JPH04114088A - Distillation of crude oil - Google Patents
Distillation of crude oilInfo
- Publication number
- JPH04114088A JPH04114088A JP23301290A JP23301290A JPH04114088A JP H04114088 A JPH04114088 A JP H04114088A JP 23301290 A JP23301290 A JP 23301290A JP 23301290 A JP23301290 A JP 23301290A JP H04114088 A JPH04114088 A JP H04114088A
- Authority
- JP
- Japan
- Prior art keywords
- distillation column
- oil
- column
- crude oil
- distillation
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
- 238000004821 distillation Methods 0.000 title claims abstract description 148
- 239000010779 crude oil Substances 0.000 title claims abstract description 56
- 239000003921 oil Substances 0.000 claims abstract description 72
- 239000003507 refrigerant Substances 0.000 claims abstract description 15
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 15
- 238000011084 recovery Methods 0.000 claims abstract description 11
- 238000000034 method Methods 0.000 claims description 18
- 238000001816 cooling Methods 0.000 claims description 7
- 239000000295 fuel oil Substances 0.000 abstract description 8
- 239000007789 gas Substances 0.000 description 23
- 238000010438 heat treatment Methods 0.000 description 17
- 239000000047 product Substances 0.000 description 12
- 230000000694 effects Effects 0.000 description 7
- 238000010586 diagram Methods 0.000 description 4
- 238000001704 evaporation Methods 0.000 description 4
- 230000008020 evaporation Effects 0.000 description 4
- 238000007796 conventional method Methods 0.000 description 3
- 230000007423 decrease Effects 0.000 description 2
- 239000007788 liquid Substances 0.000 description 2
- 230000014759 maintenance of location Effects 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- RHDGNLCLDBVESU-UHFFFAOYSA-N but-3-en-4-olide Chemical compound O=C1CC=CO1 RHDGNLCLDBVESU-UHFFFAOYSA-N 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 239000012043 crude product Substances 0.000 description 1
- 230000003247 decreasing effect Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- -1 furanone nitrogen Chemical compound 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- 239000003350 kerosene Substances 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 238000001256 steam distillation Methods 0.000 description 1
- 238000005979 thermal decomposition reaction Methods 0.000 description 1
- 238000005292 vacuum distillation Methods 0.000 description 1
Landscapes
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
Description
【発明の詳細な説明】
〔産業上の利用分野〕
本発明は、原油蒸留方法に関し、さらに詳しくは白油収
率の改善または、大幅な省エネルギー効果、さらにはこ
れら両方を達成することができる原油蒸留方法に関する
。[Detailed Description of the Invention] [Industrial Application Field] The present invention relates to a method for distilling crude oil, and more specifically to a method for distilling crude oil that can improve the yield of white oil or achieve a significant energy saving effect, and furthermore, a method for distilling crude oil that can achieve both of these effects. Regarding a distillation method.
常圧蒸留装置は、原油から粗製品を分離する手段として
広く用いろれている。Atmospheric distillation equipment is widely used as a means of separating crude products from crude oil.
第４図は、従来の２塔式の原油常圧蒸留装置の概略系統
図である。この装置は、前留塔１と、該前留塔１の塔頂
成分を冷却する塔頂コンデンサ４Ａと、該塔頂コンデン
サ４Ａの凝縮液を受ける前留塔塔頂受ｐｉ ５ Ａと、
前記前留塔塔底油を加熱する加熱炉１６と、該加熱炉１
６により加熱された前留塔塔底油を処理する主蒸留塔２
と、該主蒸留塔２の塔頂成分を冷却する主蒸留塔塔頂コ
ンデンサ１８と、該主蒸留塔塔頂コンデンサＩ８の凝縮
液を受ける主蒸留塔塔頂受槽１９とから主として構成さ
れる。FIG. 4 is a schematic diagram of a conventional two-column crude oil atmospheric distillation apparatus. This device includes a front distillation tower 1, an overhead condenser 4A for cooling the top component of the front distillation tower 1, and a front distillation tower top receiver pi 5A for receiving the condensate of the tower top condenser 4A.
a heating furnace 16 for heating the bottom oil of the front distillation column, and the heating furnace 1
Main distillation column 2 which processes the pre-distillation column bottom oil heated by 6.
The main distillation column top condenser 18 cools the top component of the main distillation column 2, and the main distillation column top receiving tank 19 receives the condensate from the main distillation column top condenser I8.
