Two-benzene production device with switchable reboilers
By modifying the reboiler pipelines of the benzene and toluene towers, the heat source was switched, solving the energy waste problem caused by the shutdown of the toluene tower and achieving energy saving, consumption reduction, and improved production flexibility of the benzene tower reboiler.
Patent Information
- Application Number
- CN202520277116.3
- Authority / Receiving Office
- CN · China
- Patent Type
- Utility models(China)
- Current Assignee / Owner
- Filing Date
- 2025-02-20
- Publication Date
- 2025-12-30
- Estimated Expiration
- 2035-02-20
AI Technical Summary
In existing co-production processes of toluene and benzene, the toluene tower and related structures are basically out of use, resulting in energy waste, and the 1.0 MPa steam cannot be effectively utilized.
Design a benzene and toluene production unit with switchable reboilers. By modifying the reboiler pipelines of the benzene tower and toluene tower, the heat source of the benzene tower reboiler and toluene tower reboiler can be switched. 1.0MPa steam and heat transfer oil are used as heat sources to reduce fuel gas consumption and steam venting.
This achieved energy saving and consumption reduction in the benzene tower reboiler, reduced system fuel gas consumption and steam venting, and improved the plant's production flexibility and economic benefits.
Smart Images
Figure CN223732137U_ABST
Abstract
Description
TECHNICAL FIELD
[0001] The utility model relates to the technical field of petroleum chemical industry, concretely relates to a two benzene production device with switchable reboiler. BACKGROUND
[0002] The co-production process of toluene and benzene is a process that utilizes the oil generated by catalytic reforming of petroleum, pyrolysis gasoline and other materials rich in aromatic hydrocarbons, and separates benzene and toluene in turn through rectification according to the boiling point difference of each component (the boiling point of benzene is 80.1℃, and the boiling point of toluene is 110.6℃). The process is as follows:
[0003] (1) The material rich in aromatic hydrocarbons such as benzene and toluene enters the benzene tower, and the benzene tower reboiler at the bottom of the benzene tower is heated by heat conduction oil, so that the benzene with low boiling point in the liquid at the bottom is preferentially vaporized into gas phase, and the toluene with high boiling point and the like mainly remains in the liquid phase;
[0004] (2) The steam at the top of the benzene tower is condensed by a condenser and then taken out, and the liquid phase at the bottom enters the bottom of the toluene tower for further separation;
[0005] (3) The reboiler at the bottom of the toluene tower is heated by heat conduction oil, so that part of the liquid at the bottom is vaporized, the steam rises, and the toluene gradually enriches in the gas phase;
[0006] (4) The steam at the top of the toluene tower is condensed by a condenser and then taken out, and the heavy components such as heavy aromatic hydrocarbons at the bottom are transported to the next processing unit or storage unit.
[0007] With the fluctuation of toluene price market, many factories choose not to produce toluene products, and the toluene tower and related structures are basically in a disabled state. On the other hand, with the deepening of energy saving optimization of each device in the factory, the 1.0MPa steam in the whole factory is in a rich condition in summer, which cannot be effectively utilized, and can only be emptied, causing waste of energy. INVENTION CONTENTS
[0008] In view of the technical problems of the co-production process device of toluene and benzene that the toluene tower and related structures are basically disabled and the rich 1.0MPa steam lacks effective utilization, the utility model provides a two benzene production device with switchable reboiler.
[0009] The technical scheme of the utility model is as follows:
[0010] The application discloses a reboiler switchable benzene production device, which comprises a benzene tower and a toluene tower, a material outlet at the bottom of the benzene tower is connected with a material inlet at the bottom of the toluene tower, a benzene tower reboiler is arranged at the bottom of the benzene tower, a toluene tower reboiler is arranged at the bottom of the toluene tower, an outlet line of the toluene tower reboiler is communicated with an outlet line of the benzene tower reboiler through an outlet cross line, an inlet line of the toluene tower reboiler is communicated with an inlet line of the benzene tower reboiler through an inlet cross line, an outlet valve one is arranged on the outlet cross line, an inlet valve one is arranged on the inlet cross line, a shell inlet pipe of the toluene tower reboiler is communicated with a 1.0 MPa steam source, and a shell outlet pipe of the toluene tower reboiler is communicated with a 1.0 MPa condensate water storage tank.
