JP2020180244A - Method for cleaning raw material oil heat exchanger of vacuum distillation apparatus - Google Patents
Method for cleaning raw material oil heat exchanger of vacuum distillation apparatus Download PDFInfo
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本発明は、減圧蒸留装置の原料油熱交換器の洗浄方法に関する。 The present invention relates to a method for cleaning a raw material oil heat exchanger of a vacuum distillation apparatus.
減圧蒸留装置は、減圧下で原料油となる常圧蒸留残渣油等を蒸留し、異なる沸点範囲を有する石油留分に分離するための装置である（例えば、特許文献１参照）。 The vacuum distillation apparatus is an apparatus for distilling atmospheric distillation residual oil or the like as a raw material oil under reduced pressure and separating it into petroleum fractions having different boiling point ranges (see, for example, Patent Document 1).
上記減圧蒸留装置の処理対象となる原料油は、熱交換器や加熱炉で３５０℃付近まで予熱されてから減圧蒸留装置に投入されている。 The raw material oil to be processed by the vacuum distillation apparatus is preheated to around 350 ° C. in a heat exchanger or a heating furnace, and then charged into the vacuum distillation apparatus.
しかしながら、本発明者が検討したところ、上述したとおり、減圧蒸留装置の処理対象となる原料油は重質なものであることから、熱交換器を用いて予熱すると熱交換部位に堆積物（汚れ）が付着して熱交換効率が低下し易くなることが判明した。熱交換効率が低下すると減圧蒸留装置に投入される原料油が十分に加温されないために、減圧蒸留装置で処理する際により大きなエネルギーが必要となり、急激な温度上昇に伴って触媒や反応装置の寿命を縮めたり、生産コストの上昇を招きやすくなる。 However, as examined by the present inventor, as described above, since the raw material oil to be processed by the vacuum distillation apparatus is heavy, when it is preheated using a heat exchanger, deposits (dirt) are formed on the heat exchange site. ) Is attached and the heat exchange efficiency is likely to decrease. When the heat exchange efficiency decreases, the raw material oil charged into the vacuum distillation apparatus is not sufficiently heated, so that more energy is required for processing in the vacuum distillation apparatus, and as the temperature rises sharply, the catalyst and reaction apparatus It tends to shorten the service life and increase the production cost.
このような状況下、本発明は、減圧蒸留装置の原料油熱交換器への汚れの付着を運転中に低減することができ、減圧蒸留装置の原料油熱交換器への汚れの付着を十分にかつ簡便に抑制し得る洗浄方法を提供することを目的とするものである。 Under such circumstances, the present invention can reduce the adhesion of dirt to the raw material oil heat exchanger of the vacuum distillation apparatus during operation, and the adhesion of dirt to the raw material oil heat exchanger of the vacuum distillation apparatus can be sufficiently reduced. It is an object of the present invention to provide a cleaning method that can be easily suppressed.
上記技術課題を解決するために本発明者等が鋭意検討したところ、予熱用熱交換器に付着する汚れ分の原因成分に対して溶解性を示す原料油基材を一定程度含む組成物であれば、熱交換器の壁面への汚れ分の付着を抑制するか、一旦付着した汚れ分を好適に溶解し得ることを着想した。 As a result of diligent studies by the present inventors in order to solve the above technical problems, the composition may contain a certain amount of raw material oil base material which is soluble in the causative component of the dirt adhering to the preheating heat exchanger. For example, the idea was to suppress the adhesion of dirt to the wall surface of the heat exchanger, or to dissolve the dirt once it had adhered.
上記知見に基づいて本発明者等がさらに検討したところ、減圧蒸留装置の原料油熱交換器の洗浄方法であって、１５℃における密度が０．９３〜１．００ｇ／ｃｍ３、アスファルテン含有量が５．０質量％以下である減圧蒸留装置用原料油を９０〜９９容量％含有するとともに、接触分解軽油、潤滑油を製造する際のフルフラール抽出工程により得られるエキストラクトおよび混合キシレンを蒸留分離する装置より得られるトルエン留分から選ばれる少なくとも１種以上の炭化水素油を含み、芳香族分含有量が４０〜８０質量％である燃料油基材を１〜１０容量％含有する洗浄用原料油を、減圧蒸留装置の原料油熱交換器に流通する洗浄方法により、上記目的を達成し得ることを見出し、本知見に基づいて本発明を完成するに至ったものである。 As a result of further studies by the present inventors based on the above findings, a method for cleaning a raw material oil heat exchanger of a vacuum distillation apparatus has a density of 0.93 to 1.00 g / cm 3 at 15 ° C. and an asphaltene content. Contains 90 to 99% by volume of raw material oil for vacuum distillation equipment having a content of 5.0% by mass or less, and distills and separates the extract and mixed xylene obtained by the furfural extraction step in the production of catalytic cracking gas oil and lubricating oil. A raw material oil for cleaning, which contains at least one hydrocarbon oil selected from the toluene distillate obtained from the device, and contains 1 to 10% by volume of a fuel oil base material having an aromatic content of 40 to 80% by mass. It has been found that the above object can be achieved by a cleaning method distributed to a raw material oil heat exchanger of a vacuum distillation apparatus, and the present invention has been completed based on this finding.
すなわち、本発明は、
（１）減圧蒸留装置の原料油熱交換器の洗浄方法であって、
１５℃における密度が０．９３〜１．００ｇ／ｃｍ３、アスファルテン含有量が５．０質量％以下である減圧蒸留装置用原料油を９０〜９９容量％含有するとともに、
接触分解軽油、潤滑油を製造する際のフルフラール抽出工程により得られるエキストラクトおよび混合キシレンを蒸留分離する装置より得られるトルエン留分から選ばれる少なくとも１種以上の炭化水素油を含み、芳香族分含有量が４０〜８０質量％である燃料油基材を１〜１０容量％含有する洗浄用原料油を、
減圧蒸留装置の原料油熱交換器に流通する
ことを特徴とする減圧蒸留装置の原料油熱交換器の洗浄方法、
（２）前記減圧蒸留装置の原料油熱交換器に対し、減圧蒸留装置用被処理油のみを流通させた後、前記洗浄用原料油を流通させる処理を繰り返し行う上記（１）に記載の洗浄方法、
（３）前記洗浄方法が以下の式（Ｉ）
｛（Ｖ２×Ｃ）／Ｖ１｝≧０．２０ （Ｉ）
（ただし、Ｖ１は、洗浄用原料油を流通させる前に流通させた減圧蒸留装置用被処理油の流通量（Ｌ）、Ｖ２は前記洗浄用原料油を流通させたときの洗浄用原料油の流通量（Ｌ）、Ｃは前記洗浄用原料油中の燃料用基材の含有割合（容量％）である。）
を満たすように洗浄用原料油を流通させることを特徴とする上記（１）または（２）に記載の洗浄方法
を提供するものである。
That is, the present invention
(1) A method for cleaning a raw material oil heat exchanger of a vacuum distillation apparatus.
