JPH0130522B2 - - Google Patents
Info
- Publication number
- JPH0130522B2 JPH0130522B2 JP56210019A JP21001981A JPH0130522B2 JP H0130522 B2 JPH0130522 B2 JP H0130522B2 JP 56210019 A JP56210019 A JP 56210019A JP 21001981 A JP21001981 A JP 21001981A JP H0130522 B2 JPH0130522 B2 JP H0130522B2
- Authority
- JP
- Japan
- Prior art keywords
- temperature
- distillation column
- control
- column
- pressure
- 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
Links
- 238000000034 method Methods 0.000 claims description 22
- 238000004821 distillation Methods 0.000 claims description 20
- 239000000446 fuel Substances 0.000 claims description 13
- 238000010438 heat treatment Methods 0.000 claims description 8
- 238000004525 petroleum distillation Methods 0.000 claims description 2
- 239000007788 liquid Substances 0.000 description 10
- 238000010992 reflux Methods 0.000 description 9
- 238000002485 combustion reaction Methods 0.000 description 8
- 238000007796 conventional method Methods 0.000 description 7
- 230000001276 controlling effect Effects 0.000 description 6
- 238000010586 diagram Methods 0.000 description 3
- 238000007670 refining Methods 0.000 description 2
- 230000000052 comparative effect Effects 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 239000003208 petroleum Substances 0.000 description 1
- 238000005504 petroleum refining Methods 0.000 description 1
- 238000003908 quality control method Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
Landscapes
- 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】
本発明は蒸留塔の温度制御方法に関し、詳しく
は石油の蒸留精製にあたり、蒸留塔内の温度制御
性の向上と加燃炉の燃料消費量の節減を図つた蒸
留塔の温度制御方法に関する。DETAILED DESCRIPTION OF THE INVENTION The present invention relates to a method for controlling the temperature of a distillation column, and more specifically, a method for controlling the temperature of a distillation column, which is used in the distillation refining of petroleum, and which improves temperature controllability in the distillation column and reduces fuel consumption in a combustion furnace. The present invention relates to a temperature control method.
従来、石油の蒸留精製における蒸留塔の温度制
御は、塔頂の温度に関しては還流量を変化させる
ことによつて制御し、一方、塔底の温度に関して
は加燃炉への燃料供給量を変化させることによつ
て制御するという如く、蒸留塔の塔頂温度と塔底
温度の制御を別個に行なつていた（第１図参照）。
そのため、双方の温度制御が干渉して最適な温度
制御を行なうことが極めて困難であり、またその
結果として製品の品質管理上また設備管理上余剰
の還流をせざるを得ず、それだけ多大な燃量を必
要としていた。 Conventionally, the temperature of a distillation column in petroleum distillation refining is controlled by changing the reflux amount to control the temperature at the top of the column, and by changing the amount of fuel supplied to the combustion furnace to control the temperature at the bottom of the column. The top temperature and bottom temperature of the distillation column were controlled separately (see Figure 1).
As a result, both temperature controls interfere, making it extremely difficult to perform optimal temperature control.As a result, for product quality control and facility management reasons, surplus must be recirculated, resulting in a large amount of combustion. I needed quantity.
本発明はこのような不都合を解消した蒸留塔の
温度制御方法を提供することを目的とし、その構
成は、石油の蒸留塔の温度を制御する方法におい
て、当該蒸留塔内の上部２割の部分乃至頂部の範
囲の温度を検出して得られる温度信号と、加燃炉
に供給する燃料の供給圧力を検出して得られる圧
力信号とにより、加燃炉に供給する燃料の圧力制
御弁をカスケード制御して蒸留塔塔底温度をコン
トロールすることを特徴とする蒸留塔の温度制御
方法である。 An object of the present invention is to provide a method for controlling the temperature of a distillation column that eliminates such inconveniences. The pressure control valve for the fuel supplied to the combustion furnace is cascaded based on the temperature signal obtained by detecting the temperature in the range from the top to the top, and the pressure signal obtained by detecting the supply pressure of the fuel supplied to the combustion furnace. This is a method for controlling the temperature of a distillation column, characterized in that the temperature at the bottom of the distillation column is controlled.