上記従来の装置において、原油はライン２１を介して、
高温製品油を熱媒とする原油熱交換器９．１０．１１、
塔底油１２および高温ポンプアラウンド液を熱媒とする
原油熱交換器１３．１４によって昇温され、前留塔１に
供給される。原油は、前留塔１において水蒸気蒸留され
、塔頂製品としてＬＰＧ留分、軽質ナフサ等の軽質留分
が得られる。前留塔塔底油は、前留塔を出た後、加熱炉
１６で加熱され、主蒸留塔２のフラノンニ゛／−ン１７
に供給される。主蒸留塔を出た塔頂版気は、水また１よ
空気を冷媒とする主蒸留塔塔頂コンデンサ■８により凝
縮され、主仄留塔塔頂受ぽ１９に流れ込む。一方、主蒸
留塔２の塔底油として重油つ・得られる。In the conventional apparatus described above, crude oil is passed through line 21,
Crude oil heat exchanger using high temperature product oil as a heat medium9.10.11,
The crude oil is heated by a crude oil heat exchanger 13 , 14 using the bottom oil 12 and high-temperature pump-around liquid as heating media, and then supplied to the pre-reduction column 1 . Crude oil is steam-distilled in the pre-distillation column 1, and light fractions such as LPG fraction and light naphtha are obtained as top products. After leaving the front distillation column, the bottom oil of the front distillation column is heated in a heating furnace 16, and is heated in a heating furnace 16, and is heated in a heating furnace 16 to form a furanone nitrogen 17 in the main distillation column 2.
is supplied to The top air from the main distillation column is condensed by the main distillation column top condenser 8 using water or air as a refrigerant, and flows into the main distillation column top receiving port 19. On the other hand, heavy oil is obtained as the bottom oil of the main distillation column 2.
前記前留塔塔頂コンデンサ４Ａの冷媒は、一般に水また
は空気であり、前留塔塔頂受槽５Ａに溜まる前留塔塔頂
蒸気凝縮液の温度は３０〜４０°Ｃ程度である。このた
め前留塔塔頂受槽の操作圧力が低いと、オフガスの発生
量が多くなる。したがって、従来は該前留塔塔頂受［５
Ａの操作圧力を２．５〜３．５ｋｇ／ｃｎＧとするのが
通常である。The refrigerant in the fore-stream column overhead condenser 4A is generally water or air, and the temperature of the fore-stream column top vapor condensate collected in the fore-stream column top receiving tank 5A is about 30 to 40°C. Therefore, when the operating pressure of the front column top receiving tank is low, the amount of off-gas generated increases. Therefore, in the past, the front column tower overhead [5
The operating pressure of A is usually 2.5 to 3.5 kg/cnG.
従来の原油常圧蒸留装置において、前留塔１は、水蒸気
蒸留塔（濃縮段２０と塔頂コンデンサ４Ａのみの濃縮塔
）、または単なるフラッシュ塔が用いられるが、いずれ
の場合も塔頂製品と塔底油との分離度はきわめて悪く、
前留塔塔底油中にＬＰＧ留分等の軽質留分が多量に混入
する。前留塔塔底油に混入したＬＰＧ留分等の軽質留分
は、主蒸留塔塔頂コンデンサ１８において凝縮し切れず
、主蒸留塔塔頂受槽１９でオフガスとなる。このため、
主蒸留塔塔頂光Ｎ１９は正圧となり、主蒸留塔塔頂受槽
も正圧となる。−毀に、王莫留塔塔底油である重油中Ｓ
こは、多量の軽油、重質軽油等の重油より価値の高い油
（白油］が多量に混入している。このような重油中に含
まれる白油を回収するには、主蒸留塔フラッシュゾーン
１７で、より多（の白油が薫発するようにするが、この
ためには前留塔塔底油を加熱炉１６においてより高温に
加熱して主蒸留塔に供給する方法、および主蒸留塔フラ
ッシュゾーンの操作圧力をより低（する方法が考えられ
る。しかし前者は、必要とする熱エネルギーが増加し、
また供給温度を高くすると原油の熱分解を生起するため
限度があり、後者は主蒸留塔塔頂受槽１９におけるオフ
ガス発生量が増加し、低下できる圧力に限度がある。In conventional crude oil atmospheric distillation equipment, the front distillation column 1 is a steam distillation column (a concentration column with only a concentration stage 20 and an overhead condenser 4A) or a simple flash column, but in either case, the top product and The degree of separation from the bottom oil is extremely poor.