It contains 90 to 99% by mass of raw material oil for vacuum distillation equipment having a density of 0.93 to 1.00 g / cm 3 at 15 ° C. and an asphaltene content of 5.0% by mass or less.
Contains at least one hydrocarbon oil selected from the toluene distillates obtained from the equipment that distills and separates the extract and mixed xylene obtained by the furfural extraction step in the production of catalytically cracked gas oil and lubricating oil, and contains aromatic components. A raw material oil for cracking containing 1 to 10% by volume of a fuel oil base material having an amount of 40 to 80% by mass.
A method for cleaning the raw material oil heat exchanger of a vacuum distillation apparatus, which is characterized by being distributed to the raw material oil heat exchanger of the vacuum distillation apparatus.
(2) The cleaning according to (1) above, wherein only the oil to be processed for the vacuum distillation apparatus is circulated to the raw material oil heat exchanger of the vacuum distillation apparatus, and then the process of circulating the raw material oil for cleaning is repeated. Method,
(3) The cleaning method is the following formula (I).
{(V2 × C) / V1} ≧ 0.20 (I)
(However, V1 is the distribution amount (L) of the oil to be processed for the vacuum distillation apparatus that was distributed before the cleaning raw material oil was distributed, and V2 is the cleaning raw material oil when the cleaning raw material oil was distributed. The distribution amount (L) and C are the content ratio (volume%) of the base material for fuel in the raw material oil for cleaning.)
The cleaning method according to (1) or (2) above is provided, wherein the raw material oil for cleaning is distributed so as to satisfy the above conditions.
本発明によれば、減圧蒸留装置の原料油熱交換器への汚れの付着を運転中に低減することができ、減圧蒸留装置の原料油熱交換器への汚れの付着を十分にかつ簡便に抑制し得る洗浄方法を提供することができる。 According to the present invention, it is possible to reduce the adhesion of dirt to the raw material oil heat exchanger of the vacuum distillation apparatus during operation, and the adhesion of dirt to the raw material oil heat exchanger of the vacuum distillation apparatus can be sufficiently and easily performed. A cleaning method that can be suppressed can be provided.
本発明に係る減圧蒸留装置の原料油熱交換器の洗浄方法は、減圧蒸留装置の原料油熱交換器の洗浄方法であって、
１５℃における密度が０．９３〜１．００ｇ／ｃｍ３、アスファルテン含有量が５．０質量％以下である減圧蒸留装置用原料油を９０〜９９容量％含有するとともに、
接触分解軽油、潤滑油を製造する際のフルフラール抽出工程により得られるエキストラクトおよび混合キシレンを蒸留分離する装置より得られるトルエン留分から選ばれる少なくとも１種以上の炭化水素油を含み、芳香族分含有量が４０〜８０質量％である燃料油基材を１〜１０容量％含有する洗浄用原料油を、
減圧蒸留装置の原料油熱交換器に流通する
ことを特徴とするものである。
The method for cleaning the raw material oil heat exchanger of the vacuum distillation apparatus according to the present invention is a method for cleaning the raw material oil heat exchanger of the vacuum distillation apparatus.
It contains 90 to 99% by mass of raw material oil for vacuum distillation equipment having a density of 0.93 to 1.00 g / cm 3 at 15 ° C. and an asphaltene content of 5.0% by mass or less.
Contains at least one hydrocarbon oil selected from the toluene distillates obtained from the equipment that distills and separates the extract and mixed xylene obtained by the furfural extraction step in the production of catalytically cracked gas oil and lubricating oil, and contains aromatic components. A raw material oil for cracking containing 1 to 10% by volume of a fuel oil base material having an amount of 40 to 80% by mass.
It is characterized in that it is distributed to a raw material oil heat exchanger of a vacuum distillation apparatus.
本発明において、洗浄用原料油は、減圧蒸留装置用原料油として、１５℃における密度が０．９３〜１．００ｇ／ｃｍ３、アスファルテン含有量が５．０質量％以下であるものを含有する。 In the present invention, the raw material oil for cleaning contains a raw material oil for a vacuum distillation apparatus having a density of 0.93 to 1.00 g / cm 3 at 15 ° C. and an asphaltene content of 5.0% by mass or less. ..
本発明おいて、減圧蒸留装置用原料油の１５℃における密度は、０．９３〜１．００ｇ／ｃｍ３であり、好ましくは０．９４〜１．００ｇ／ｃｍ３、より好ましくは０．９５〜１．００ｇ／ｃｍ３である。 In the present invention, the density of the raw material oil for a vacuum distillation apparatus at 15 ° C. is 0.93 to 1.00 g / cm 3 , preferably 0.94 to 1.00 g / cm 3 , and more preferably 0.95. ~ 1.00 g / cm 3 .
なお、本出願書類において、１５℃における密度は、ＪＩＳ Ｋ２２４９−１：２０１１により測定される値を意味する。 In this application document, the density at 15 ° C. means the value measured by JIS K2247-1: 2011.
本発明において、減圧蒸留装置用原料油のアスファルテン含有量は、５．０質量％以下であり、４．５質量％以下であることが好ましく、４．０質量％以下であることがより好ましい。
洗浄用原料油を構成する減圧蒸留装置用原料油のアスファルテン含有量が上記範囲内にあることにより、熱交換器に付着する汚れを低減または抑制し易くなる。
In the present invention, the asphaltene content of the raw material oil for a vacuum distillation apparatus is 5.0% by mass or less, preferably 4.5% by mass or less, and more preferably 4.0% by mass or less.
When the asphaltene content of the raw material oil for the vacuum distillation apparatus constituting the raw material oil for cleaning is within the above range, it becomes easy to reduce or suppress the dirt adhering to the heat exchanger.
なお、本出願書類において、アスファルテン含有量は、ＪＰＩ−５Ｓ−２２−８３に準じて測定される値を意味する。 In this application document, the asphaltene content means a value measured according to JPI-5S-22-83.