[0011] An outlet valve two is arranged on the outlet line of the benzene tower reboiler, and the outlet valve two is located between the communication of the outlet of the benzene tower reboiler to the outlet cross line and the outlet line of the benzene tower reboiler.
[0012] An inlet valve two is arranged on the inlet line of the benzene tower reboiler, and the inlet valve two is located between the communication of the inlet of the benzene tower reboiler to the inlet cross line and the inlet line of the benzene tower reboiler.
[0013] An outlet valve three is arranged on the outlet line of the toluene tower reboiler, and the outlet valve three is located between the communication of the outlet cross line and the outlet line of the toluene tower reboiler to the toluene tower.
[0014] An inlet valve three is arranged on the inlet line of the toluene tower reboiler, and the inlet valve three is located between the communication of the inlet cross line and the inlet line of the toluene tower reboiler to the toluene tower.
[0015] Further, the shell inlet pipe and the shell outlet pipe of the benzene tower reboiler are respectively communicated with a heat conducting oil storage tank.
[0016] Further, the shell inlet pipe of the toluene tower reboiler is further communicated with a medium-pressure steam source, and the shell outlet pipe of the toluene tower reboiler is further communicated with a medium-pressure condensate water storage tank.
[0017] Further, valves are respectively arranged on the communication pipelines of the shell inlet pipe of the toluene tower reboiler and the 1.0 MPa steam source and the medium-pressure steam source, and valves are respectively arranged on the communication pipelines of the shell outlet pipe of the toluene tower reboiler and the 1.0 MPa condensate water storage tank and the medium-pressure condensate water storage tank. Through the arrangement of the valves, the switching of the heat source of the toluene tower reboiler can be realized.
[0018] Further, a blind plate is installed on the side of the outlet valve three close to the toluene tower, and a blind plate is installed on the side of the inlet valve three close to the toluene tower reboiler.
[0019] Valves are respectively arranged on the communication pipelines of the shell inlet pipe of the toluene tower reboiler and the medium-pressure steam source and the communication pipelines of the shell outlet pipe of the toluene tower reboiler and the medium-pressure condensate water storage tank, and blind plates are respectively installed on the sides of the valves close to the toluene tower reboiler and the medium-pressure condensate water storage tank.
[0020] Further, the outlet valve one, the outlet valve two, the outlet valve three, the inlet valve one, the inlet valve two, and the inlet valve three are gate valves.
[0021] The utility model discloses the beneficial effect lies in:
[0022] The utility model discloses the outlet, inlet pipeline of benzene tower reboiler with the outlet, inlet pipeline of toluene tower reboiler are reformed, can make full use of the 1.0MPa steam of pipe network surplus during toluene tower inoperable, realizes the heating mode of benzene tower reboiler using heat conducting oil and / or 1.0MPa steam as heat source, fundamentally reduces the system fuel gas consumption and 1.0MPa steam emptying amount, reaches the purpose of energy saving and consumption reduction, can obtain appreciable economic benefits, widens the operation space of benzene tower reboiler in the original two benzene production device simultaneously, improves the ability of device to respond production fluctuation. BRIEF DESCRIPTION OF DRAWINGS
[0023] In order to more clearly illustrate the technical scheme of the utility model, the following will be to the description needed to use the drawings briefly introduced, obviously, the following description in the drawings only some embodiments of the utility model, for those skilled in the art, under the premise of not paying creative labor, can also obtain other drawings according to these drawings.
[0024] Figure 1 It is the structure schematic diagram of two benzene production device of reboiler switchable of example 1.