A large amount of light fractions such as LPG fractions are mixed into the bottom oil of the front distillation column. Light fractions such as LPG fractions mixed in the bottom oil of the front distillation column are not completely condensed in the main distillation column top condenser 18, and become off gas in the main distillation column top receiving tank 19. For this reason,
The main distillation column top light N19 has a positive pressure, and the main distillation column top receiving tank also has a positive pressure. - In addition, Wang Moli tower bottom oil is heavy oil medium S
This contains a large amount of oil (white oil) that is more valuable than heavy oil such as light oil and heavy gas oil.In order to recover the white oil contained in such heavy oil, the main distillation column flash In zone 17, a larger amount of white oil is smoked, but for this purpose, there is a method in which the bottom oil of the front distillation column is heated to a higher temperature in the heating furnace 16 and fed to the main distillation column, and One possibility is to lower the operating pressure in the tower flash zone. However, the former requires more thermal energy and
In addition, there is a limit to increasing the supply temperature because it causes thermal decomposition of the crude oil, and the latter increases the amount of off-gas generated in the main distillation column top receiving tank 19, and there is a limit to the pressure that can be lowered.
本発明の目的は、前記の従来方法の欠点をなくし、前留
塔と主蒸留塔の間の加熱装置の負荷を低減し、大幅な省
エネルギーを図るか、また１；！／および装置全体とし
ての白油収率の改善された原油遺留装置を提供すること
にある。The purpose of the present invention is to eliminate the drawbacks of the conventional methods described above, reduce the load on the heating device between the pre-distillation column and the main distillation column, and achieve significant energy savings. An object of the present invention is to provide a crude oil retention device with an improved white oil yield as a whole.
〔課題を解決するための手段］
本発明の第１は、前留塔と主蒸留塔とから主として構成
される原油遺留装置を用いて原油を遺留する方法におい
て、前留塔の塔頂圧力を０．５〜１゜５ｋｇ／ｃｍ２Ｇ
とし、かつ該前留塔にリボイラおよび軽質油の回収段を
設けることにより該前留塔の塔頂油を増加せしめ、軽質
油の減少した該前留塔の塔底油を主蒸留塔に供給し、蒸
留を行うとともに、主蒸留塔の塔頂蒸気を水または空気
を冷媒として冷却し、凝縮成分を回収し、その結果該主
蒸留塔塔頂圧力を−０，５〜Ｏｋｇ／ｃ−ｊＧに自己減
圧することを特徴とする原油蒸留方法である。[Means for Solving the Problems] A first aspect of the present invention is a method for retaining crude oil using a crude oil retention apparatus mainly composed of a pre-distillation column and a main distillation column, in which the top pressure of the pre-distillation column is reduced. 0.5~1゜5kg/cm2G
and by providing a reboiler and a light oil recovery stage in the pre-distillation column, the top oil of the pre-distillation column is increased, and the bottom oil of the pre-distillation column with reduced light oil is supplied to the main distillation column. At the same time as distillation, the top vapor of the main distillation column is cooled using water or air as a refrigerant, and the condensed components are recovered. This is a crude oil distillation method characterized by self-depressurization.
本発明の第２は、前記第１の発明の原油蒸留方法におい
て前留塔の塔頂から発生するオフガスを５〜２０ｋｇ／
ｄＧに加圧後、水または空気を冷媒として該オフガスを
冷却し、凝縮成分を回収することを特徴とする原油蒸留
装置である。The second aspect of the present invention is to reduce the amount of off-gas generated from the top of the pre-distillation column in the crude oil distillation method according to the first aspect of the present invention by 5 to 20 kg/
This crude oil distillation apparatus is characterized in that after pressurizing dG, the off-gas is cooled using water or air as a refrigerant, and condensed components are recovered.
本発明の第３は、前留塔と主７留塔とから主としてＮｌ
ｔ成される原油蒸留装置を用いて原ン由を蒸留する方法
において、前留塔の塔頂圧力を０．５〜１゜５ｋｇ／ｃ
−ｆｆｌＧとすることにより該前留塔の塔頂油を増加せ
しめ、かつ該前留塔塔頂から発生するオフガスを５〜２
０ｋｇ／ａ！Ｇに加圧後、水または空気を冷媒として該
オフガスを冷却し、凝縮成分を回収するとともに、軽質
油の減少した該前留塔の塔底油を主蒸留塔に供給し、蒸
留を行うとともに、主蒸留塔の塔頂蒸気を水または空気
を冷媒として冷却し、凝縮成分を回収し、その結果該主
蒸留塔塔頂圧力を−０，５〜Ｏｋｇ／ｃｆｌｌＧに自己
減圧することを特徴とする原油蒸留方法である。The third aspect of the present invention is that the pre-reduction column and the main 7-reduction column mainly contain Nl.