本発明において、洗浄用原料油を構成する減圧蒸留装置用原料油の芳香族分含有量は、３０〜５０質量％であることが好ましく、３２〜５０質量％であることより好ましく、３５〜５０質量％であることがさらに好ましい。 In the present invention, the aromatic content of the raw material oil for a vacuum distillation apparatus constituting the raw material oil for cleaning is preferably 30 to 50% by mass, more preferably 32 to 50% by mass, and 35 to 50%. It is more preferably by mass%.
なお、本出願書類において、芳香族分含有量は、ＪＰＩ−５Ｓ−４９−９７で測定される値を意味する。 In addition, in this application document, the aromatic content means the value measured by JPI-5S-49-97.
本発明において、減圧蒸留装置用原料油の沸点範囲は、２１０〜７９０℃であることが好ましく、２１５〜７９０℃であることがより好ましく、２２０〜７９０℃であることがさらに好ましい。
なお、本出願書類において、沸点範囲は、ＪＩＳ Ｋ２２５４：１９９８により測定される値を意味する。
In the present invention, the boiling point range of the raw material oil for a vacuum distillation apparatus is preferably 210 to 790 ° C, more preferably 215 to 790 ° C, and even more preferably 220 to 790 ° C.
In this application document, the boiling point range means a value measured by JIS K2254: 1998.
本発明において、減圧蒸留装置用原料油の９０容量％留出温度は、６３０〜７００℃であることが好ましく、６３０〜６９０℃であることがより好ましく、６３０〜６８０℃であることがさらに好ましい。減圧蒸留装置用原料油の９０容量％留出温度が上記範囲内であることにより、熱交換器の汚れ原因と考えられる重質なワックス留分の含有量が抑制され、効果的に汚れを低減することができる。
なお、本出願書類において、９０容量％留出温度は、ＪＩＳ Ｋ２２５４：１９９８で測定される値を意味する。
In the present invention, the 90% by volume distillation temperature of the raw material oil for a vacuum distillation apparatus is preferably 630 to 700 ° C, more preferably 630 to 690 ° C, and even more preferably 630 to 680 ° C. .. When the 90% by volume distillation temperature of the raw material oil for vacuum distillation equipment is within the above range, the content of heavy wax distillate, which is considered to be the cause of stains on the heat exchanger, is suppressed, and the stains are effectively reduced. can do.
In addition, in this application document, 90% by volume distillation temperature means the value measured by JIS K2254: 1998.
本発明において、減圧蒸留装置用原料油としては、上記特性を有するものであれば特に制限されないが、例えば、常圧蒸留装置から得られる常圧蒸留残渣油を挙げることができる。 In the present invention, the raw material oil for a vacuum distillation apparatus is not particularly limited as long as it has the above characteristics, and examples thereof include atmospheric distillation residual oil obtained from an atmospheric distillation apparatus.
本発明において、洗浄用原料油は、接触分解軽油、潤滑油を製造する際のフルフラール抽出工程により得られるエキストラクトおよび混合キシレンを蒸留分離する装置より得られるトルエン留分から選ばれる少なくとも１種以上の炭化水素油を含み、芳香族分含有量が４０〜８０質量％である燃料油基材を含有する。 In the present invention, the raw material oil for cleaning is at least one selected from a toluene distillate obtained from an apparatus for distilling and separating an extract obtained by a cracking gas oil, a furfural extraction step in producing a lubricating oil, and a mixed xylene. It contains a hydrocarbon oil and contains a fuel oil base material having an aromatic content of 40 to 80% by mass.
本発明において、燃料油基材の芳香族分含有量は、４０〜８０質量％であり、４２〜８０質量％であることが好ましく、４５〜８０質量％であることがより好ましい。
燃料油基材の芳香族分含有量が上記範囲内にあることにより、洗浄用原料油が優れた溶解力を発揮して、より効果的に熱交換器の汚れを低減することができる。
In the present invention, the aromatic content of the fuel oil base material is 40 to 80% by mass, preferably 42 to 80% by mass, and more preferably 45 to 80% by mass.
When the aromatic content of the fuel oil base material is within the above range, the raw material oil for cleaning exhibits excellent dissolving power, and the dirt on the heat exchanger can be reduced more effectively.
本発明において、燃料油基材の９０容量％留出温度は、７０〜６００℃であることが好ましく、７２〜６００℃であることがより好ましく、７５〜６００℃であることがさらに好ましい。
燃料油基材の９０容量％留出温度が上記範囲内にあることにより、熱交換器の汚れ原因と考えられる重質なワックス留分の含有量が抑制され、効果的に汚れを低減することができる。
In the present invention, the 90% by volume distillation temperature of the fuel oil base material is preferably 70 to 600 ° C., more preferably 72 to 600 ° C., and even more preferably 75 to 600 ° C.
When the 90% by volume distillate temperature of the fuel oil base material is within the above range, the content of heavy wax distillate, which is considered to be the cause of stains on the heat exchanger, is suppressed, and the stains are effectively reduced. Can be done.
本発明において、燃料油基材のアスファルテン含有量は、１．０質量％以下であることが好ましく、０．８質量％以下であることがより好ましく、０．５質量％以下であることがさらに好ましい。
燃料油基材のアスファルテン含有量が上記範囲内であることにより、原料油熱交換器に付着する汚れを容易に低減または抑制することができる。
In the present invention, the asphaltene content of the fuel oil base material is preferably 1.0% by mass or less, more preferably 0.8% by mass or less, and further preferably 0.5% by mass or less. preferable.
When the asphaltene content of the fuel oil base material is within the above range, dirt adhering to the raw material oil heat exchanger can be easily reduced or suppressed.
本発明において、燃料油基材は、接触分解軽油、潤滑油を製造する際のフルフラール抽出工程により得られるエキストラクトまたは混合キシレンを蒸留分離する装置より得られるトルエンから選ばれる少なくとも１種以上の留分を含む。
燃料油基材が上記留分を含むことにより、減圧蒸留処理への影響を抑制しつつ、原料油の処理量をさほど落とすことなく、減圧蒸留装置の連続運転を止めずに原料油熱交換器に付着した汚れを低減させることができる。
In the present invention, the fuel oil base material is a distillate of at least one selected from toluene obtained from an apparatus for distilling and separating an extract or mixed xylene obtained by a furfural extraction step in producing catalytically cracked gas oil and lubricating oil. Including minutes.
Since the fuel oil base material contains the above fraction, the raw material oil heat exchanger suppresses the influence on the vacuum distillation process, does not significantly reduce the processing amount of the raw material oil, and does not stop the continuous operation of the vacuum distillation apparatus. Distillation attached to can be reduced.
