CN213266389U

CN213266389U - Butane removing system

Info

Publication number: CN213266389U
Application number: CN202022124563.5U
Authority: CN
Inventors: 刘哲; 邓宏达; 昝大鑫; 王鑫; 吕云飞
Original assignee: Zhangjiagang Free Trade Zone Huixin Chemical Technology Co ltd
Current assignee: Zhangjiagang Free Trade Zone Huixin Chemical Technology Co ltd
Priority date: 2020-09-24
Filing date: 2020-09-24
Publication date: 2021-05-25
Anticipated expiration: 2030-09-24

Abstract

The application discloses a debutanizing system relates to suspension bed hydrogenation technical field. The debutanizer column comprises: a debutanizer column; a reboiler, the reboiler comprising: the pipeline five is connected with the bottom of the debutanizer and is used for inputting a bottom product of the debutanizer into the reboiler; the pipeline six is connected with the bottom of the debutanizer and is used for refluxing the bottom product subjected to impurity removal by heating to the bottom of the debutanizer; the steam inlet pipe is used for inputting high-pressure steam to the reboiler; the condensate outlet pipe is used for discharging condensate in the reboiler; and the adjusting system is used for adjusting the heat load of the reboiler. This application sets up the reboiler and is used for adjusting reboiler heat load's regulation module through the bottom at the debutanizer, heats the bottom product of debutanizer, gets rid of butane or lighter impurity wherein, provides the assurance for the steady operation of low reaches naphtha fractionating tower system, more can adapt to the market demand.

Description

Butane removing system

Technical Field

The application relates to the technical field of suspension bed hydrogenation, in particular to a butane removing system.

Background

The suspension bed hydrocracking technology is a thermal hydrocracking process, and can convert petroleum residue and coarse coal into marketable liquid fraction. The suspension bed reactor adopts slurry feeding, namely oil-solid mixed feeding. The oil phase is heavy oil to be processed, such as vacuum residuum, coal tar, catalytic slurry oil, asphalt and the like, and the solid phase is added catalyst, additive or coal powder.

In addition, another fixed bed reactor system can be matched at the downstream of the suspension bed reactor system, and gasoline and diesel oil products with high economy can be obtained through re-hydrofining and hydrocracking of the suspension bed reactor products, so that the total product yield is increased, and the operation flexibility of the whole device is greatly improved.

The main function of the debutanizer is to separate the liquefied gas component (C, C) in the bottom stream of the light hydrocarbon stripper from the top of the tower. Because of the relatively low separation efficiency of the debutanizer of the prior art, the feed to the downstream naphtha fractionator system typically contains a significant amount of butane and lighter impurities, which in turn affects the normal operation of the fractionator and the quality of the naphtha product.

SUMMERY OF THE UTILITY MODEL

The application aims at providing a debutanization system, which solves the problem that the separation efficiency of a debutanization tower in the prior art is low, so that impurities of butane and lighter components are contained in a separation product.

In order to achieve the above purpose, the embodiments of the present application adopt the following technical solutions: a debutanization system, comprising: a debutanizer column; the feeding pipe is used for conveying bottom materials from the light hydrocarbon stripping tower to the debutanizer; the discharge pipe is arranged at the bottom of the debutanizer, and a product at the bottom of the debutanizer is discharged out of the discharge pipe; a reboiler, the reboiler comprising: the pipeline five is connected with the bottom of the debutanizer and is used for inputting a bottom product of the debutanizer into the reboiler; the pipeline six is connected with the bottom of the debutanizer and is used for refluxing the bottom product subjected to impurity removal by heating to the bottom of the debutanizer; the steam inlet pipe is used for inputting high-pressure steam to the reboiler; the condensate outlet pipe is used for discharging condensate in the reboiler; a regulation module for regulating the heat duty of the reboiler, the regulation module comprising: the control valve IV is arranged on the condensate outlet pipe; the third flowmeter is arranged on the condensate outlet pipe; the liquid level meter II is arranged on the reboiler; the thermometer is arranged on the debutanizer, and the thermometer is connected with the flowmeter III in series; and the flow calculator is communicated with the third flowmeter and the second liquid level meter and controls the fourth control valve.

In above-mentioned technical scheme, this application embodiment through set up reboiler and the regulation module that is used for adjusting reboiler heat load in the bottom at the debutanizer, heats the bottom product of debutanizer, gets rid of butane or lighter impurity wherein, provides the assurance for the steady operation of low reaches naphtha fractionating tower system, more can adapt to market demand.

Further, according to this application embodiment, wherein, the debutanizing system still includes the heat exchanger, and the heat exchanger is shell and tube heat exchanger, and the shell side entry and the inlet pipe of heat exchanger are connected, and the tube side entry and the discharging pipe of heat exchanger are connected.