In a method of distilling raw materials using a crude oil distillation apparatus, the pressure at the top of the pre-distillation column is set to 0.5 to 1.5 kg/c.
-fflG, the amount of oil at the top of the fore-distillation column is increased, and the off-gas generated from the top of the fore-distillation column is reduced by 5 to 2
0kg/a! After pressurizing G, the off-gas is cooled using water or air as a refrigerant, the condensed components are recovered, and the bottom oil of the pre-distillation column with reduced light oil is supplied to the main distillation column to perform distillation. , the top vapor of the main distillation column is cooled using water or air as a refrigerant, the condensed components are recovered, and as a result, the pressure at the top of the main distillation column is self-reduced to -0.5 to Okg/cfllG. This is a crude oil distillation method.
〔作用］
請求項（１）記載の原油蒸留方法は、前留塔を従来より
低圧（０，５〜１．５ ｋｇ／ｄ Ｇ ）とすることに
より、前留塔に供給される油をより蒸発し易くし従来で
あれば前留塔塔底油中に混入する軽質留分を前留塔塔頂
油として留出せしめ、これにより前留塔かａ王１奮塔に
供給される油は軽質留分がある程度除去されることとな
り、主蒸留塔の塔頂製品がより重質化し、このため主蒸
留塔塔頂コンデンサにて水、空気以外の特別の冷媒を使
って冷却度を高めることなく、また主蒸留塔にて特別の
減圧装置を使うことなく主蒸留塔塔頂受層圧力を０．５
〜Ｏｋｇ／ｃｉＧと減圧にすることができる。[Function] The crude oil distillation method according to claim (1) lowers the pressure of the pre-distillation column (0.5 to 1.5 kg/dG) compared to the conventional method, thereby increasing the oil supplied to the pre-distillation column. The light fraction, which would otherwise be mixed in the bottom oil of the front distillation tower, is distilled out as the top oil of the front distillation tower. As light fractions are removed to some extent, the product at the top of the main distillation column becomes heavier, and therefore a special refrigerant other than water or air is used in the main distillation column top condenser to increase the degree of cooling. In addition, the pressure at the top of the main distillation column can be reduced to 0.5 without using a special pressure reducing device in the main distillation column.
The pressure can be reduced to ~Okg/ciG.
原料油の蒸発量が増加し、このため、従来は重油（主蒸
留塔塔底油）中に混入していた軽油、重質軽油等のより
価値の高い製品油（白油）の収率が高くなり、いわゆる
深絞り効果を生じる。また白油の収率をそれ程高める必
要のない時は、前留塔から主蒸留塔に供給される油の加
熱装置の負荷を低減でき、大幅な省エネルギーを図るこ
とができる。The amount of evaporation of feedstock oil increases, and as a result, the yield of more valuable product oils (white oil) such as light oil and heavy gas oil, which were conventionally mixed in heavy oil (main distillation column bottom oil), has decreased. This results in a so-called deep drawing effect. Furthermore, when there is no need to increase the yield of white oil to that extent, the load on the heating device for oil supplied from the pre-distillation column to the main distillation column can be reduced, resulting in significant energy savings.
本発明において、前留塔を低圧とすることにより、原料
油次第で前留塔塔頂受槽から発生するオフガスが増加す
る場合に、該オフガスを加圧する装置と該加圧されたオ
フガスを冷却して凝縮成分を回収する装置を設けること
は、有価値成分を回収することができるほか、前記前留
塔塔頂受槽の圧力の調節の面からも好ましい。In the present invention, by lowering the pressure in the front distiller, when the amount of off gas generated from the top receiving tank of the front distiller increases depending on the feedstock oil, a device for pressurizing the off gas and a device for cooling the pressurized off gas can be used. Providing a device for recovering condensed components is preferable not only because valuable components can be recovered, but also from the viewpoint of regulating the pressure in the receiving tank at the top of the front distillation column.
また本発明において、前留塔塔頂油の収率が上がる二と
により、前留塔塔頂油との分離度が悪化する場合に、前
留塔番こリボイラおよび軽質油の回収段を設けることは
、前留塔塔頂油の芸留性状を改善することができるほか
、前留塔塔底油中への軽質油の混入を防ぎ、主蒸留塔の
減圧化の面からも好ましい。In addition, in the present invention, when the yield of the oil at the top of the front distillation column increases and the degree of separation from the oil at the top of the front distillation column deteriorates, a front distillation column reboiler and a recovery stage for light oil are provided. This is preferable from the viewpoint of not only improving the distillation properties of the oil at the top of the front distillation column, but also preventing light oil from being mixed into the bottom oil of the front distillation column, and reducing the pressure in the main distillation column.