本発明において、接触分解軽油とは、重質油を接触分解処理したときに中間留分として得られる接触分解軽油、すなわちライトサイクルオイル（ＬＣＯ）を意味する。 In the present invention, the catalytic cracking gas oil means a catalytic cracking gas oil (LCO) obtained as an intermediate distillate when a heavy oil is subjected to a catalytic cracking treatment.
本発明において、接触分解軽油の芳香族分含有量は、４０〜８０質量％であることが好ましく、４２〜８０質量％であることがより好ましく、４５〜８０質量％であることがさらに好ましい。
接触分解軽油の芳香族分含有量が上記範囲内であることにより、混合された減圧蒸留装置用原料油の溶解力が向上し、効果的に原料油熱交換器に付着した汚れを低減することができる。
In the present invention, the aromatic content of the catalytically cracked diesel fuel is preferably 40 to 80% by mass, more preferably 42 to 80% by mass, and further preferably 45 to 80% by mass.
When the aromatic content of the catalytic cracking gas oil is within the above range, the dissolving power of the mixed raw material oil for vacuum distillation equipment is improved, and the dirt adhering to the raw material oil heat exchanger is effectively reduced. Can be done.
本発明において、接触分解軽油の９０容量％留出温度は、２８０〜３９０℃であることが好ましく、２９０〜３９０℃であることがより好ましく、３００〜３９０℃であることがさらに好ましい。
接触分解軽油の９０容量％留出温度が上記範囲内にあることにより、原料油に混合する際、重質なワックスの含有量が容易に抑制され、効果的に汚れを低減できる。
In the present invention, the 90% by volume distillation temperature of the catalytically cracked gas oil is preferably 280 to 390 ° C, more preferably 290 to 390 ° C, and even more preferably 300 to 390 ° C.
When the 90% by volume distillation temperature of the catalytic cracking gas oil is within the above range, the content of heavy wax is easily suppressed when mixed with the raw material oil, and stains can be effectively reduced.
本発明において、接触分解軽油のアスファルテン含有量は、０．１質量％以下であることが好ましく、０．０５質量％以下であることがより好ましく、０．０１質量％以下であることがさらに好ましい。
接触分解軽油のアスファルテン含有量が上記範囲内にあることにより、原料油熱交換器に付着する汚れを容易に低減または抑制することができる。
In the present invention, the asphaltene content of the catalytically cracked gas oil is preferably 0.1% by mass or less, more preferably 0.05% by mass or less, and further preferably 0.01% by mass or less. ..
When the asphaltene content of the catalytically cracked gas oil is within the above range, dirt adhering to the raw material oil heat exchanger can be easily reduced or suppressed.
本発明において、エキストラクトとは、原油の常圧蒸留残渣油を減圧蒸留して得られる中質・重質の減圧蒸留留出油あるいは減圧蒸留残渣油の脱歴油（ブライトストック油）をフルフラール等で抽出分離した油を意味する。
上記フルフラール等で抽出した残分は、ラフィネートと称される潤滑油基油として使用されることから、エキストラクトは工業的には潤滑油製造工程で得られるものである。
In the present invention, the extract is a medium or heavy vacuum distillation distillate obtained by vacuum distillation of a crude oil at atmospheric pressure or a deflated oil (bright stock oil) of a vacuum distillation residue oil. It means oil extracted and separated by.
Since the residue extracted with furfural or the like is used as a lubricating oil base oil called raffinate, the extract is industrially obtained in the lubricating oil manufacturing process.
本発明において、エキストラクトの芳香族分含有量は、４０〜７０質量％であることが好ましく、４５〜７０質量％であることがより好ましく、５０〜７０質量％であることがさらに好ましい。
エキストラクトの芳香族分含有量が上記範囲内にあることにより、混合された減圧蒸留装置用原料油の溶解力が向上し、効果的に原料油熱交換器に付着した汚れを低減することができる。
In the present invention, the aromatic content of the extract is preferably 40 to 70% by mass, more preferably 45 to 70% by mass, and even more preferably 50 to 70% by mass.
When the aromatic content of the extract is within the above range, the dissolving power of the mixed raw material oil for vacuum distillation equipment is improved, and the stains adhering to the raw material oil heat exchanger can be effectively reduced. it can.
本発明において、エキストラクトの９０容量％留出温度は、５００〜６００℃であることが好ましく、５１０〜６００℃であることがより好ましく、５２０〜６００℃であることがさらに好ましい。
エキストラクトの９０容量％留出温度が上記範囲内にあることにより、原料油に混合する際、重質なワックスの含有量が容易に抑制され、効果的に汚れを低減できる。
In the present invention, the 90% by volume distillation temperature of the extract is preferably 500 to 600 ° C., more preferably 510 to 600 ° C., and even more preferably 520 to 600 ° C.
When the 90% by volume distillate temperature of the extract is within the above range, the content of heavy wax is easily suppressed when mixed with the raw material oil, and stains can be effectively reduced.
本発明において、エキストラクトのアスファルテン含有量は、１．０質量％以下であることが好ましく、０．８質量％以下であることがより好ましく、０．５質量％以下であることがさらに好ましい。
エキストラクトのアスファルテン含有量が上記範囲内であることにより、原料油熱交換器に付着する汚れを低減または抑制することができる。
In the present invention, the asphaltene content of the extract is preferably 1.0% by mass or less, more preferably 0.8% by mass or less, and further preferably 0.5% by mass or less.
When the asphaltene content of the extract is within the above range, dirt adhering to the raw material oil heat exchanger can be reduced or suppressed.
本発明において、トルエン留分は、混合キシレンを蒸留分離する装置より得られるトルエンを主成分とした留分を意味し、沸点範囲が、７０〜１３０℃であるものが好ましく、７２〜１３０℃であるものがより好ましく、７５〜１３０℃であるものがさらに好ましい。
混合キシレンを蒸留分離する装置とは、重質改質ナフサを蒸留して、ｏ−キシレン及びｐ−キシレンを主成分とした混合キシレンを得るための装置であり、副生物としてトルエンを蒸留分離することができる。
In the present invention, the toluene fraction means a toluene-based fraction obtained from an apparatus that distills and separates mixed xylene, and has a boiling point range of 70 to 130 ° C., preferably 72 to 130 ° C. Some are more preferred, and those at 75-130 ° C are even more preferred.
The device for distilling and separating mixed xylene is a device for distilling heavy-modified naphtha to obtain mixed xylene containing o-xylene and p-xylene as main components, and distilling and separating toluene as a by-product. be able to.