Further, according to the embodiment of the application, a first pipeline is arranged on a shell pass outlet of the heat exchanger, the end part of the first pipeline is connected with the middle part of the debutanizer, and the bottom material of the light hydrocarbon stripping tower after heat exchange is conveyed into the debutanizer; and a second pipeline is arranged on a tube pass outlet of the heat exchanger and used for discharging a bottom product of the debutanizer after heat exchange.

Further, according to this application embodiment, wherein, be provided with flowmeter one and control valve one on the pipeline one, flowmeter one and control valve intercommunication, flowmeter one still receives the liquid level cascade control of light hydrocarbon stripper.

Further, according to the embodiment of the application, a second flow meter and a second control valve are arranged on the second pipeline, a first liquid level meter is arranged on the debutanizer, the first liquid level meter is connected with the second flow meter in series, and the second flow meter is communicated with the second control valve.

Further, according to the embodiment of the application, a first pressure gauge and a third control valve are arranged on the steam inlet pipe, and the first pressure gauge is communicated with the third control valve.

Further, according to the embodiment of the application, a third pipeline is arranged above the debutanizer, and the third pipeline is used for discharging the tower top gas of the debutanizer; and an air cooler and a water cooler are arranged on the third pipeline, a reflux tank is arranged at the tail end of the third pipeline, and the condensed tower top gas is conveyed into the reflux tank.

Further, according to the embodiment of the application, the top of the return tank is provided with an exhaust pipe.

Further, according to the embodiment of the application, the bottom of the reflux tank is provided with a drain pipe.

Further, according to the embodiment of the application, a return pipe and a pipeline IV are arranged at the bottom of the return tank, and the return pipe is connected with the top of the debutanizer.

Compared with the prior art, the method has the following beneficial effects: this application sets up the reboiler and is used for adjusting reboiler heat load's regulation module through the bottom at the debutanizer, heats the bottom product of debutanizer, gets rid of butane or lighter impurity wherein, provides the assurance for the steady operation of low reaches naphtha fractionating tower system, more can adapt to the market demand.

Drawings

The present application is further described below with reference to the drawings and examples.

FIG. 1 is a schematic diagram of a debutanizer system of the present application.

In the attached drawings

1. Debutanizer tower 2, feed pipe 3, heat exchanger

4. Pipeline I5, discharge pipe 6 and pipeline II

7. Pipeline three 8, air cooler 9 and water cooler

10. Return tank 11, return pipe 12, exhaust pipe

13. Pipeline four 14, drain pipe 15 and balance pipeline

16. Pipeline five 17, reboiler 18 and pipeline six

19. Steam inlet pipe 20 and condensate outlet pipe

Detailed Description

In order to make the objects, technical solutions and advantages of the present invention clear and fully described, embodiments of the present invention are further described in detail below with reference to the accompanying drawings. It is to be understood that the specific embodiments described herein are merely illustrative of some embodiments of the invention and are not limiting of the invention, and that all other embodiments obtained by those of ordinary skill in the art without the exercise of inventive faculty are within the scope of the invention.

In the description of the present invention, it should be noted that the terms "center", "middle", "upper", "lower", "left", "right", "inner", "outer", "top", "bottom", "side", "vertical", "horizontal", and the like indicate orientations or positional relationships based on those shown in the drawings, and are only for convenience of description and simplicity of description, but do not indicate or imply that the referred device or element must have a specific orientation, be constructed in a specific orientation, and be operated, and thus, should not be construed as limiting the present invention. Furthermore, the terms "a," "an," "first," "second," "third," "fourth," "fifth," and "sixth" are used for descriptive purposes only and are not to be construed as indicating or implying relative importance.

In the description of the present invention, it should be noted that, unless otherwise explicitly specified or limited, the terms "mounted," "connected," and "connected" are to be construed broadly, e.g., as meaning either a fixed connection, a removable connection, or an integral connection; can be mechanically or electrically connected; they may be connected directly or indirectly through intervening media, or they may be interconnected between two elements. The specific meanings of the above terms in the present invention can be understood in specific cases to those skilled in the art.

For the purposes of simplicity and explanation, the principles of the embodiments are described by referring mainly to examples. In the following description, numerous specific details are set forth in order to provide a thorough understanding of the embodiments. It will be apparent, however, to one skilled in the art that the embodiments may be practiced without these specific details. In some instances, well-known methods and structures have not been described in detail so as not to unnecessarily obscure the embodiments. In addition, all embodiments may be used in combination with each other.