以下、本発明を図面によりさらに詳細に説明する。 Hereinafter, the present invention will be explained in more detail with reference to the drawings.
第１図は、本発明の一実施例を示す原油蒸留装置の概略
系統図である。第１図に示す本発明の原油蒸留装置は、
前留塔１が回収段２２およびリボイラ３を有する点にお
いて、第４図に示す従来の原油常圧蒸留装置と異なる。FIG. 1 is a schematic system diagram of a crude oil distillation apparatus showing an embodiment of the present invention. The crude oil distillation apparatus of the present invention shown in FIG.
This differs from the conventional crude oil atmospheric distillation apparatus shown in FIG. 4 in that the front distillation column 1 has a recovery stage 22 and a reboiler 3.
第１図において、原油は原油仕込ライン２１を介して、
高温製品油または高温ポンプアラウンド液を熱媒とする
原油熱交換器９．１０，１１．１２．１３および■４に
より昇温され、前留塔ｌのフラッシュゾーン１５に供給
される。In FIG. 1, crude oil is passed through a crude oil feed line 21,
The crude oil heat exchangers 9, 10, 11, 12, 13, and 4 use high-temperature product oil or high-temperature pump-around liquid as a heat medium to raise the temperature, and the crude oil is supplied to the flash zone 15 of the pre-reduction column 1.
前留塔ｌの塔頂低圧受槽５は、０．５〜１．５ｋｇ／Ｃ
１１１Ｇの比較的低圧で運転されるだめ、前留塔フラッ
シュゾーン１５ではＬＰＧ留分、軽質ナフサ等の他に重
質ナフサの一部も蒸発する。The top low pressure receiving tank 5 of the front distillation column 1 has a pressure of 0.5 to 1.5 kg/C.
Since it is operated at a relatively low pressure of 111 G, a portion of the heavy naphtha is also evaporated in the front column flash zone 15 in addition to the LPG fraction, light naphtha, etc.
前留塔すボイラ３および回収段２２の設置により、塔底
油中の軽質留分の回収能力が強化され、フランシュゾー
ン１５における重賞ナフサの蒸発とあいまって塔底油中
の軽質留分が減少する。第１図において、リボイラ３の
熱源は主蒸留塔塔底油である重油であるが、リボイラ３
として専用の加熱炉を設けてもよい。The installation of the pre-column boiler 3 and the recovery stage 22 strengthens the recovery capacity of light fractions in the column bottom oil, and together with the evaporation of heavy naphtha in the Franche zone 15, the light fractions in the column bottom oil are Decrease. In Figure 1, the heat source of reboiler 3 is heavy oil, which is the bottom oil of the main distillation column;
A dedicated heating furnace may also be provided.
前留塔１の塔頂蒸気は水または空気を冷媒とする塔頂低
圧コンデンサ４により冷却凝縮されるが、一部凝縮され
ない成分が生ずることがある。このような非凝縮ガス中
には軽質ナフサ留分が含まれるため、この非凝縮ガスを
第２図に示すようにコンプレッサ６により約５〜１５ｋ
ｇ／ｃ−７Ｇに加圧し、さらに水または空気を冷媒とす
る前留塔塔頂高圧コンデンサ７によって冷却し、ガソリ
ン留分、軽質ナフサ留分を前留塔塔頂高圧受［３内に凝
縮回収することができる。一般一二、前留塔の操作圧力
を下げていくと、塔頂低圧受層５におけるオフガス発生
量が増加する。一方、フラッシュゾーンにおける原油の
蒸発量も増加することによって塔頂製品の収率も増加し
、塔頂製品におけるオフガスの占める分圧が相対的に小
さくなり、オフガス発生を抑制する効果を生し、その発
生量が極端にふえることはない。The overhead vapor of the pre-distillation column 1 is cooled and condensed by an overhead low-pressure condenser 4 using water or air as a refrigerant, but some components may be left uncondensed. Since such non-condensable gas contains a light naphtha fraction, this non-condensable gas is compressed by a compressor 6 of about 5 to 15 kg as shown in FIG.
g/c-7G and further cooled by a high-pressure condenser 7 at the top of the fore-stream column using water or air as a refrigerant, and the gasoline fraction and light naphtha fraction are condensed in the high-pressure receiver at the top of the fore-stream column [3]. It can be recovered. General 12. As the operating pressure of the front distillation column is lowered, the amount of off-gas generated in the low-pressure receiving layer 5 at the top of the column increases. On the other hand, as the amount of evaporation of crude oil in the flash zone increases, the yield of the top product also increases, and the partial pressure occupied by off-gas in the top product becomes relatively small, which has the effect of suppressing off-gas generation. The amount generated will not increase significantly.
