets having means for adding powder, e.g. earth
    • A47K11/035—Dry closets, e.g. incinerator closets having means for adding powder, e.g. earth with chemical solvents
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/72—Treatment of water, waste water, or sewage by oxidation
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F9/00—Multistage treatment of water, waste water or sewage
    • E—FIXED CONSTRUCTIONS
    • E04—BUILDING
    • E04H—BUILDINGS OR LIKE STRUCTURES FOR PARTICULAR PURPOSES; SWIMMING OR SPLASH BATHS OR POOLS; MASTS; FENCING; TENTS OR CANOPIES, IN GENERAL
    • E04H1/00—Buildings or groups of buildings for dwelling or office purposes; General layout, e.g. modular co-ordination or staggered storeys
    • E04H1/12—Small buildings or other erections for limited occupation, erected in the open air or arranged in buildings, e.g. kiosks, waiting shelters for bus stops or for filling stations, roofs for railway platforms, watchmen's huts or dressing cubicles
    • E04H1/1205—Small buildings erected in the open air
    • E04H1/1216—Public W.C.s
    • 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
    • C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
    • C10G2400/04—Diesel oil
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
    • Y02W10/00—Technologies for wastewater treatment
    • Y02W10/10—Biological treatment of water, waste water, or sewage

Definitions

  • the present invention relates to the stripping of the oil produced in the middle stage of the main separation tower of oil refining and petrochemical plant, and more specifically, in the RFCC process, the product of the middle stage of the separation column is hardened by the partial pressure of nitrogen injected into the stripper. It relates to a method for removing oil and water.
  • Residue Fluid Catalyst Cracking is a process that produces gasoline feedstock through fluidized bed catalytic cracking from low sulfur fuel oil and low sulfur atmospheric pressure residue produced in heavy oil desulfurization.
  • the middle stage of the main separation tower of the FCC process produces the oil necessary for the blending of kerosene, diesel, etc., which is commonly referred to as a side cut.
  • the components of the sidecut fractions mainly include HCN and LCO fractions.
  • HCN heavy catalytic naphtha
  • LCO light cycle oil
  • Auxiliary separation towers for this purpose were a type using a reboiler, a vacuum stripping type, and a steam stripping type.
  • a side cut is introduced into the steam using separator 110 through a side cut introduction pipe 115 at an intermediate end of the main separator 100, and injected through the steam injection unit 115. Separation takes place by steam. Thereafter, the separated oil is introduced into the additional water separator 120 along the pipe 3 (119), and the separated water is discharged along the water discharge pipe 121 and the oil is removed from the water pipe 4 (123). Go through
  • U.S. Patent No. 4,606,816 and the like also disclose inventions related to the distillation of crude oil or separation using steam in auxiliary separators, and do not suggest ways to increase or improve the effects thereof.
  • the vacuum stripping type requires a lot of equipment, such as a vacuum equipment, a condenser, a receiver, a pump, etc., and thus has a problem of high cost.
  • the object of the present invention was to find that nitrogen is preferred as a suitable gas used to separate the products of the middle stage of the main separation tower in the auxiliary separator in the above FCC process, and in case of using nitrogen, To solve the problem and at the same time provide a way to lower the water to less than saturated water.
  • HCN and LCO having a boiling point of 180 ° C to 360 ° C is separated from the main separation column and then mixed with nitrogen gas before being mixed into the diesel product.
  • Another embodiment of the present invention is to provide an auxiliary separator using the method in an FCC process.
  • the present invention in comparison with the conventional method, there is no additional equipment other than the auxiliary separator, which is advantageous in terms of cost, and the above-mentioned effect is achieved only by connecting the nitrogen injection pipe when applied to the existing conventional auxiliary separator.
  • the advantage is that it is possible.
  • it is possible to reduce the moisture to below the saturation level at the same time as meeting the flash point specification in terms of efficiency, and solve the appearance problem fundamentally.