FIG. 1 shows a schematic diagram of a debutanizer system of the present application. As shown in FIG. 1, the debutanizing system comprises a debutanizing tower 1, a feeding pipe 2, a heat exchanger 3 and a discharging pipe 5. Wherein, inlet pipe 2 is used for carrying the bottom material that comes from the light hydrocarbon stripper, and discharging pipe 5 sets up in the bottom of debutanizer 1 for discharge the bottom product of debutanizer 1, the material in inlet pipe 2 and the material in discharging pipe 5 carry out the heat transfer through heat exchanger 3. The heat exchanger 3 is a shell-and-tube heat exchanger, the end part of the feeding pipe 2 is connected with a shell pass inlet of the heat exchanger 3, and the end part of the discharging pipe 5 is connected with a tube pass inlet of the heat exchanger 3. A first pipeline 4 is arranged on a shell pass outlet of the heat exchanger 3, the end part of the first pipeline 4 is connected with the middle part of the debutanizer 1, and a material at the bottom of the light hydrocarbon stripping tower after heat exchange is conveyed into the debutanizer 1. And a second pipeline 6 is arranged on a tube pass outlet of the heat exchanger 3 and used for discharging a bottom product of the debutanizer after heat exchange.

The first pipeline 4 is provided with a first flow meter and a first control valve, the first flow meter is communicated with the first control valve, and the first flow meter is communicated with the first light hydrocarbon stripping tower in a liquid level cascade mode and used for regulating and controlling the opening degree of the first control valve.

Secondly, a second flow meter and a second control valve are arranged on the second pipeline 6, a first liquid level meter is arranged on the debutanizer 1, the first liquid level meter is connected with the second flow meter in series, the second flow meter is communicated with the second control valve, and the opening degree of the second control valve is regulated and controlled through the liquid level in the debutanizer 1 and the flow in the second pipeline 6.

In addition, in order to ensure that the bottom product of the debutanizer column 1 does not contain butane or lighter impurities, the debutanizer system further comprises a reboiler 17 and a regulating module for regulating the heat load of the reboiler 17. Wherein, the inlet of the reboiler 17 is connected with the bottom of the debutanizer 1 through a pipeline five 16, and the bottom product of the debutanizer 1 is input into the reboiler 17. The outlet of the reboiler 17 is connected with the bottom of the debutanizer 1 through a pipeline six 18, and the bottom product after being heated and the impurities are removed is refluxed to the bottom of the debutanizer 1. The reboiler 17 uses high pressure steam as a heating medium and includes a steam inlet pipe 19 and a condensate outlet pipe 20. The steam inlet pipe 19 is provided with a first pressure gauge and a third control valve, and the first pressure gauge is communicated with the third control valve and used for controlling the pressure of the steam inlet pipe 19.

And the adjusting module comprises a flow calculator, a control valve IV, a flow meter III, a liquid level meter II and a thermometer. The fourth control valve and the third flow meter are arranged on the condensate outlet pipe 20, the flow in the condensate outlet pipe 20 is measured through the third flow meter, and the flow in the condensate outlet pipe 20 is controlled by adjusting the opening of the fourth control valve. The second liquid level meter is arranged on the reboiler 17 and is used for measuring the liquid level in the reboiler 17. The thermometer is arranged at one side of the debutanizer 1 and is used for measuring the temperature of a tray in the debutanizer 1. The thermometer is connected with the third flowmeter in series, the flow calculator receives the flow signal and the temperature signal from the third flowmeter and the liquid level signal from the second liquid level meter, calculates the heat load required by the reboiler 17 and the flow required to be adjusted of the condensate outlet pipe 20 according to the temperature signal and the liquid level signal, and then adjusts the opening degree of the fourth control valve.

And finally, a third pipeline 7 is arranged above the debutanizer 1 and used for discharging the tower top gas of the debutanizer 1. An air cooler 8 and a water cooler 10 are arranged on the third pipeline 7, a reflux tank 10 is arranged at the tail end of the third pipeline 7, and the tower top gas is condensed and then conveyed into the reflux tank 10. The condensed overhead gas enters the reflux drum 10 and is separated into a gas phase product, an oil phase product and a water phase product. Wherein the gas phase product is discharged through an exhaust pipe 12 arranged at the top of the reflux tank 10, the water phase product is discharged through a drain pipe 14 arranged at the bottom of the reflux tank 10, and the oil phase product is divided into two parts: one strand of the mixed gas flows back through a return pipe 11 communicated with the top of the debutanizer 1, the other strand of the mixed gas is discharged through a pipeline IV 13, and a first booster pump and a second booster pump are respectively arranged on the return pipe 11 and the pipeline IV 13.

Wherein, be provided with pressure gauge two and control valve five on the pipeline three 7, pressure gauge two and control valve five intercommunication for the pressure in the control pipeline three 7.

And a balance pipeline 15 is arranged between the third pipeline 7 and the reflux tank 10 and is used for maintaining the pressure balance in the debutanizer 1 and the reflux tank 10.