このような場合、コンプレッサ６、塔頂高圧コンデンサ
７および塔頂高圧受槽８を設置しなくともよい場合もあ
る。In such a case, the compressor 6, the tower top high pressure condenser 7, and the tower top high pressure receiving tank 8 may not need to be installed.
原油中の軽質留分が充分に除去された前留塔塔底油は、
加熱炉１６で加熱されたのち主蒸留塔２に供給され、主
蒸留塔フランシュゾーン１７において重質ナフサ、灯油
、軽油、重質軽油等の留分が蒸発する。主蒸留塔塔頂蒸
気は水または空気を冷媒とする主蒸留塔塔頂コンデンサ
１８によって全凝縮させるが、前述のように前留塔で軽
質留分が充分除去されているので、王芋留塔塔頂受（可
１９はＯ〜−０，５ｋｚ／ｃゴＧの減圧ａ″態となり、
工芸留塔のフラノンユゾーンｌτの操作圧力を減圧ない
し低圧化することができるため、加熱炉１６の負荷を上
げることなしにフラッシュゾーン１７二こおける原料油
の蒸発量が増加することＳ：よって白油の収率が増加す
ることになる。なお、この場合の減圧度は主芳留塔塔項
コンデンサ１８より留出してくる凝縮液の冷却温度を変
えることにより、調節することができる。また、白油の
収率をそれ程増加させるｌ・要のない場合ユニは、加熱
炉１６の負荷を従来より下げて省エネルギーを図ること
ができる。The bottom oil of the front distillation tower from which the light fractions in the crude oil have been sufficiently removed is
After being heated in the heating furnace 16, it is supplied to the main distillation column 2, and in the main distillation column Franche zone 17, fractions such as heavy naphtha, kerosene, gas oil, and heavy gas oil are evaporated. The vapor at the top of the main distillation column is completely condensed by the main distillation column top condenser 18 which uses water or air as a refrigerant, but as mentioned above, the light fraction has been sufficiently removed in the front distillation column. The tower top receiver (possible 19 becomes the reduced pressure a″ state of O~-0.5kz/c go G,
Since the operating pressure of the furanone zone lτ of the craft distillation column can be reduced or lowered, the amount of evaporation of the feedstock oil in the flash zone 17 increases without increasing the load on the heating furnace 16. The yield of white oil will increase. Note that the degree of pressure reduction in this case can be adjusted by changing the cooling temperature of the condensate distilled from the main distillation column condenser 18. Further, in cases where it is not necessary to increase the yield of white oil by that much, the load on the heating furnace 16 can be lowered compared to the conventional method, thereby saving energy.
以下に、第１図に示す本発明の原油常圧蒸留装置と、第
４図に示す従来の原油常圧蒸留装置の運転例を示す。原
油処理量は５０，０００ハ一レル／日、処理原油はミナ
ス原油１００％である。白油収率を増加せしめる場合の
主な運転条件を第１表に示し、製品得率を第２表に示す
。また省エネルギーを行う場合の主な運転条件を第３表
に示す。Below, examples of operation of the crude oil atmospheric distillation apparatus of the present invention shown in FIG. 1 and the conventional crude oil atmospheric distillation apparatus shown in FIG. 4 will be shown. The amount of crude oil processed is 50,000 ha/day, and the crude oil processed is 100% Minas crude oil. Table 1 shows the main operating conditions for increasing the white oil yield, and Table 2 shows the product yield. Table 3 shows the main operating conditions for energy saving.
第
表
第
表
第２表
以下余白
第１表および第２表の結果から、本発明によれば、加熱
炉の負荷を増加する二となく、遺留状態また製品性状が
良好な状態で、白油収率が改善されたことがわかる。ま
た第３表から必要に応じ加熱炉負荷を低減し、省工ふル
ギー効果を得ることができることがわかる。From the results in Tables 1 and 2, it can be seen that according to the present invention, white oil can be heated without increasing the load on the heating furnace, while maintaining good residual conditions and product properties. It can be seen that the yield was improved. Moreover, from Table 3, it is seen that the load on the heating furnace can be reduced as necessary, and a labor-saving and fuel-saving effect can be obtained.