  • the oil can be directly blended into kerosene and diesel products.
  • FIG 1 shows that the steam stripper is used in the conventional FCC process.
  • Figure 2 shows a stripper using nitrogen in the FCC process.
  • main separator 105 side cut introduction tube
  • the side-cut oil produced at the intermediate stage of the main separator 100 is introduced into the nitrogen-using stripper 200 along the side-cut introduction tube 105.
  • Nitrogen is introduced into the nitrogen utilization stripper 200 along the nitrogen injection unit 201.
  • the injection pressure of nitrogen should be set higher than the stripper pressure so that nitrogen can be injected into the stripper sufficiently.
  • the pressure of the stripper may vary in each case, but is obvious to those skilled in the art. Nitrogen is then injected into the separator at the same point as the pressure inside the separator.
  • the injection amount of nitrogen ranges from 0.1 kgmole / m 3 (oil) to 0.4 kgmole / m 3 (oil), preferably 0.2 kgmole / m 3 (oil) to 0.3 kgmole / m 3 (oil).
  • the injection amount of nitrogen is less than 0.1 kgmole / m 3 (oil)
  • the nitrogen is excessive to the nitrogen
  • the light oil and water removed in the separator are returned back to the main separation column through pipe 2 (203).
  • the hard oil and the oil removed from the separator are sent to the storage tank along the pipe 1 (205).
  • the domestic diesel products usually have a flash point of 40 °C or more
  • the oil separated from the stripper has a flash point of 60 to 68 °C.
  • the appearance also satisfies B & C (Bright & Clear).
  • the appearance standard is judged by the naked eye, and is determined by selecting the most similar standard picture by comparing light with a standard sample by transmitting light through a transparent sample bottle. Standard photographs here are well known in the art and are classified into six grades: Bright & Clear, Slight Hazy, Hazy, Free Water, Sediment, and Suspended Solid.
  • the oil separated in the separator can be used for blending in kerosene and diesel products without additional water removal, unlike steam.
  • Table 1 compares the results of Example 1 with the state before stripping with nitrogen.
  • Example 2 The same implementation as in Example 1 was repeated except that the amount of nitrogen used was changed to 0.15 kgmole / m 3 (oil).
  • Example 2 The same run as in Example 1 was repeated except that 0.28 kgmole / m 3 (oil) of steam was used instead of nitrogen for the stripper.
  • Example 1 The results of Example 1 and Comparative Example 1 are shown in the following table.
  • the flash point was formed in a similar range, but it can be seen that the moisture content when using nitrogen is much smaller than using steam.
  • B & C is satisfied when nitrogen is used as compared to hazy.
  • the use of nitrogen does not require the addition of a water removal process additionally required in the use of steam, and also an additional process for satisfying the appearance is not required.
  • Example 1 was repeated in the same manner except that the nitrogen injection amount was 0.1 kgmole / m 3 (oil).
  • Example 1 was repeated in the same manner except that no nitrogen was injected.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Architecture (AREA)
  • Organic Chemistry (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • General Chemical & Material Sciences (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Hydrology & Water Resources (AREA)
  • Environmental & Geological Engineering (AREA)
  • Water Supply & Treatment (AREA)
  • Health & Medical Sciences (AREA)
  • Public Health (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Civil Engineering (AREA)
  • Structural Engineering (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
  • Fats And Perfumes (AREA)

Abstract

The present invention relates to a method for stripping oils, produced at the intermediate part of a main stripper in an FCC process, using nitrogen, to thereby meet the inflammation point and appearance standards. The method of the present invention meets the inflammation point and reduces moisture to a level lower than a saturation level, and thus prevents appearance problems. The method of the present invention enables easy adjustment of the inflammation point, thus enabling oils to be directly mixed with kerosene products and diesel products. Further, the method of the present invention eliminates the necessity of additional equipment, and can be applied to conventional separators by simply connecting a nitrogen injection pipe, thereby achieving significant economical advantages.

