JPH0613709B2 - Fractional distillation of oil under hydrogen atmosphere - Google Patents
Fractional distillation of oil under hydrogen atmosphereInfo
- Publication number
- JPH0613709B2 JPH0613709B2 JP11420585A JP11420585A JPH0613709B2 JP H0613709 B2 JPH0613709 B2 JP H0613709B2 JP 11420585 A JP11420585 A JP 11420585A JP 11420585 A JP11420585 A JP 11420585A JP H0613709 B2 JPH0613709 B2 JP H0613709B2
- Authority
- JP
- Japan
- Prior art keywords
- hydrogen
- oil
- distillation column
- gas
- 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.)
- Expired - Lifetime
Links
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- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Description
【発明の詳細な説明】 （産業上の利用分野） 本発明は、蒸留塔の塔頂材料の腐食の問題のない水素雰
囲気下での油の分留方法に関する。Description: TECHNICAL FIELD The present invention relates to a method for fractionating oil under a hydrogen atmosphere, which is free from the problem of corrosion of the overhead material of a distillation column.
（従来の技術） 従来の原油蒸留の概要フローシートを第４図に示す。第
４図において、ライン１からの原油１０１は、ライン２
からの水蒸気１０２と混合された後、加熱炉３で３５０
〜４００℃に昇温され、蒸留塔４へ供給される。蒸留塔
４の運転圧力は、常圧付近である。(Prior Art) A schematic flow sheet of conventional crude oil distillation is shown in FIG. In FIG. 4, crude oil 101 from line 1 is
350 in the heating furnace 3 after being mixed with steam 102 from
The temperature is raised to ˜400 ° C. and supplied to the distillation column 4. The operating pressure of the distillation column 4 is near normal pressure.
蒸留塔４塔底から、さらにストリツピング用にライン５
から水蒸気が注入され、原油は、ナフサ１０４、灯油１
０５、軽質軽油１０６、重質軽油１０７および残渣油１
０８に分留される。通常、蒸留塔４の塔頂よりナフサ１
０４、塔側より灯油１０５、軽質軽油１０６及び重質軽
油、塔底より残渣油１０８が取出される。蒸留塔４の塔
底より注入された水蒸気１０３は、塔頂を出て、凝縮器
６に入り、冷却され、凝縮槽７で凝縮され凝縮水１０９
となる。なお、１１０はオフガスを示す。水蒸気の凝縮
に際し、蒸留塔４の塔頂温度が水蒸気の露点近くになる
と、塔頂で水蒸気が凝縮し、塔頂材料腐食の原因となる
ので露点より高い温度で運転する。From the bottom of the distillation column 4 to line 5 for stripping
Water vapor is injected from the crude oil, naphtha 104, kerosene 1
05, light gas oil 106, heavy gas oil 107 and residual oil 1
Fractionated to 08. Usually, naphtha 1 from the top of distillation column 4
04, kerosene 105, light gas oil 106 and heavy gas oil from the tower side, and residual oil 108 from the tower bottom. The steam 103 injected from the bottom of the distillation column 4 exits from the top of the column, enters the condenser 6, is cooled, is condensed in the condensing tank 7, and is condensed water 109.
Becomes In addition, 110 shows off gas. When the temperature of the top of the distillation column 4 approaches the dew point of the steam during the condensation of the steam, the steam condenses at the top of the tower and causes corrosion of the material at the top of the distillation column, so the operation is performed at a temperature higher than the dew point.
かかる従来の原油蒸留方法の欠点は、(1)熱回収が十分
出来ない事、(2)ストリツピング用に系外から水蒸気を
導入しなければならない事、(3)凝縮水を廃水するため
には処理が必要である事である。Disadvantages of such conventional crude oil distillation methods are (1) heat recovery is not sufficient, (2) steam must be introduced from outside the system for stripping, and (3) in order to drain condensed water. That is, processing is necessary.
（発明が解決しようとする問題点） 本発明の目的は、上記従来方法の欠点を解消し、蒸留塔
の塔頂材料腐食の問題のない水素雰囲気下での油の分留
方法を提供することである。(Problems to be Solved by the Invention) An object of the present invention is to solve the above-mentioned drawbacks of the conventional method and to provide a method for fractionating oil under a hydrogen atmosphere without the problem of corrosion of the top material of a distillation column. Is.