第３図は、前留塔オフガスの加圧、冷却および凝縮の各
手段ならびに前留塔塔底部にリボイラおよび回収段を設
けた実施例を示す。FIG. 3 shows an embodiment in which means for pressurizing, cooling and condensing the front distiller off-gas, as well as a reboiler and a recovery stage are provided at the bottom of the front distiller.
本発明の原油常圧蒸留装置は、前留塔に回収段およびリ
ボイラを設置し、または／およびオフガスの加圧および
凝縮装置を設け、前留塔を低圧で操作することにより、
前留塔塔底油中へのＬＰＧ留分等の軽質留分の混入が防
止され、主蒸留塔の塔頂製品がより重質になるとともに
、主蒸留塔塔頂受槽におけるオフガスの発生が抑制され
、主蒸留塔の減圧蒸留が可能になる。このため、主蒸留
塔フラッシュゾーンの操作圧力も低下するので、フラッ
シュゾーンにおける原料油のフラッシュ量が増加し、重
油中の軽油、重質軽油等のより価値の高い製品油の収率
が向上する（深絞り効果）。The crude oil atmospheric distillation apparatus of the present invention includes a recovery stage and a reboiler in the front distillation tower, and/or an off-gas pressurization and condensation device, and operates the front distillation tower at low pressure.
This prevents light fractions such as LPG fractions from being mixed into the bottom oil of the front distillation column, making the top product of the main distillation column heavier, and suppressing the generation of off-gas in the main distillation column top receiving tank. This enables vacuum distillation in the main distillation column. As a result, the operating pressure in the main distillation column flash zone also decreases, which increases the amount of feedstock flashed in the flash zone, improving the yield of higher value product oils such as light oil in heavy oil and heavy gas oil. (deep drawing effect).
深絞りの必要の無い時は、主蒸留塔への原油供給温度を
下げることができるので省工享ルギー効果も得られる。When deep drawing is not required, the temperature at which crude oil is supplied to the main distillation column can be lowered, resulting in labor and energy savings.
第１図、第２図および第３図は、それぞれ本発明の原油
常圧蒸留装置の一実施例を示す系統図、第４図は、従来
の原油常圧蒸留装置の一例を示す系統図である。
■・・・前留塔、２・・・主蒸留塔、３・・・前留塔す
ボイラ、４・・・前留塔塔頂低圧コンデンサ、４Ａ・・
・前留塔塔頂コンデンサ、５・・・前留塔塔頂低圧受槽
、５Ａ・・・前留塔塔頂受槽、６・・・コンプレッサ、
７・・・前留塔塔頂高圧コンデンサ、８・・・前留塔塔
頂高圧受槽、９・・・原油熱交換器、ｌＯ・・・原油熱
交換器、１１・・・原油熱交換器、１２・・・原油熱交
換器、１３・・・原油熱交換器、１４・・・原油熱交換
器、１５・・・前留塔フラッシュゾーン、１６・・・加
熱炉、１７・・・主蒸留塔フラッシュゾーン、１８・・
・主蒸留塔塔頂コンデンサ、１９・・・主蒸留塔塔頂受
槽、２０・・・前留塔濃縮段、２１・・・原油仕込ライ
ン、２２・・・回収段。1, 2, and 3 are system diagrams showing an embodiment of the crude oil atmospheric distillation apparatus of the present invention, and FIG. 4 is a system diagram showing an example of a conventional crude oil atmospheric distillation apparatus. be. ■... Pre-distillation column, 2... Main distillation column, 3... Pre-distillation column boiler, 4... Pre-distillation column top low pressure condenser, 4A...
- Front distillation column top condenser, 5... Front distillation column top low pressure receiver tank, 5A... Front distillation column top receiver tank, 6... Compressor,
7... High pressure condenser at the top of the front distillation column, 8... High pressure receiver tank at the top of the front distillation column, 9... Crude oil heat exchanger, lO... Crude oil heat exchanger, 11... Crude oil heat exchanger , 12... Crude oil heat exchanger, 13... Crude oil heat exchanger, 14... Crude oil heat exchanger, 15... Front distiller flash zone, 16... Heating furnace, 17... Main Distillation column flash zone, 18...
- Main distillation column top condenser, 19... Main distillation column top receiving tank, 20... Front distillation column concentration stage, 21... Crude oil charging line, 22... Recovery stage.