本発明の方法は、蒸留塔内の上部温度と底部温
度とを別個に制御していた従来法とは異なり、両
者の温度を関連付け一元的に制御することに大き
な特徴を有する。この本発明の方法を従来法と比
較しながら図面に基いて説明すれば次の如くであ
る。第１図は従来法の一例を示す工程図である
が、この従来法によれば、まず原料油を蒸留塔１
に張込んで蒸留し、得られた塔頂蒸気は塔頂より
抜出して冷却器２で冷却して一部を凝縮させ受槽
３へ導く。この受槽３の液は塔頂温度制御のため
に一部還流させ、残りを製品として取出す。ここ
で液の還流量は塔頂の温度検出器６からの温度信
号と流量検出器７からの流量信号とによりカスケ
ード制御を行なつて流量調節弁５を制御し、適切
な流量に調節している。このように還流量を調節
することにより、塔頂温度を所望の範囲に調節し
ているのである。なお、受槽３中のガスは他へ抜
き出され、系内の圧力は一定に保持されている。
一方、塔底の液は一部抜出してポンプ１２により
加熱炉１０に導入し、ここで熱を与えて蒸留塔１
に返す。このとき、加燃炉出口の温度を温度検出
器８にて検出すると共に、圧力検出器９にて燃料
供給量を検出することによりカスケード制御を行
なつて燃料の供給量を決定している。このような
燃料の供給量の制御を行なうことにより、塔底温
度を所望範囲に調節しているのである。なお、こ
こで塔底液の一部は冷却器１３で冷却して製品と
して抜出す。 The method of the present invention differs from the conventional method in which the top temperature and bottom temperature within the distillation column are controlled separately, and is characterized in that both temperatures are linked and controlled in a unified manner. The method of the present invention will be explained below with reference to the drawings while comparing it with the conventional method. Figure 1 is a process diagram showing an example of a conventional method.
The vapor obtained at the top of the tower is extracted from the top of the tower, cooled by a cooler 2, and partially condensed, and led to a receiving tank 3. A portion of the liquid in the receiving tank 3 is refluxed to control the temperature at the top of the tower, and the remainder is taken out as a product. Here, the reflux amount of the liquid is adjusted to an appropriate flow rate by performing cascade control using the temperature signal from the temperature detector 6 at the top of the tower and the flow rate signal from the flow rate detector 7 to control the flow rate regulating valve 5. There is. By adjusting the reflux amount in this way, the tower top temperature is controlled within a desired range. Note that the gas in the receiving tank 3 is extracted elsewhere, and the pressure within the system is maintained constant.
On the other hand, a part of the liquid at the bottom of the column is extracted and introduced into a heating furnace 10 by a pump 12, where heat is applied to the distillation column 1.
Return to. At this time, a temperature detector 8 detects the temperature at the outlet of the combustion furnace, and a pressure detector 9 detects the amount of fuel supplied, thereby performing cascade control to determine the amount of fuel supplied. By controlling the amount of fuel supplied in this manner, the bottom temperature of the column is adjusted within a desired range. Note that here, a part of the bottom liquid is cooled by a cooler 13 and extracted as a product.
このように、上記従来法では塔頂の温度制御と
塔底の温度制御を全く別々に無関係に行なつてい
るため、互いに干渉して最適な温度制御が困難で
ある。 As described above, in the above-mentioned conventional method, the temperature control at the top of the column and the temperature control at the bottom are performed completely separately and unrelatedly, so that they interfere with each other, making it difficult to control the temperature optimally.