Description

질소를 이용한 스트리핑 방법Nitrogen Stripping Method
본 발명은 정유 및 석유 화학 공장의 주분리탑 중간단에서 생산된 유분의 스트리핑에 관한 것으로, 보다 구체적으로는 RFCC 공정에 있어서 분리탑 중간단의 생성물을 스트리퍼 하부에 주입된 질소의 분압에 의하여 경질 유분 및 수분을 제거하는 방법에 관한 것이다.The present invention relates to the stripping of the oil produced in the middle stage of the main separation tower of oil refining and petrochemical plant, and more specifically, in the RFCC process, the product of the middle stage of the separation column is hardened by the partial pressure of nitrogen injected into the stripper. It relates to a method for removing oil and water.
중질유 유동상촉매 분해공정(RFCC, Residue Fluid Catalystic Cracking)은 중질유 탈황공정에서 생산된 저유황 연료유와 저유황 상압 잔사유를 원료로 유동상 촉매분해를 통해 휘발유 원료 등을 생산하는 공정이다. FCC 공정의 주분리탑의 중간 단에서 등유, 디젤 등의 배합에 필요한 유분을 생산하는데, 이 유분을 일반적으로 사이드컷(side cut)이라고 한다. 사이드컷 유분의 성분은 주로 HCN 및 LCO 유분을 포함한다. 주분리탑에서 생산된 HCN(Heavy Catalytic Naphtha)유분과 LCO(Light Cycle Oil) 유분의 경우, 디젤의 제품에 배합용으로 사용하기 위해서는 인화점 및 외관 규격이 충족 되어야 한다. 인화점은, 국내 경유 제품의 경우 40 ℃ 이상이며, 외관은 B&C로 관리하고 있다. Residue Fluid Catalyst Cracking (RFCC) is a process that produces gasoline feedstock through fluidized bed catalytic cracking from low sulfur fuel oil and low sulfur atmospheric pressure residue produced in heavy oil desulfurization. The middle stage of the main separation tower of the FCC process produces the oil necessary for the blending of kerosene, diesel, etc., which is commonly referred to as a side cut. The components of the sidecut fractions mainly include HCN and LCO fractions. In the case of heavy catalytic naphtha (HCN) and light cycle oil (LCO) fractions produced in the main separation column, the flash point and appearance specifications must be met for use in blending diesel products. The flash point is over 40 ℃ for domestic diesel products, and the appearance is managed by B & C.
이를 위해 보조 분리탑(side stripper)에서 경질 유분 및 수분의 제거가 요구된다. 이를 위한 보조 분리탑으로는 통상적으로 리보일러(reboiler)를 이용하는 형식, 진공 스트리핑 형식, 스팀 스트리핑 형식이 있었다.This requires the removal of light oil and water in a side stripper. Auxiliary separation towers for this purpose were a type using a reboiler, a vacuum stripping type, and a steam stripping type.