本発明において、トルエン留分の芳香族分含有量は、６０〜８０質量％であることが好ましく、６２〜８０質量％であることがより好ましく、６５〜８０質量％であることがさらに好ましい。
トルエン留分の芳香族分含有量が上記範囲内にあることにより、混合された減圧蒸留装置用原料油の溶解力が容易に向上し、効果的に原料油熱交換器に付着した汚れを低減することができる。
In the present invention, the aromatic content of the toluene fraction is preferably 60 to 80% by mass, more preferably 62 to 80% by mass, and even more preferably 65 to 80% by mass.
When the aromatic content of the toluene fraction is within the above range, the dissolving power of the mixed raw material oil for vacuum distillation equipment is easily improved, and the dirt adhering to the raw material oil heat exchanger is effectively reduced. can do.
本発明において、洗浄用原料油を構成する減圧蒸留装置用原料油の含有割合は、９０〜９９容量％であり、９０〜９８．５容量％であることが好ましく、９０〜９８容量％であることがより好ましい。 In the present invention, the content ratio of the raw material oil for a vacuum distillation apparatus constituting the raw material oil for cleaning is 90 to 99% by volume, preferably 90 to 98.5% by volume, and 90 to 98% by volume. Is more preferable.
また、本発明において、洗浄用原料油を構成する燃料油基材の含有割合は、１〜１０容量％であり、１．５〜１０容量％であることが好ましく、２〜１０容量％であることがより好ましい。 Further, in the present invention, the content ratio of the fuel oil base material constituting the raw material oil for cleaning is 1 to 10% by volume, preferably 1.5 to 10% by volume, and 2 to 10% by volume. Is more preferable.
洗浄用原料油を構成する燃料油基材の含有割合が上記範囲内にあることにより、減圧蒸留装置の連続運転を止めずに原料油熱交換器に付着した汚れを低減させることができ、減圧蒸留装置の連続運転を停止して熱交換器を解放洗浄するまでの期間を延長することができる。また、原料油の処理量をさほど落とすことなく、さらに洗浄のために使用する付加価値の高い燃料油基材の使用量を抑えつつ、経済的に処理することができる。 When the content ratio of the fuel oil base material constituting the raw material oil for cleaning is within the above range, it is possible to reduce the dirt adhering to the raw material oil heat exchanger without stopping the continuous operation of the vacuum distillation apparatus, and the pressure is reduced. It is possible to extend the period until the continuous operation of the distillation apparatus is stopped and the heat exchanger is released and washed. In addition, it is possible to economically process the raw material oil without significantly reducing the amount of the raw material oil processed, while further reducing the amount of the high value-added fuel oil base material used for cleaning.
本発明に係る洗浄方法においては、上記減圧蒸留装置の原料油熱交換器に対し、減圧蒸留装置用被処理油のみを流通させた後、前記洗浄用原料油を流通させる処理を繰り返し行うことが好ましい。
減圧蒸留装置用被処理油としては、上述した減圧蒸留装置用原料油と同様のものを挙げることができる。
減圧蒸留装置用被処理油の流通後の洗浄用原料油の流通は定期的に行ってもよいし、非定期的に行ってもよいが、定期的に行うことが好ましい。
このように、減圧蒸留装置用被処理油の流通と、洗浄用原料油の流通を交互に行うことにより、減圧蒸留装置装置の連続運転を止めずに原料油熱交換器に付着した十分にかつ簡便に低減することができる。
In the cleaning method according to the present invention, after only the oil to be processed for the vacuum distillation apparatus is circulated to the raw material oil heat exchanger of the vacuum distillation apparatus, the process of distributing the raw material oil for cleaning is repeated. preferable.
Examples of the oil to be treated for the vacuum distillation apparatus include the same oils as the above-mentioned raw material oil for the vacuum distillation apparatus.
The raw material oil for cleaning after the distribution of the oil to be processed for the vacuum distillation apparatus may be distributed regularly or irregularly, but it is preferable to perform it regularly.
By alternately circulating the oil to be processed for the vacuum distillation apparatus and the raw material oil for cleaning in this way, the oil heat exchanger is sufficiently adhered to the raw material oil heat exchanger without stopping the continuous operation of the vacuum distillation apparatus. It can be easily reduced.
本発明に係る洗浄方法においては、以下の式（Ｉ）
｛（Ｖ２×Ｃ）／Ｖ１｝≧０．２０ （Ｉ）
（ただし、Ｖ１は、洗浄用原料油を流通させる前に流通させた減圧蒸留装置用被処理油の流通量（Ｌ）、Ｖ２は前記洗浄用原料油を流通させたときの洗浄用原料油の流通量（Ｌ）、Ｃは前記洗浄用原料油中の燃料用基材の含有割合（容量％）である。）
を満たすように洗浄用原料油を流通させることが好ましい。
In the cleaning method according to the present invention, the following formula (I)
{(V2 × C) / V1} ≧ 0.20 (I)
(However, V1 is the distribution amount (L) of the oil to be processed for the vacuum distillation apparatus that was distributed before the cleaning raw material oil was distributed, and V2 is the cleaning raw material oil when the cleaning raw material oil was distributed. The distribution amount (L) and C are the content ratio (volume%) of the base material for fuel in the raw material oil for cleaning.)
It is preferable to distribute the raw material oil for cleaning so as to satisfy the above conditions.
式（Ｉ）において、減圧蒸留装置用被処理油の流通と、洗浄用原料油の流通を各々１回づつ行ったときは、Ｖ１およびＶ２は、各々の流通量（Ｌ）である。
式（Ｉ）において、減圧蒸留装置用被処理油のみを流通させた後、洗浄用原料油を流通させる処理を繰り返し行ったときは、減圧蒸留装置用被処理油のみの流通とその直後の洗浄用原料油の流通を１つの処理として、各処理時における、減圧蒸留装置用被処理油の流通量をＶ１（Ｌ）、洗浄用原料油の流通量をＶ２（Ｌ）として、上記比を算出する。
In the formula (I), when the distribution of the oil to be processed for the vacuum distillation apparatus and the distribution of the raw material oil for cleaning are performed once each, V1 and V2 are the respective distribution amounts (L).
In formula (I), when only the oil to be processed for the vacuum distillation apparatus is circulated and then the process of circulating the raw material oil for cleaning is repeated, only the oil to be processed for the vacuum distillation apparatus is circulated and the cleaning immediately after that is performed. The above ratio is calculated with the distribution of the feedstock for cleaning as one treatment, the flow of the oil to be processed for the vacuum distillation apparatus at each treatment as V1 (L), and the flow of the feedstock for cleaning as V2 (L). To do.