（問題点を解決するための手段） 本発明は、油の分留において、加熱炉前流に水素を含む
ガスを少量供給すると同時に、系内の水素リツチガスを
蒸留塔の塔頂から凝縮器に導き、冷却凝縮させた上で凝
縮槽にてナフサと水素リツチガスとに分離した後、水素
リツチガスを圧縮機で昇圧し、ストリツピングガスとし
て蒸留塔塔底と加熱炉前流へ導き、再循環利用すること
を特徴とする水素雰囲気下での油の分留方法に関する。(Means for Solving Problems) In the fractional distillation of oil, the present invention is to supply a small amount of hydrogen-containing gas to the upstream of the heating furnace, and at the same time, to supply hydrogen-rich gas in the system from the top of the distillation column to the condenser. It is introduced, cooled and condensed, and then separated into naphtha and hydrogen-rich gas in a condensing tank, then the hydrogen-rich gas is boosted by a compressor and introduced as stripping gas to the bottom of the distillation column and the upstream of the heating furnace, and recycled. The present invention relates to a method for fractionating oil under a hydrogen atmosphere, which is characterized by being used.
（作用） 第１図に、本発明方法の概要フローシートを示す。(Operation) FIG. 1 shows a schematic flow sheet of the method of the present invention.
従来、原油蒸留塔でストリツピング用に使用されていた
水蒸気の代りに、本発明では、加熱炉３の前流に水素を
含むガスをライン２８より少量供給し、かつ、凝縮器６
を経て凝縮槽７で分離した水素リツチガス１１１を圧縮
機８で、圧縮循環し、水素リツチガス１１２及び１１３
としてストリツピング用に使用する事により、水蒸気を
使用する事なく原油を効率よく分留するものである。In the present invention, a small amount of hydrogen-containing gas is supplied from the line 28 to the upstream of the heating furnace 3 instead of steam conventionally used for stripping in a crude oil distillation column, and the condenser 6
The hydrogen-rich gas 111 separated in the condensing tank 7 via the compressor 8 is compressed and circulated by the compressor 8 to generate hydrogen-rich gas 112 and 113.
Is used for stripping to efficiently fractionate crude oil without using steam.
第１図において、蒸留塔４の塔底より注入する水素リツ
チガス１１２を塔頂より回収して分離、圧縮循環し、オ
フガス１１６の量を制御することにより循環量を任意に
選ぶ事が出来、原油１０１を重質ナフサ１１４、灯油１
０５、軽質軽油１０６、重質軽油１０７および残渣油１
０８を一本の蒸留塔４で且つ軽質ナフサ１１５を凝縮槽
７で分留出来る。また、水素リツチガス１１２をストリ
ツピングに使用し、蒸留塔４を水素雰囲気下で運転する
ため、蒸留塔４の塔頂での水蒸気の露点が低くなり、腐
食の問題なしに塔頂温度を下げて運転出来る。その為、
塔頂部での熱回収が向上する。In FIG. 1, the hydrogen-rich gas 112 injected from the bottom of the distillation column 4 is recovered from the top of the column, separated, compressed and circulated, and the amount of offgas 116 can be controlled to arbitrarily select the circulation amount. 101 for heavy naphtha 114, kerosene 1
05, light gas oil 106, heavy gas oil 107 and residual oil 1
08 can be fractionated in one distillation column 4 and light naphtha 115 can be fractionated in the condensing tank 7. Further, since the hydrogen lit gas 112 is used for stripping and the distillation column 4 is operated in a hydrogen atmosphere, the dew point of water vapor at the top of the distillation column 4 becomes low, and the column top temperature can be lowered without causing corrosion problems. I can. For that reason,
Heat recovery at the top of the tower is improved.
一方、従来法では、第４図に示すように、蒸留塔４の塔
底で注入した水蒸気１０３は、塔頂で凝縮し、凝縮器６
の負荷が大きかつたが、本発明の方法では、水素リツチ
ガスの顕熱のみを取除けばよく、凝縮器負荷が著しく低
減できる。なお、原油の他に、軽質油、重質油、石炭液
化油、シエールオイル、タールサンド油、コールタール
等の分留についても、本発明の方法は適用できる。On the other hand, in the conventional method, as shown in FIG. 4, the water vapor 103 injected at the bottom of the distillation column 4 is condensed at the top of the column and condensed in the condenser 6
However, in the method of the present invention, only the sensible heat of the hydrogen-rich gas needs to be removed, and the condenser load can be significantly reduced. In addition to crude oil, the method of the present invention can be applied to fractional distillation of light oil, heavy oil, coal liquefied oil, shale oil, tar sand oil, coal tar and the like.