일반적으로 가장 대표적으로 쓰이고 있는 스팀을 이용한 공정은. 도 1에서 보듯이 주분리기(100)의 중간 단에서 사이드컷(side cut)이 사이드컷도입관(115)을 통하여 스팀이용분리기(110)으로 도입되고, 스팀주입부(115)를 통하여 주입된 스팀에 의하여 분리가 일어난다. 이후 분리된 유분은 관3(119)을 따라 추가적인 수분분리기(120)로 도입되고 여기서 분리된 수분은 수분배출관(121)을 따라 배출되고 관4(123)로 수분이 제거된 유분이 도출되는 공정을 거친다. In general, the most commonly used process using steam. As shown in FIG. 1, a side cut is introduced into the steam using separator 110 through a side cut introduction pipe 115 at an intermediate end of the main separator 100, and injected through the steam injection unit 115. Separation takes place by steam. Thereafter, the separated oil is introduced into the additional water separator 120 along the pipe 3 (119), and the separated water is discharged along the water discharge pipe 121 and the oil is removed from the water pipe 4 (123). Go through
상기의 스팀 스트리핑 형식을 이용하는 경우에도, 인화점의 규격을 충족하는데 문제점이 없으나, 수증기의 주입으로 인하여 제품 내에 수분 함량이 높아지므로 외관이 흐리게 되는 문제점을 지고, 이러한 문제점의 해결을 위하여 추가적인 수분의 제거를 위한 장치, 예를 들어 Coalesver, Salt Drier 등을 설치하는 방법이 있으나, 효과에 비하여 과다한 설비가 필요하며 추가적인 비용의 부담이 있다.Even when using the above steam stripping type, there is no problem in meeting the specification of the flash point, but the water content in the product is increased due to the injection of water vapor has a problem that the appearance is blurred, the removal of additional moisture to solve this problem There is a method for installing a device for, for example, Coalesver, Salt Drier, etc., but there is an excessive cost compared to the effect and there is an additional cost.
미국 특허 제4,606,816호 등에서도 원유의 증류에 관한 공정에 대한 발명이나 보조 분리기에서 스팀을 이용한 분리만을 개시하고 있고, 이에 대한 효과의 증대나 개선 방안 등을 제시하지 않고 있다. U.S. Patent No. 4,606,816 and the like also disclose inventions related to the distillation of crude oil or separation using steam in auxiliary separators, and do not suggest ways to increase or improve the effects thereof.
리보일러 형식의 경우 인화점 조절 및 수분으로 인한 외관 문제는 해결이 가능하나, 리보일러 설치가 필요하고 리보일러의 적절한 열 매체가 없어 고온의 Heavy Oil을 열 매체로 사용하는 경우 리보일러의 파울링이 과도하게 되어 설비의 유지 및 보수에 시간과 비용의 문제가 있었다.In the case of the reboiler type, it is possible to solve the appearance problem caused by the flash point control and the moisture.However, if the reboiler needs to be installed and the reboiler does not have a suitable heat medium, the reboiler fouling may not be possible. Excessive, there was a problem of time and money in the maintenance and repair of equipment.
또한, 진공 스트리핑 형식은 진공 설비, 응축기, 리시버, 펌프 등의 많은 설비를 요하므로 고비용이라는 문제점이 있었다.In addition, the vacuum stripping type requires a lot of equipment, such as a vacuum equipment, a condenser, a receiver, a pump, etc., and thus has a problem of high cost.
이에 상술한 문제를 해결하기 위한 연구를 수행한 결과, 보조 분리기 하부에 질소를 주입하는 경우, 인화점 및 외관의 충족과 동시에 수분을 포화 수준 미만으로 낮추는 것이 가능함을 발견하였고, 본 발명은 이를 기초로 완성되었다. As a result of the research to solve the above problem, when nitrogen is injected into the lower portion of the auxiliary separator, it was found that it is possible to lower the moisture to less than the saturation level at the same time as satisfying the flash point and appearance, the present invention based on this It is finished.
따라서, 본 발명의 목적은 상기의 FCC 공정에 있어서 주분리탑 중간단의 생성물을 보조 분리기에서 분리하는데 사용되는 적합한 기체로서 질소가 바람직함을 발견하였고, 질소를 이용하여 경우 인화점 규격 총족 및 외관의 문제를 해결하고 동시에 수분을 포화 수분이하로 낮추는 방법을 제공하는 것에 있다.Accordingly, the object of the present invention was to find that nitrogen is preferred as a suitable gas used to separate the products of the middle stage of the main separation tower in the auxiliary separator in the above FCC process, and in case of using nitrogen, To solve the problem and at the same time provide a way to lower the water to less than saturated water.