The exhaust pipe 12 is provided with a third pressure gauge and a sixth control valve which are communicated with each other and used for adjusting the pressure in the reflux tank 10.

The return pipe 11 is provided with a flow meter IV and a control valve VII, and the flow meter IV is communicated with the control valve VII and is used for controlling the flow in the return pipe 11.

The fourth pipeline 13 is provided with a fifth flow meter and an eighth control valve, the end part of the backflow tank 10 is provided with a third liquid level meter, the third liquid level meter is connected with the fifth flow meter in series, the fifth flow meter is communicated with the eighth control valve, and the opening of the eighth control valve is regulated and controlled through the liquid level in the backflow tank 10 and the flow in the fourth pipeline 13.

A control valve nine is arranged on the drain pipe 14, a liquid level meter four is arranged at the joint of the drain pipe 14 and the reflux tank 10, the liquid level meter four is communicated with the control valve nine, and the opening of the control valve is regulated and controlled through the liquid level in the reflux tank 10.

In above-mentioned technical scheme, this application sets up the reboiler and is used for adjusting reboiler heat load's regulation module through the bottom at debutanizer 1, heats debutanizer 1's bottom product, gets rid of butane or lighter impurity wherein, provides the assurance for the steady operation of low reaches naphtha fractionating tower system, more can adapt to the market demand.

Although the illustrative embodiments of the present application have been described above to enable those skilled in the art to understand the present application, the present application is not limited to the scope of the embodiments, and various modifications within the spirit and scope of the present application defined and determined by the appended claims will be apparent to those skilled in the art from this disclosure.

Claims

1. A debutanization system, comprising:

a debutanizer column;

a feed line for feeding bottoms from a light hydrocarbon stripper to the debutanizer column;

the discharge pipe is arranged at the bottom of the debutanizer, and a product at the bottom of the debutanizer is discharged out of the discharge pipe;

a reboiler, the reboiler comprising:

a fifth pipeline connected with the bottom of the debutanizer for feeding the bottom product of the debutanizer to the reboiler;

the pipeline six is connected with the bottom of the debutanizer and is used for refluxing the bottom product subjected to impurity removal by heating to the bottom of the debutanizer;

a steam inlet pipe, wherein the steam inlet pipe is used for inputting high-pressure steam to the reboiler;

a condensate outlet pipe for discharging condensate in the reboiler;

a regulation module for regulating a heat duty of the reboiler, the regulation module comprising:

the control valve IV is arranged on the condensate outlet pipe;

the third flowmeter is arranged on the condensate outlet pipe;

the liquid level meter II is arranged on the reboiler;

the thermometer is arranged on the debutanizer, and the thermometer is connected with the flowmeter III in series;

and the flow calculator is communicated with the third flowmeter and the second liquid level meter and controls the fourth control valve.

2. The debutanizer system of claim 1, further comprising a heat exchanger, wherein the heat exchanger is a shell and tube heat exchanger, the shell-side inlet of the heat exchanger is connected to the feed pipe, and the tube-side inlet of the heat exchanger is connected to the discharge pipe.

3. The debutanizer system of claim 2, wherein a first pipeline is arranged at the shell-side outlet of the heat exchanger, the end part of the first pipeline is connected with the middle part of the debutanizer, and the bottom material of the light hydrocarbon stripper after heat exchange is conveyed into the debutanizer; and a second pipeline is arranged on a tube pass outlet of the heat exchanger and is used for discharging a bottom product of the debutanizer after heat exchange.

4. The debutanizer system of claim 3, wherein the first pipeline is provided with a first flow meter and a first control valve, the first flow meter is communicated with the first control valve, and the first flow meter is further controlled by a liquid level cascade of the light hydrocarbon stripper.

5. The debutanizer system of claim 3, wherein a second flow meter and a second control valve are arranged on the second pipeline, a first liquid level meter is arranged on the debutanizer, the first liquid level meter is connected with the second flow meter in series, and the second flow meter is communicated with the second control valve.

6. A debutanizer system according to claim 1, wherein said vapor inlet pipe is provided with a first pressure gauge and a third control valve, said first pressure gauge and said third control valve being in communication.

7. The debutanizer system of claim 1, wherein a third pipeline is arranged above the debutanizer and is used for discharging the overhead gas of the debutanizer; and an air cooler and a water cooler are arranged on the third pipeline, a reflux tank is arranged at the tail end of the third pipeline, and the tower top gas is condensed and then conveyed into the reflux tank.

8. A debutanizer system according to claim 7, wherein the top of the reflux drum is provided with a vent pipe.

9. A debutanizer system according to claim 7, wherein a drain is provided at the bottom of the reflux drum.

10. A debutanizer system according to claim 7, wherein a return line is provided at the bottom of said reflux drum, said return line being connected to the top of said debutanizer column, and a line four.