上記式｛（Ｖ２×Ｃ）／Ｖ１｝で表される値は、０．２０以上であり、０．２２以上が好ましく、０．２５以上がより好ましい。 The value represented by the above formula {(V2 × C) / V1} is 0.20 or more, preferably 0.22 or more, and more preferably 0.25 or more.
本発明に係る洗浄方法において式（Ｉ）を満たすように定期的ないし非定期的に洗浄用原料油を流通させることにより、減圧蒸留装置装置の連続運転を止めずに原料油熱交換器に付着した汚れを低減させることができ、減圧蒸留装置の連続運転を停止して熱交換器を解放洗浄するまでの期間を延長することができる。また、原料油の処理量をさほど落とすことなく、さらに洗浄のために使用する付加価値の高い燃料油基材の使用量を抑えることができ、経済的な処理が可能となる。 By regularly or irregularly distributing the raw material oil for cleaning so as to satisfy the formula (I) in the cleaning method according to the present invention, it adheres to the raw material oil heat exchanger without stopping the continuous operation of the vacuum distillation apparatus. It is possible to reduce the amount of dirt generated, and it is possible to extend the period until the continuous operation of the vacuum distillation apparatus is stopped and the heat exchanger is released and washed. Further, it is possible to reduce the amount of the high value-added fuel oil base material used for cleaning without significantly reducing the amount of the raw material oil to be processed, which enables economical processing.
本発明によれば、減圧蒸留装置の原料油熱交換器への汚れの付着を運転中に低減することができ、減圧蒸留装置の原料油熱交換器への汚れの付着を十分にかつ簡便に抑制し得るの洗浄方法を提供することができる。 According to the present invention, it is possible to reduce the adhesion of dirt to the raw material oil heat exchanger of the vacuum distillation apparatus during operation, and the adhesion of dirt to the raw material oil heat exchanger of the vacuum distillation apparatus can be sufficiently and easily performed. A cleaning method that can be suppressed can be provided.
次に、本発明を実施例および比較例によりさらに具体的に説明するが、本発明はこれらの例により何ら制限されるものではない。 Next, the present invention will be described in more detail with reference to Examples and Comparative Examples, but the present invention is not limited to these examples.
（実施例１）
（１）基材
減圧蒸留装置の原料油（被処理油）として、表１に示す物性を有する常圧蒸留残渣油（ＡＢＭ）を用意するとともに、燃料油基材Ｂとして、表１に示す物性を有する接触分解軽油（ＬＣＯ）を用意した。
上記常圧蒸留残渣油（ＡＢＭ）を９０容量％、ＬＣＯを１０容量％の割合で混合して洗浄用原料油とした。
(Example 1)
(1) Base material Atmospheric distillation residual oil (ABM) having the physical properties shown in Table 1 is prepared as the raw material oil (oil to be processed) of the vacuum distillation apparatus, and the physical properties shown in Table 1 are used as the fuel oil base material B. A cracked gas oil (LCO) having the above was prepared.
The atmospheric distillation residual oil (ABM) was mixed at a ratio of 90% by volume and LCO at a ratio of 10% by volume to prepare a raw material oil for cleaning.
（２）洗浄方法
図１に概略断面図で示すように、原料油タンクＴ１に貯蔵されホットプレートＨＰにより７０℃に加温された１．２Ｌの上記常圧蒸留残渣油（ＡＢＭ）を、同じく（図示しない）リボンヒーターにより流路全体が７０℃に維持された流通配管ｃ（直径６．５ｍｍ）内に毎分１０ｍＬで送液しつつ、上記常圧蒸留残渣油（ＡＢＭ）の流通配管内に各々ヒーターロッドＲ（ステンレス鋼製、長さ２００ｍｍ、直径６ｍｍ）を配置した加熱ヒーターＨＴ１および加熱ヒーターＨＴ２でそれぞれ設定温度Ｔ１（１７０℃）、Ｔ２（３００℃）で順次加熱して上記原料油タンクＴ１に返送する操作を３７０分間継続した後、バルブＶ１を切り替え、洗浄タンクＴ２に貯蔵された洗浄用原料油を毎分１０ｍＬで１０分間通油した。この際バルブＶ２を開くことで洗浄用原料油が原料タンクに混入しないようにする。１０分後バルブＶ１を原料油タンクＴ１側に戻し、流路内の洗浄油が完全に排出されたのちバルブＶ２を閉じ、原料油の通油を再開し、２６０分間継続した。上記加熱ヒーターＨＴ２の原料油出口に配置された原料油温度計測手段ＴＭ２ｏｕｔで原料油のヒーター出口温度Ｔ３を測定したときの結果を表２に示す。
(2) Cleaning Method As shown in a schematic cross-sectional view in FIG. 1, 1.2 L of the atmospheric distillation residual oil (ABM) stored in the raw material oil tank T1 and heated to 70 ° C. by the hot plate HP is similarly added. Inside the flow pipe of the atmospheric distillation residual oil (ABM) while sending the liquid at 10 mL / min into the flow pipe c (diameter 6.5 mm) whose entire flow path is maintained at 70 ° C. by a ribbon heater (not shown). The above raw material oil is sequentially heated at set temperatures T1 (170 ° C.) and T2 (300 ° C.) by the heating heater HT1 and the heating heater HT2, respectively, in which heater rods R (stainless steel, length 200 mm, diameter 6 mm) are arranged. After continuing the operation of returning to the tank T1 for 370 minutes, the valve V1 was switched and the raw material oil for cleaning stored in the cleaning tank T2 was passed through at 10 mL / min for 10 minutes. At this time, the valve V2 is opened to prevent the raw material oil for cleaning from being mixed into the raw material tank. After 10 minutes, the valve V1 was returned to the raw material oil tank T1 side, the cleaning oil in the flow path was completely discharged, the valve V2 was closed, the raw material oil was restarted, and continued for 260 minutes. Table 2 shows the results when the heater outlet temperature T3 of the raw material oil was measured by the raw material oil temperature measuring means TM2out arranged at the raw material oil outlet of the heater HT2.