상기 목적을 달성하기 위하여, 본 발명의 일 구체예에서는, FCC 공정에 있어서, 180℃ 내지 360℃의 비점을 갖는 HCN 및 LCO가 주분리탑에서 분리된 후 디젤 제품에 혼합되기 이전에 질소가스에 의하여, 경질 유분 및 수분을 제거시키는 단계를 포함하는 것을 특징으로하는 유분의 스트리핑 방법을 제공한다.In order to achieve the above object, in one embodiment of the present invention, in the FCC process, HCN and LCO having a boiling point of 180 ° C to 360 ° C is separated from the main separation column and then mixed with nitrogen gas before being mixed into the diesel product. Thereby, to provide a stripping method of the oil comprising the step of removing the hard oil and water.
본 발명의 다른 일 구체예는 FCC 공정에서 본 방법을 사용하는 보조 분리기를 제공하는 것이다.Another embodiment of the present invention is to provide an auxiliary separator using the method in an FCC process.
기타 본 발명의 구체예들의 상세한 사항은 이하의 상세한 설명에서 더 자세히 설명하도록 한다.Other details of embodiments of the invention will be described in more detail in the following detailed description.
본 발명에 따르면, 기존에 사용된 방법에 비하여, 보조 분리기 이외의 추가적인 설비가 없어 비용적인 면에서 유리함을 지니고, 기존의 통상적인 보조 분리기에 적용시 질소 주입 배관의 연결만으로 상기 언급한 효과를 달성하는 것이 가능하다는 이점이 있다. 질소를 사용하는 것이 비용이나 설비의 간소함 이외에도 효과적인 측면에서도 인화점 규격 충족과 동시에 수분을 포화 수준 미만으로 낮추는 것이 가능하여 외관 문제를 근본적으로 해결할 수 있으며, 인화점의 조절이 용이하여 중간단에서 분리된 유분을 등유 및 디젤 제품에 직배합을 가능케한다. According to the present invention, in comparison with the conventional method, there is no additional equipment other than the auxiliary separator, which is advantageous in terms of cost, and the above-mentioned effect is achieved only by connecting the nitrogen injection pipe when applied to the existing conventional auxiliary separator. The advantage is that it is possible. In addition to the cost and simplicity of using nitrogen, it is possible to reduce the moisture to below the saturation level at the same time as meeting the flash point specification in terms of efficiency, and solve the appearance problem fundamentally. The oil can be directly blended into kerosene and diesel products.
도 1은 종래의 FCC공정에서 스팀 스트리퍼가 사용된 것을 나타낸 것이다.Figure 1 shows that the steam stripper is used in the conventional FCC process.
도 2는 FCC 공정에서 질소가 사용된 스트리퍼를 나타낸 것이다.Figure 2 shows a stripper using nitrogen in the FCC process.
※도면의 주요 부분의 설명※ Explanation of main parts of drawing
100: 주분리기 105: 사이드컷 도입관100: main separator 105: side cut introduction tube
110: 스팀이용스트리퍼 115: 스팀주입부110: steam using stripper 115: steam injection unit
119: 관3 120: 수분분리기119: tube 3 120: water separator
121: 수분배출관 123: 관4121: water discharge pipe 123: pipe 4
200: 질소이용스트리퍼 201: 질소주입부200: nitrogen using stripper 201: nitrogen injection unit
205: 관1 203: 관2205: Tube 1 203: Tube 2
이하, 본 발명의 기술적 사상에 대하여 상세히 설명하기로 한다. Hereinafter, the technical spirit of the present invention will be described in detail.