また、本発明方法における蒸留塔４の操作条件として
は、圧力０〜１０kg／cm2Ｇ、温度１００〜５００℃が
適当である。Further, as operating conditions of the distillation column 4 in the method of the present invention, a pressure of 0 to 10 kg / cm 2 G and a temperature of 100 to 500 ° C. are suitable.
このように、本発明方法は、原油、軽質油、重質油の分
留、不活性ガスを含む多成分系の分留、コールタールの
分留、水素化分解装置や水素化精製装置の蒸留工程、石
炭液化油、タールサンド油、シエールオイルの分留、そ
の他類似の分留工程に広く適用できる。As described above, the method of the present invention comprises fractionation of crude oil, light oil, heavy oil, fractionation of a multi-component system containing an inert gas, fractionation of coal tar, distillation of hydrocracker and hydrorefining equipment. It can be widely applied to the process, fractionation of coal liquefied oil, tar sands oil, sheer oil, and other similar fractionation processes.
（実施例） 以下、アラビアンライト原油を本発明の分留方法で各留
分に分離した実施例について説明する。(Example) Hereinafter, an example in which Arabian light crude oil is separated into each fraction by the fractionation method of the present invention will be described.
本実施例の概略フローシートを第２図に示す。これは、
加熱炉３、蒸留塔４、凝縮器６、凝縮槽７、圧縮機８、
原油導管１１、水素リツチガス供給導管９，１０、供給
水素導管１２から成り、蒸留塔４の矢印側線は、各留分
の分離を示し、その段数は４２段である。A schematic flow sheet of this example is shown in FIG. this is,
Heating furnace 3, distillation column 4, condenser 6, condensing tank 7, compressor 8,
It consists of a crude oil conduit 11, hydrogen-rich gas supply conduits 9 and 10, and a supply hydrogen conduit 12, and the arrow side line of the distillation column 4 indicates the separation of each fraction, and the number of plates is 42.
原油（アラビアンライト原油）１０１を原油導管１１に
より、加熱炉炉３に送り、又原油導管１１および蒸留塔
４の塔底に、水素リツチガス導管９，１０を通じて原油
１m3当り２４Nm3の水素リツチガス（加熱炉前流に１０
％、蒸留塔に９０％）を注入し分留する。加熱炉３の出
口温度３４６℃、蒸留塔３の運転圧力０．８kg／cm2Ｇ
である。なお１１６はオフガスを示す。Crude oil (Arabian light crude oil) 101 is sent to the heating furnace 3 through the crude oil conduit 11, and 24 Nm 3 of hydrogen rich gas per 1 m 3 of crude oil is supplied to the crude oil conduit 11 and the bottom of the distillation column 4 through the hydrogen rich gas conduits 9 and 10. 10 in front of heating furnace
%, 90%) into the distillation column and fractionally distilled. The outlet temperature of the heating furnace 3 is 346 ° C., the operating pressure of the distillation column 3 is 0.8 kg / cm 2 G
Is. Reference numeral 116 represents off gas.
この蒸留塔４において分留された成分を第１表に示す。The components fractionated in this distillation column 4 are shown in Table 1.
この分離状態を、ASTM D-2892曲線により第３図に示
す。 This separated state is shown in FIG. 3 by the ASTM D-2892 curve.
この実施例の結果から、塔頂の水蒸気露点は、従来法の
９５℃に対し５０℃、凝縮器負荷は、従来法を１００と
すれば５６となり、著しい凝縮器負荷の軽減が出来た。
すなわち、原油蒸留に於て、水蒸気注入する事なく分留
が達成され、凝縮器負荷は、従来のものの５６％で、し
かも、通常の炭素鋼を用いて塔を建設できる事が判明し
た。From the results of this example, the water vapor dew point at the top of the column was 50 ° C. as compared with 95 ° C. in the conventional method, and the condenser load was 56 when the conventional method was 100, and the condenser load was remarkably reduced.
That is, it was found that in crude oil distillation, fractional distillation was achieved without injecting steam, the condenser load was 56% of the conventional one, and the column could be constructed using ordinary carbon steel.