（実施例２）
原料油である常圧蒸留残渣油（ＡＢＭ）の送液を運転開始から５００分間継続した後に、洗浄用原料油を毎分１０ｍＬで１０分間通油する以外は実施例１と同じ条件でヒーター出口温度Ｔ３を測定した。結果を表２に示す。
(Example 2)
The heater outlet under the same conditions as in Example 1 except that the feedstock of atmospheric distillation residual oil (ABM), which is the raw material oil, is continuously fed for 500 minutes from the start of operation, and then the raw material oil for cleaning is passed through at 10 mL / min for 10 minutes. The temperature T3 was measured. The results are shown in Table 2.
（実施例３）
原料油である常圧蒸留残渣油（ＡＢＭ）の送液を運転開始から３００分間継続した後に、洗浄用原料油を毎分１０ｍＬで１０分間通油し、その後原料油である常圧蒸留残渣油（ＡＢＭ）を６０分間通油した。その後、洗浄油原料油を毎分１０ｍＬで１０分間通油し、原料油である常圧蒸留残渣油（ＡＢＭ）を６０分間通油した。さらにその後、洗浄用原料油を毎分１０ｍＬで１０分間通油し、原料油である常圧蒸留残渣油（ＡＢＭ）を６０分間通油した。さらにその後、洗浄用原料油を毎分１０ｍＬで通油し、原料油である常圧蒸留残渣油（ＡＢＭ）を１２０分間通油した以外は実施例１と同じ条件でヒーター出口温度Ｔ３を測定した。結果を表２に示す。
(Example 3)
After continuing the feeding of the raw material oil, atmospheric distillation residual oil (ABM) for 300 minutes from the start of operation, the raw material oil for cleaning is passed through at 10 mL / min for 10 minutes, and then the raw material oil, atmospheric distillation residual oil. (ABM) was oiled for 60 minutes. Then, the raw material oil for cleaning oil was passed through at 10 mL / min for 10 minutes, and the raw material oil, atmospheric distillation residual oil (ABM), was passed through for 60 minutes. After that, the raw material oil for cleaning was passed through at 10 mL / min for 10 minutes, and the raw material oil, atmospheric distillation residual oil (ABM), was passed through for 60 minutes. Further, after that, the heater outlet temperature T3 was measured under the same conditions as in Example 1 except that the raw material oil for cleaning was passed at 10 mL / min and the raw material oil, atmospheric distillation residual oil (ABM), was passed for 120 minutes. .. The results are shown in Table 2.
（比較例１）
洗浄用原料油を通油しない以外は実施例１と同じ条件でヒーター出口温度Ｔ３を測定した。結果を表２に示す。
(Comparative Example 1)
The heater outlet temperature T3 was measured under the same conditions as in Example 1 except that the raw material oil for cleaning was not passed through. The results are shown in Table 2.
また、各実施例および比較例における式｛（Ｖ２×Ｃ）／Ｖ１｝の算出結果を表３に示す。 Table 3 shows the calculation results of the formula {(V2 × C) / V1} in each Example and Comparative Example.
表２より、実施例１は測定開始後３７０〜３８０分の間に、実施例２は測定開始後５００〜５１０分の間に、実施例３は測定開始後３００〜３１０分、３７０〜３８０分、４４０〜４５０分、５１０〜５２０分の間に洗浄用原料油が通油されたことにより、ヒーター出口温度Ｔ３がその前後で下降傾向から上昇傾向に転じていることが分かる。
一方、表２より、比較例１は洗浄用原料油を混合しないために、ヒーター出口温度が測定期間中にほぼ減少傾向にあり、測定開始時点から約５０℃も低下していることが分かる。
From Table 2, Example 1 is between 370 and 380 minutes after the start of measurement, Example 2 is between 500 and 510 minutes after the start of measurement, and Example 3 is 300 to 310 minutes and 370 to 380 minutes after the start of measurement. It can be seen that the heater outlet temperature T3 has changed from a downward trend to an upward trend before and after the passage of the cleaning raw material oil between 440 to 450 minutes and 510 to 520 minutes.
On the other hand, from Table 2, it can be seen that in Comparative Example 1, since the raw material oil for cleaning was not mixed, the heater outlet temperature tended to decrease almost during the measurement period, and decreased by about 50 ° C. from the start of measurement.
洗浄用原料油を混合した実施例１〜実施例３では、測定終了時において比較例１と比べ、ヒーター出口温度が高いことから、原料油の通油によりヒーターロッドＲに付着した汚れが１０分間程度洗浄用原料油を流通させる洗浄により低減されたことを示している。
このため、減圧蒸留装置の原料油熱交換器への原料油の供給を極く短時間だけ洗浄用原料油に切り替えることにより、汚れの付着を運転中に低減することができ、減圧蒸留装置の原料油熱交換器への汚れの付着を十分にかつ簡便に抑制し得ることが分かる。
また実施例３のように洗浄用原料油を繰り返し通油することで、熱交換器による汚れ付着がより効果的に軽減され、減圧蒸留装置および原料油熱交換器の連続運転の期間を容易に延長することができることが分かる。
In Examples 1 to 3 in which the raw material oil for cleaning was mixed, the heater outlet temperature was higher than that in Comparative Example 1 at the end of the measurement, so that the dirt adhering to the heater rod R due to the oil flow of the raw material oil was allowed for 10 minutes. It is shown that the temperature was reduced by cleaning with the raw material oil for cleaning.
Therefore, by switching the supply of the raw material oil to the raw material oil heat exchanger of the vacuum distillation apparatus to the raw material oil for cleaning for a very short time, it is possible to reduce the adhesion of dirt during operation, and the vacuum distillation apparatus can be used. It can be seen that the adhesion of dirt to the raw material oil heat exchanger can be sufficiently and easily suppressed.
Further, by repeatedly passing the raw material oil for cleaning as in Example 3, dirt adhesion by the heat exchanger is more effectively reduced, and the period of continuous operation of the vacuum distillation apparatus and the raw material oil heat exchanger can be facilitated. It turns out that it can be extended.