본 발명의 일 구체예에 따르면, 스트리퍼에 질소를 주입하여 질소의 분압을 이용하여 경질 유분 및 수분을 동시에 제거할 수 있다. 본 발명의 일구체예인 도 2에서 개시된 바와 같이 주분리기(100)의 중간 단에서 생성된 사이드컷(side-cut) 유분은 사이드컷 도입관(105)을 따라 질소이용스트리퍼(200)에 도입된다. 질소는 질소 주입부(201)를 따라 질소이용스트리퍼(200)에 도입된다. 질소의 주입 압력은 질소가 스트리퍼에 충분히 주입될 수 있도록 스트리퍼 압력보다 높게 설정하여야한다. 스트리퍼의 압력은 각각의 경우마다 다를 수 있으나, 당업자에게 자명한 사항이다. 이후 질소는 분리기에 주입되어 주입된 지점에서 분리기 내부의 압력과 동일하게 된다. 이때 질소의 주입량의 범위는 0.1 kgmole/m3(oil) 내지 0.4 kgmole/m3(oil)이고, 바람직하게는 0.2 kgmole/m3(oil) 내지 0.3 kgmole/m3(oil)이다. 질소의 주입량이 0.1 kgmole/m3(oil) 이하인 경우, 질소의 분압에 의한 분리 효과가 미미해지는 문제점이 있고, 주입량이 0.4 kgmole/m3(oil) 이상인 경우는 질소가 과다하게되어 질소에 대한 비용이 과다해지는 문제점 및 주분리탑의 압축기가 과부하되는 등의 문제점을 지닌다. 분리기에서 제거된 경질 유분 및 수분은 관2(203)를 통하여 주분리탑으로 다시 회수된다. 상기 분리기에서 경질 유분과 수분이 제거된 유분은 관1(205)을 따라 저장탱크로 보내어진다. According to one embodiment of the present invention, by injecting nitrogen into the stripper it is possible to remove the light oil and water at the same time using the partial pressure of nitrogen. As disclosed in FIG. 2, which is one embodiment of the present invention, the side-cut oil produced at the intermediate stage of the main separator 100 is introduced into the nitrogen-using stripper 200 along the side-cut introduction tube 105. . Nitrogen is introduced into the nitrogen utilization stripper 200 along the nitrogen injection unit 201. The injection pressure of nitrogen should be set higher than the stripper pressure so that nitrogen can be injected into the stripper sufficiently. The pressure of the stripper may vary in each case, but is obvious to those skilled in the art. Nitrogen is then injected into the separator at the same point as the pressure inside the separator. At this time, the injection amount of nitrogen ranges from 0.1 kgmole / m 3 (oil) to 0.4 kgmole / m 3 (oil), preferably 0.2 kgmole / m 3 (oil) to 0.3 kgmole / m 3 (oil). When the injection amount of nitrogen is less than 0.1 kgmole / m 3 (oil), there is a problem that the separation effect due to the partial pressure of nitrogen is insignificant, and when the injection amount is more than 0.4 kgmole / m 3 (oil), the nitrogen is excessive to the nitrogen Excessive costs and problems such as overloading the compressor of the main separation tower. The light oil and water removed in the separator are returned back to the main separation column through pipe 2 (203). The hard oil and the oil removed from the separator are sent to the storage tank along the pipe 1 (205).
각각의 사용되는 제품에 따라 상이하기는 하나, 통상 국내 경유 제품의 경우 40℃ 이상의 인화점을 규격으로 하고 있는데, 상기 스트리퍼에서 분리된 유분은 60 내지 68 ℃의 인화점을 갖는다. 또한, 외관의 경우도 B&C(Bright & Clear)를 만족한다. 외관 규격은 육안으로 판단하며, 투명한 시료병에 빛을 투과시켜 표준사진과 비교하여 가장 비슷한 표준사진을 선택하여 결정된다. 여기의 표준 사진은 기술분야에서 널리 알려져 있는 것으로, B&C(Bright & Clear), Slight Hazy, Hazy, Free Water, Sediment, Suspended Solid의 6가지 등급으로 분류된다. 상기 분리기에서 분리된 유분은 스팀을 이용한 경우와 달리, 추가적인 수분 제거가 없이, 등유 및 디젤 제품에 배합용으로 사용될 수 있다.Although different depending on the product used, the domestic diesel products usually have a flash point of 40 ℃ or more, the oil separated from the stripper has a flash point of 60 to 68 ℃. In addition, the appearance also satisfies B & C (Bright & Clear). The appearance standard is judged by the naked eye, and is determined by selecting the most similar standard picture by comparing light with a standard sample by transmitting light through a transparent sample bottle. Standard photographs here are well known in the art and are classified into six grades: Bright & Clear, Slight Hazy, Hazy, Free Water, Sediment, and Suspended Solid. The oil separated in the separator can be used for blending in kerosene and diesel products without additional water removal, unlike steam.