これに対して本発明の方法（第２図参照）によ
れば、まず原料油を蒸留塔１に張込んで蒸留し、
得られた塔頂蒸気は塔頂より抜出して冷却器２で
冷却して一部を凝縮させ受槽３へ導く。この受槽
３の液は一部を還流させ、残りを製品として取出
す。ここで液の還流量は塔頂製品の抜出し量に対
して一定の比率とし、温度制御から切離されてい
る。従つて、塔上部乃至塔頂の温度検出器６と流
量検出器７とのカスケード制御は不要である。ま
た塔底の液は一部抜出してポンプ１２により加熱
炉１０に導入し、ここで熱を与えて蒸留塔１に返
す。この際、加熱炉１０に供給する燃料の供給圧
力を圧力検出器９にて検出して圧力信号とすると
共に、蒸留塔１の上部、具体的には塔の上部２割
の部分乃至頂部の範囲の適宜位置の温度を温度検
出器６にて検出して温度信号とし、この両信号に
よりカスケード制御を行ない、加熱炉１０に供給
する燃料の圧力制御弁１１を調節する。このよう
に蒸留塔１の上部の温度を考慮しながら、燃料の
圧力制御弁を制御して塔底温度をコントロールす
る本発明の方法は、塔内の温度を一元的に制御す
るものであり、従来法に比べて格段にすぐれたも
のである。 On the other hand, according to the method of the present invention (see Fig. 2), the raw oil is first charged into the distillation column 1 and distilled.
The obtained tower top vapor is extracted from the top of the tower, cooled by a cooler 2, partially condensed, and led to a receiving tank 3. A part of the liquid in the receiving tank 3 is refluxed, and the rest is taken out as a product. Here, the amount of liquid reflux is set at a constant ratio to the amount of product withdrawn from the top of the column, and is separated from temperature control. Therefore, cascade control of the temperature detector 6 and the flow rate detector 7 at the top of the tower is not necessary. A portion of the liquid at the bottom of the column is extracted and introduced into a heating furnace 10 by a pump 12, where it is heated and returned to the distillation column 1. At this time, the supply pressure of the fuel supplied to the heating furnace 10 is detected by the pressure detector 9 and used as a pressure signal, and the upper part of the distillation column 1, specifically, the upper 20% of the column or the top area. The temperature at an appropriate position is detected by a temperature detector 6 and used as a temperature signal, and cascade control is performed using these two signals to adjust the pressure control valve 11 for fuel supplied to the heating furnace 10. In this way, the method of the present invention, which controls the bottom temperature by controlling the fuel pressure control valve while considering the temperature at the upper part of the distillation column 1, centrally controls the temperature inside the column. This method is significantly superior to conventional methods.
上述した本発明の方法によれば、塔頂あるいは
塔上部の温度制御と塔底あるいは塔下部の温度制
御の干渉がなくなり、温度制御の精度が一段と向
上し、還流比も最低に調節することができる。ま
たその結果として、加燃炉で燃焼させるべき燃料
の消費量が、従来の方法に比べて５〜７％節減で
きる。 According to the method of the present invention described above, there is no interference between the temperature control at the top or upper part of the column and the temperature control at the bottom or lower part of the column, the accuracy of temperature control is further improved, and the reflux ratio can be adjusted to the minimum. can. As a result, the amount of fuel to be burned in the furnace can be reduced by 5 to 7% compared to conventional methods.
従つて本発明の方法は、石油精製をはじめとし
て石油化学工業、化学工業の分野に広く利用する
ことができる。 Therefore, the method of the present invention can be widely used in the fields of petroleum refining, petrochemical industry, and chemical industry.
次に本発明の実施例を示す。 Next, examples of the present invention will be shown.
実施例
LPGとナフサの混合物を水添脱硫し、この処
理油を原料として脱ブタン処理する際の脱ブタン
塔として第２図に示す蒸留塔ならびにその工程を
使用した。その結果、塔頂液の還流量の変化、塔
頂温度変化および加燃炉出口温度変化はそれぞれ
第３図ａ、第４図ａ、第５図ａのとおりであつ
た。Example A mixture of LPG and naphtha was hydrodesulfurized, and the distillation column shown in FIG. 2 and its process were used as a debutanizer when debutanizing the treated oil as a raw material. As a result, the changes in the reflux amount of the tower top liquid, the changes in the tower top temperature, and the changes in the combustion furnace outlet temperature were as shown in Fig. 3a, Fig. 4a, and Fig. 5a, respectively.