また表２および表３より、式｛（Ｖ２×Ｃ）／Ｖ１｝≧０．２０を満たすように洗浄用原料油を流通した実施例１〜実施例３は、ヒーター出口温度が洗浄用原料油の流通後すぐに上昇していることから、洗浄用原料油の流通前に付着した汚れを効果的に低減できていることがわかる。また最も汚れが付着している実施例２の式｛（Ｖ２×Ｃ）／Ｖ１｝により算出される値が０．２０であり所望の効果が得られていること、汚れの原因となる原料油の流通量がより少なく式｛（Ｖ２×Ｃ）／Ｖ１｝により算出される値が実施例２より大きい実施例１や実施例３でも所望の効果が得られていることから、洗浄用原料油の流通量と原料油の比である式｛（Ｖ２×Ｃ）／Ｖ１｝により算出される値が０．２０以上であれば所望の効果が得られることがわかる。
一方、比較例１では、洗浄油原料油を投入していないことにより、原料油の流通量が増えるとともに付着した汚れが低減されることなく、その結果、ヒーター出口温度が下降していることがわかる。
Further, from Tables 2 and 3, in Examples 1 to 3 in which the cleaning raw material oil was distributed so as to satisfy the formula {(V2 × C) / V1} ≧ 0.20, the heater outlet temperature was the cleaning raw material oil. It can be seen that the amount of dirt adhering to the cleaning raw material oil before distribution can be effectively reduced because the amount of oil increases immediately after distribution. Further, the value calculated by the formula {(V2 × C) / V1} of Example 2 to which the dirt is most adhered is 0.20, the desired effect is obtained, and the raw material oil causing the dirt. Since the desired effect was obtained in Examples 1 and 3 in which the amount of the oil in circulation was smaller and the value calculated by the formula {(V2 × C) / V1} was larger than that in Example 2, the raw material oil for cleaning was obtained. It can be seen that the desired effect can be obtained if the value calculated by the formula {(V2 × C) / V1}, which is the ratio of the distribution amount of the oil to the feedstock, is 0.20 or more.
On the other hand, in Comparative Example 1, since the cleaning oil raw material oil was not added, the distribution amount of the raw material oil was increased and the adhered dirt was not reduced, and as a result, the heater outlet temperature was lowered. Understand.
本発明によれば、減圧蒸留装置の原料油熱交換器への汚れの付着を運転中に低減することができ、減圧蒸留装置の原料油熱交換器への汚れの付着を十分にかつ簡便に抑制し得る洗浄方法を提供することができる。 According to the present invention, it is possible to reduce the adhesion of dirt to the raw material oil heat exchanger of the vacuum distillation apparatus during operation, and the adhesion of dirt to the raw material oil heat exchanger of the vacuum distillation apparatus can be sufficiently and easily performed. A cleaning method that can be suppressed can be provided.
Ｔ１、Ｔ２ ：タンク
Ｖ１、Ｖ２ ：切り替えバルブ
ＨＰ ：ホットプレート
ｃ ：流通配管
ＨＴ１、ＨＴ２ ：加熱ヒーター
Ｒ ：ヒーターロッド
Ｐ ：ポンプ
T1, T2: Tank V1, V2: Switching valve HP: Hot plate c: Distribution pipe HT1, HT2: Heater R: Heater rod P: Pump
Claims (3)
１５℃における密度が０．９３〜１．００ｇ／ｃｍ３、アスファルテン含有量が５．０質量％以下である減圧蒸留装置用原料油を９０〜９９容量％含有するとともに、
接触分解軽油、潤滑油を製造する際のフルフラール抽出工程により得られるエキストラクトおよび混合キシレンを蒸留分離する装置より得られるトルエン留分から選ばれる少なくとも１種以上の炭化水素油を含み、芳香族分含有量が４０〜８０質量％である燃料油基材を１〜１０容量％含有する洗浄用原料油を、
減圧蒸留装置の原料油熱交換器に流通する
ことを特徴とする減圧蒸留装置の原料油熱交換器の洗浄方法。 A method for cleaning the raw material oil heat exchanger of a vacuum distillation unit.
It contains 90 to 99% by mass of raw material oil for vacuum distillation equipment having a density of 0.93 to 1.00 g / cm 3 at 15 ° C. and an asphaltene content of 5.0% by mass or less.
Contains at least one hydrocarbon oil selected from the toluene distillates obtained from the equipment that distills and separates the extract and mixed xylene obtained by the furfural extraction step in the production of catalytically cracked gas oil and lubricating oil, and contains aromatic components. A raw material oil for cracking containing 1 to 10% by volume of a fuel oil base material having an amount of 40 to 80% by mass.
A method for cleaning a raw material oil heat exchanger of a vacuum distillation apparatus, which comprises distributing to a raw material oil heat exchanger of the vacuum distillation apparatus.
｛（Ｖ２×Ｃ）／Ｖ１｝≧０．２０ （Ｉ）
（ただし、Ｖ１は、洗浄用原料油を流通させる前に流通させた減圧蒸留装置用被処理油の流通量（Ｌ）、Ｖ２は前記洗浄用原料油を流通させたときの洗浄用原料油の流通量（Ｌ）、Ｃは前記洗浄用原料油中の燃料用基材の含有割合（容量％）である。）
を満たすように洗浄用原料油を流通させることを特徴とする請求項１または請求項２に記載の洗浄方法。
The cleaning method is the following formula (I)
{(V2 × C) / V1} ≧ 0.20 (I)
(However, V1 is the distribution amount (L) of the oil to be processed for the vacuum distillation apparatus that was distributed before the cleaning raw material oil was distributed, and V2 is the cleaning raw material oil when the cleaning raw material oil was distributed. The distribution amount (L) and C are the content ratio (volume%) of the base material for fuel in the raw material oil for cleaning.)
The cleaning method according to claim 1 or 2, wherein the raw material oil for cleaning is distributed so as to satisfy the above conditions.
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| JP2003213470A (en) * | 2002-01-23 | 2003-07-30 | Kurita Engineering Co Ltd | Method of cleaning petroleum refining plant |
| US20090038995A1 (en) * | 2007-08-06 | 2009-02-12 | Exxonmobil Research And Engineering Company | Method for reducing oil fouling in heat transfer equipment |
| CN102216428A (en) * | 2008-11-24 | 2011-10-12 | 埃克森美孚研究工程公司 | Methods of isolating and using components from a high solvency dispersive power (hsdp) crude oil |
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| JP2003213470A (en) * | 2002-01-23 | 2003-07-30 | Kurita Engineering Co Ltd | Method of cleaning petroleum refining plant |
| US20090038995A1 (en) * | 2007-08-06 | 2009-02-12 | Exxonmobil Research And Engineering Company | Method for reducing oil fouling in heat transfer equipment |
| CN102216428A (en) * | 2008-11-24 | 2011-10-12 | 埃克森美孚研究工程公司 | Methods of isolating and using components from a high solvency dispersive power (hsdp) crude oil |
| JP2012509954A (en) * | 2008-11-24 | 2012-04-26 | エクソンモービル リサーチ アンド エンジニアリング カンパニー | Method of separating components from high dissolution dispersibility (HSDP) crude oil |
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