이하, 실시예 및 비교예를 통하여 종래 스팀을 사용한 기술에 비하여 향상된 본 발명의 효과를 알아보도록 한다.Hereinafter, the effect of the present invention is improved as compared to the technique using the conventional steam through Examples and Comparative Examples.
실시예1Example 1
일반적으로 사용되는 RFCC 공정에서 본 발명에 따른 질소를 주입하는 것을 특징으로 하는 스트리퍼를 사용하였다. 질소의 주입압력은 7 kg/cm2g이었으며, 스트리퍼의 운전온도는 200℃이고, 질소 주입량은 0.23 kgmole/m3(oil)이었다.In the commonly used RFCC process was used a stripper characterized in that the injection of nitrogen according to the invention. The nitrogen injection pressure was 7 kg / cm 2 g, the operating temperature of the stripper was 200 ° C, and the nitrogen injection amount was 0.23 kgmole / m 3 (oil).
실시예1의 결과를 질소에 의한 스트리핑 이전의 상태와 비교한 것을 표 1에 나타내었다.Table 1 compares the results of Example 1 with the state before stripping with nitrogen.
표 1
Figure PCTKR2010000565-appb-T000001
 Table 1
Figure PCTKR2010000565-appb-T000001
실시예2Example 2
질소 사용량을 0.15 kgmole/m3(oil)로 변경한 것을 제외하고는 실시예1과 동일한 실시를 반복하였다.The same implementation as in Example 1 was repeated except that the amount of nitrogen used was changed to 0.15 kgmole / m 3 (oil).
비교예1Comparative Example 1
스트리퍼에 질소 대신 0.28 kgmole/m3(oil)의 스팀을 사용한 것을 제외하고는 실시예1과 동일한 실시를 반복하였다.The same run as in Example 1 was repeated except that 0.28 kgmole / m 3 (oil) of steam was used instead of nitrogen for the stripper.
상기 실시예1와 비교예1의 결과를 하기의 표에 나타내었다.The results of Example 1 and Comparative Example 1 are shown in the following table.
표 2
Figure PCTKR2010000565-appb-T000002
 TABLE 2
Figure PCTKR2010000565-appb-T000002
상기 표에서 보듯이, 인화점은 비슷한 범위에서 형성되었으나, 질소를 사용한 경우의 수분함량이 스팀을 사용한 것에 비하여 훨씬 적은 것을 알 수 있다. 또한 외관에서도 수분의 경우, hazy한 것에 비하여 질소를 사용한 경우에 B&C를 만족함을 알 수 있다. 따라서, 질소를 사용함이 스팀의 사용시 추가적으로 요구되는 수분 제거 공정의 추가가 필요없을 뿐더러 외관의 만족을 위한 추가적인 공정 또한 요구되지 않음을 알 수 있다. As shown in the table, the flash point was formed in a similar range, but it can be seen that the moisture content when using nitrogen is much smaller than using steam. In addition, it can be seen that in the case of water, B & C is satisfied when nitrogen is used as compared to hazy. Thus, it can be seen that the use of nitrogen does not require the addition of a water removal process additionally required in the use of steam, and also an additional process for satisfying the appearance is not required.
실시예3Example 3
실시예1를 질소 주입량을 0.1 kgmole/m3(oil)인 것을 제외하고는 동일하게 반복하였다.Example 1 was repeated in the same manner except that the nitrogen injection amount was 0.1 kgmole / m 3 (oil).