比較例
実施例において第２図に示される工程の代わり
に第１図に示される工程を使用したこと以外は実
施例と同様に操作した。その結果、塔頂液の還流
量の変化、塔頂温度変化および加燃炉出口温度変
化はそれぞれ第３図ｂ、第４図ｂ、第５図ｂのと
おりであつた。Comparative Example The procedure was the same as in the example except that the process shown in FIG. 1 was used instead of the process shown in FIG. 2 in the example. As a result, the changes in the reflux amount of the tower top liquid, the changes in the tower top temperature, and the changes in the combustion furnace outlet temperature were as shown in FIG. 3b, FIG. 4b, and FIG. 5b, respectively.
なお、第３図ａおよびｂにおける縦軸の数値は
計器指示値であり、この値に流量係数350を乗じ
た値が実際の還流量（Kl／日）となる。 Note that the numerical values on the vertical axis in FIGS. 3a and 3b are meter indication values, and the value obtained by multiplying this value by a flow rate coefficient of 350 becomes the actual reflux amount (Kl/day).
第１図は従来法の一例を示す工程図であり、第
２図は本発明の方法の一態様を示す工程図であ
る。第３図は塔頂液の還流量の変化、第４図は塔
頂温度変化、第５図は加熱炉出口温度変化を示す
グラフである。
１……蒸留塔、２……冷却器、３……受槽、４
……ポンプ、５……流量調節弁、６……温度検出
器、７……流量検出器、８……温度検出器、９…
…圧力検出器、１０……加熱炉、１１……圧力制
御弁、１２……ポンプ、１３……冷却器。
FIG. 1 is a process diagram showing an example of a conventional method, and FIG. 2 is a process diagram showing one embodiment of the method of the present invention. FIG. 3 is a graph showing changes in the reflux amount of tower top liquid, FIG. 4 is a graph showing changes in tower top temperature, and FIG. 5 is a graph showing changes in heating furnace outlet temperature. 1... Distillation column, 2... Cooler, 3... Receiving tank, 4
... Pump, 5 ... Flow control valve, 6 ... Temperature detector, 7 ... Flow rate detector, 8 ... Temperature detector, 9 ...
...Pressure detector, 10...Heating furnace, 11...Pressure control valve, 12...Pump, 13...Cooler.
Claims (1)
て、当該蒸留塔内の上部２割の部分乃至頂部の範
囲の温度を検出して得られる温度信号と、加熱炉
に供給する燃料の供給圧力を検出して得られる圧
力信号とにより、加熱炉に供給する燃料の圧力制
御弁をカスケード制御して蒸留塔塔底温度をコン
トロールすることを特徴とする蒸留塔の温度制御
方法。1 In a method for controlling the temperature of a petroleum distillation column, a temperature signal obtained by detecting the temperature in the upper 20% of the distillation column or the top, and the supply pressure of fuel supplied to the heating furnace are detected. A method for controlling the temperature of a distillation column, characterized in that the temperature at the bottom of the distillation column is controlled by cascading control of pressure control valves for fuel supplied to a heating furnace using a pressure signal obtained by the above-mentioned pressure signal.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP21001981A JPS58128103A (en) | 1981-12-28 | 1981-12-28 | Temperature controlling method of distilling column |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP21001981A JPS58128103A (en) | 1981-12-28 | 1981-12-28 | Temperature controlling method of distilling column |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS58128103A JPS58128103A (en) | 1983-07-30 |
| JPH0130522B2 true JPH0130522B2 (en) | 1989-06-20 |
Family
ID=16582472
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP21001981A Granted JPS58128103A (en) | 1981-12-28 | 1981-12-28 | Temperature controlling method of distilling column |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS58128103A (en) |
Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS55145505A (en) * | 1979-04-21 | 1980-11-13 | Krupp Koppers Gmbh | Method of adjusting heat value supplied to tower bottom of extracting distilling tower |
-
1981
- 1981-12-28 JP JP21001981A patent/JPS58128103A/en active Granted
Patent Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS55145505A (en) * | 1979-04-21 | 1980-11-13 | Krupp Koppers Gmbh | Method of adjusting heat value supplied to tower bottom of extracting distilling tower |
Also Published As
| Publication number | Publication date |
|---|---|
| JPS58128103A (en) | 1983-07-30 |
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