Claims (3)
蒸留装置を用いて原油を蒸留する方法において、前留塔
の塔頂圧力を０．５〜１．５ｋｇ／ｃｍ＾２Ｇとし、か
つ該前留塔にリボイラおよび軽質油の回収段を設けるこ
とにより該前留塔の塔頂油を増加せしめ、軽質油の減少
した該前留塔の塔底油を主蒸留塔に供給し、蒸留を行う
とともに、主蒸留塔の塔頂蒸気を水または空気を冷媒と
して冷却し、凝縮成分を回収し、その結果該主蒸留塔塔
頂圧力を−０．５〜０ｋｇ／ｃｍ＾２Ｇに自己減圧する
ことを特徴とする原油蒸留方法。(1) In a method of distilling crude oil using a crude oil distillation apparatus mainly composed of a front distillation column and a main distillation column, the top pressure of the front distillation column is set to 0.5 to 1.5 kg/cm^2G, and increasing the top oil of the pre-distillation column by providing a reboiler and a light oil recovery stage in the pre-distillation column, and supplying the bottom oil of the pre-distillation column with reduced light oil to the main distillation column; At the same time as distillation, the top vapor of the main distillation column is cooled using water or air as a refrigerant, and the condensed components are recovered. A crude oil distillation method characterized by reducing pressure.
の塔頂から発生するオフガスを５〜２０ｋｇ／ｃｍ＾２
Ｇに加圧後、水または空気を冷媒として該オフガスを冷
却し、凝縮成分を回収することを特徴とする原油蒸留方
法。(2) In the crude oil distillation method according to claim (1), the amount of off-gas generated from the top of the pre-distillation column is 5 to 20 kg/cm^2.
A crude oil distillation method characterized in that after pressurizing G, the off-gas is cooled using water or air as a refrigerant, and condensed components are recovered.
蒸留装置を用いて原油を蒸留する方法において、前留塔
の塔頂圧力を０．５〜１．５ｋｇ／ｃｍ＾２Ｇとするこ
とにより該前留塔の塔頂油を増加せしめ、かつ該前留塔
塔頂から発生するオフガスを５〜２０ｋｇ／ｃｍ＾Ｇに
加圧後、水または空気を冷媒として該オフガスを冷却し
、凝縮成分を回収するとともに、軽質油の減少した該前
留塔の塔底油を主蒸留塔に供給し、蒸留を行うとともに
、主蒸留塔の塔頂蒸気を水または空気を冷媒として冷却
し、凝縮成分を回収し、その結果該主蒸留塔塔頂圧力を
−０．５〜０ｋｇ／ｃｍ＾２Ｇに自己減圧することを特
徴とする原油蒸留方法。(3) In a method of distilling crude oil using a crude oil distillation apparatus mainly consisting of a front distillation column and a main distillation column, the top pressure of the front distillation column is set to 0.5 to 1.5 kg/cm^2G. By increasing the oil at the top of the fore-distillation column, and after pressurizing the off-gas generated from the top of the fore-distillation column to 5 to 20 kg/cm^G, cooling the off-gas using water or air as a refrigerant, While recovering the condensed components, supplying the bottom oil of the pre-distillation column with reduced light oil to the main distillation column to perform distillation, and cooling the top vapor of the main distillation column using water or air as a refrigerant, A method for distilling crude oil, characterized in that the condensed components are recovered and, as a result, the pressure at the top of the main distillation column is self-reduced to -0.5 to 0 kg/cm^2G.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP23301290A JPH0692583B2 (en) | 1990-09-03 | 1990-09-03 | Crude oil distillation method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP23301290A JPH0692583B2 (en) | 1990-09-03 | 1990-09-03 | Crude oil distillation method |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH04114088A true JPH04114088A (en) | 1992-04-15 |
| JPH0692583B2 JPH0692583B2 (en) | 1994-11-16 |
Family
ID=16948434
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP23301290A Expired - Lifetime JPH0692583B2 (en) | 1990-09-03 | 1990-09-03 | Crude oil distillation method |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH0692583B2 (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US7172686B1 (en) | 2002-11-14 | 2007-02-06 | The Board Of Regents Of The University Of Oklahoma | Method of increasing distillates yield in crude oil distillation |
-
1990
- 1990-09-03 JP JP23301290A patent/JPH0692583B2/en not_active Expired - Lifetime
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US7172686B1 (en) | 2002-11-14 | 2007-02-06 | The Board Of Regents Of The University Of Oklahoma | Method of increasing distillates yield in crude oil distillation |
Also Published As
| Publication number | Publication date |
|---|---|
| JPH0692583B2 (en) | 1994-11-16 |
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