비교예2Comparative Example 2
실시예1를 질소를 주입하지 않은 것을 제외하고는 동일하게 반복하였다.Example 1 was repeated in the same manner except that no nitrogen was injected.
상기 실시예와 비교예를 하기의 표 3에 나타내었다.The Examples and Comparative Examples are shown in Table 3 below.
표 3
Figure PCTKR2010000565-appb-T000003
 TABLE 3
Figure PCTKR2010000565-appb-T000003
상기 표에서 알 수 있듯이, 스팀 주입의 경우는 수분 함량이 과다하여 추가적으로 수분을 제거하는 장치 또는 공정이 요구되어 적당치 않고, 질소 주입량이 0.1 kgmole/m3(oil) 이하인 경우 외관 규격을 만족하지 못할 뿐더러, 인화점 또한 상당히 낮아, 적합하지 않았다. 질소 주입량이 0.4 kgmole/m3(oil) 이상인 경우에는 외관 및 인화점은 향상될 것으로 예측되나, 상세한 설명에서 언급했던 바와 같이 질소의 비용과다, 및 압축기 과부하 등의 문제점을 지닌다.As can be seen from the above table, in case of steam injection, an additional device or process for removing water is required due to excessive moisture content, and when the nitrogen injection amount is 0.1 kgmole / m 3 (oil) or less, it does not satisfy the appearance specification. In addition, the flash point was also quite low, which was not suitable. When the amount of nitrogen injected is 0.4 kgmole / m 3 (oil) or more, the appearance and flash point are expected to be improved, but as mentioned in the detailed description, there are problems such as excessive cost of nitrogen and overload of the compressor.

Claims (4)

  1. 중질유 유동상촉매 분해공정에 있어서, 180℃ 내지 360℃의 비점을 갖는 HCN 및 LCO가 주분리탑에서 분리된 후 디젤 제품에 혼합되기 이전에 질소가스에 의하여, 경질 유분 및 수분을 제거시키는 단계를 포함하는 것을 특징으로 하는 유분의 스트리핑 방법.In the heavy oil fluid bed catalyst cracking process, HCN and LCO having a boiling point of 180 ° C. to 360 ° C. are separated from the main separation tower and then removed by the nitrogen gas before being mixed into the diesel product. Stripping method of the oil comprising a.
  2. 청구항 1에 있어서, 상기 질소의 주입 압력은 주분리탑과 보조 분리탑 압력 이상인 것을 특징으로 스트리핑 방법.The stripping method according to claim 1, wherein the injection pressure of nitrogen is equal to or greater than the pressure of the main separation column and the auxiliary separation column.
  3. 청구항 1에 있어서, 상기 질소의 주입량은 0.1 kgmole/m3(oil) 내지 0.4 kgmole/m3(oil)인 것을 특징으로 하는 스트리핑 방법.The stripping method according to claim 1, wherein the injection amount of nitrogen is 0.1 kgmole / m 3 (oil) to 0.4 kgmole / m 3 (oil).
  4. 청구항 1 내지 3 중 어느 한 항의 방법을 이용하는 것을 특징으로 하는 FCC 공정의 보조 분리기(stripper).An auxiliary stripper of an FCC process, characterized by using the method of claim 1.
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WO2012139181A1 (en) * 2011-04-15 2012-10-18 Petróleo Brasileiro S.A. - Petrobas Fcc process for diesel maximization using two distinct converters
CN113617052A (en) * 2021-07-19 2021-11-09 茂名海和石油化工有限公司 Stripping oil refining process using nitrogen as gas source

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WO2012139181A1 (en) * 2011-04-15 2012-10-18 Petróleo Brasileiro S.A. - Petrobas Fcc process for diesel maximization using two distinct converters
CN113617052A (en) * 2021-07-19 2021-11-09 茂名海和石油化工有限公司 Stripping oil refining process using nitrogen as gas source

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