（発明の効果） (1)本発明によれば、加熱炉前流に供給水素を混入し、
さらに系内を循環する水素リツチガスを凝縮槽で分離
後、圧縮機で圧縮循環し、ストリツピング用に用いる事
により、水蒸気を用いる事なく分留出来る。(Effects of the Invention) (1) According to the present invention, hydrogen is mixed in the upstream of the heating furnace,
Furthermore, after separating hydrogen hydrogen gas circulating in the system in a condensing tank, it is compressed and circulated in a compressor and used for stripping, whereby fractionation can be performed without using steam.
(2)循環系からパージするオフガスの量を制御すること
により、圧縮機で圧縮循環する循環量が任意に選べる事
ができる。(2) By controlling the amount of off-gas to be purged from the circulation system, the circulation amount to be compressed and circulated in the compressor can be arbitrarily selected.
(3)水素雰囲気下で蒸留する事により、塔頂での腐食を
防止でき、通常の炭素鋼を用いて塔を建設できる。ま
た、塔頂温度を下げて運転する事により、熱回収を向上
できる。(3) By distilling under a hydrogen atmosphere, corrosion at the top of the tower can be prevented, and the tower can be constructed using ordinary carbon steel. In addition, heat recovery can be improved by lowering the column top temperature for operation.
(4)塔頂ガスの凝縮は水素リツチガスの顕熱のみを取除
けばよく凝縮器負荷が著しく低減できる。(4) Condensation of the overhead gas only needs to remove the sensible heat of the hydrogen-rich gas, and the condenser load can be significantly reduced.
【図面の簡単な説明】 第１図は、本発明方法の概要フローシート、第２図は、
実施例の概要フローシート、第３図は、実施例における
原油の分離状態を示すASTM曲線である。第４図は、従来
方法の概要フローシートである。BRIEF DESCRIPTION OF THE DRAWINGS FIG. 1 is a schematic flow sheet of the method of the present invention, and FIG.
Outline Flow Sheet of Example, FIG. 3 is an ASTM curve showing a separated state of crude oil in the example. FIG. 4 is a schematic flow sheet of the conventional method.
Claims (1)
むガスを少量供給すると同時に、系内の水素リツチガス
を蒸留塔の塔頂から凝縮器に導き、冷却凝縮させた上で
凝縮槽にてナフサと水素リツチガスとに分離した後、水
素リツチガスを圧縮機で昇圧し、ストリツピングガスと
して蒸留塔塔底と加熱炉前流へ導き、再循環利用するこ
とを特徴とする水素雰囲気下での油の分留方法。1. In oil fractional distillation, a small amount of hydrogen-containing gas is supplied to the upstream of the heating furnace, and at the same time, the hydrogen-rich gas in the system is introduced from the top of the distillation column to a condenser, cooled and condensed, and then condensed. After separating it into naphtha and hydrogen-rich gas in the tank, the hydrogen-rich gas is pressurized by a compressor and led as stripping gas to the bottom of the distillation column and to the upstream of the heating furnace for recycle use. How to fractionate oil below.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP11420585A JPH0613709B2 (en) | 1985-05-29 | 1985-05-29 | Fractional distillation of oil under hydrogen atmosphere |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP11420585A JPH0613709B2 (en) | 1985-05-29 | 1985-05-29 | Fractional distillation of oil under hydrogen atmosphere |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS61272286A JPS61272286A (en) | 1986-12-02 |
| JPH0613709B2 true JPH0613709B2 (en) | 1994-02-23 |
Family
ID=14631839
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP11420585A Expired - Lifetime JPH0613709B2 (en) | 1985-05-29 | 1985-05-29 | Fractional distillation of oil under hydrogen atmosphere |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH0613709B2 (en) |
Families Citing this family (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103706139B (en) * | 2013-12-29 | 2015-09-09 | 康乃尔化学工业股份有限公司 | Nitrobenzene vaporization rectifying blender |
| JP6676364B2 (en) * | 2015-12-18 | 2020-04-08 | 株式会社テイエルブイ | Steam injection device |
-
1985
- 1985-05-29 JP JP11420585A patent/JPH0613709B2/en not_active Expired - Lifetime
Also Published As
| Publication number | Publication date |
|---|---|
| JPS61272286A (en) | 1986-12-02 |
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