[0025] In the drawing, 1-benzene tower, 2-benzene tower reboiler, 3-toluene tower, 4-toluene tower reboiler, 5-outlet valve two, 6-inlet valve two, 7-inlet valve one, 8-outlet valve one, 9-inlet valve three, 10-outlet valve three, 11-1.0MPa steam cross line valve, 12-1.0MPa condensate cross line valve. DETAILED DESCRIPTION
[0026] In order to make the purpose, feature, advantage of the utility model more obvious and easy to understand, the following will be to the technical scheme in the utility model, clear, complete description is described in the specific embodiment of the utility model, obviously, the following described embodiment only a part of the embodiment of the utility model, not all embodiments. Based on the embodiment in the patent of the present application, all other embodiments obtained by those skilled in the art without making creative labor are within the scope of the patent protection.
[0027] Example 1
[0028] The reboiler switchable biphenyl production device comprises a benzene tower 1 and a toluene tower 3, a material outlet at the bottom of the benzene tower 1 is connected with a material inlet at the bottom of the toluene tower 3, the benzene tower 1 is provided with a benzene tower reboiler 2, a shell inlet pipe and a shell outlet pipe of the benzene tower reboiler 2 are respectively communicated with a heat conducting oil storage tank, the toluene tower 3 is provided with a toluene tower reboiler 4, an outlet line of the toluene tower reboiler 4 is communicated with an outlet line of the benzene tower reboiler 2 through an outlet cross line, an inlet line of the toluene tower reboiler 4 is communicated with an inlet line of the benzene tower reboiler 2 through an inlet cross line, an outlet valve 1 is arranged on the outlet cross line, an inlet valve 1 is arranged on the inlet cross line, a shell inlet pipe of the toluene tower reboiler 4 is respectively communicated with a 1.0 MPa steam source and a medium pressure steam source, a shell outlet pipe of the toluene tower reboiler 4 is respectively communicated with a 1.0 MPa condensate water storage tank and a medium pressure condensate water storage tank, and a 1.0 MPa steam cross line valve 11 is arranged on a communication pipeline of the shell inlet pipe of the toluene tower reboiler 4 and the 1.0 MPa steam source, a medium pressure steam valve is arranged on a communication pipeline of the shell inlet pipe of the toluene tower reboiler 4 and the medium pressure steam source, a 1.0 MPa condensate water cross line valve 12 is arranged on a communication pipeline of the shell outlet pipe of the toluene tower reboiler 4 and the 1.0 MPa condensate water storage tank, and a medium pressure condensate water valve is arranged on a communication pipeline of the shell outlet pipe of the toluene tower reboiler 4 and the medium pressure condensate water storage tank.
[0029] An outlet valve 2 is arranged on the outlet line of the benzene tower reboiler 2, and the outlet valve 2 is located between the communication of the outlet of the benzene tower reboiler 2 to the outlet cross line and the outlet line of the benzene tower reboiler 2.
[0030] An inlet valve 2 is arranged on the inlet line of the benzene tower reboiler 2, and the inlet valve 2 is located between the communication of the inlet of the benzene tower reboiler 2 to the inlet cross line and the inlet line of the benzene tower reboiler 2.
[0031] An outlet valve 3 is arranged on the outlet line of the toluene tower reboiler 4, and the outlet valve 3 is located between the communication of the outlet cross line and the outlet line of the toluene tower reboiler 4 and the toluene tower 3.
[0032] An inlet valve 3 is arranged on the inlet line of the toluene tower reboiler 4, and the inlet valve 3 is located between the communication of the inlet cross line and the inlet line of the toluene tower reboiler 4 and the toluene tower 3.
[0033] The internal structure of the benzene tower 1 and the benzene steam condensing device and the like can be arranged according to the prior art, and the internal structure of the toluene tower 3, the toluene steam condensing device and the treatment device of the heavy aromatic hydrocarbon after rectification and the like can also be arranged according to the prior art.
[0034] The working principle of the embodiment is as follows:
[0035] The main function of the outlet valve two and the inlet valve two arranged on the outlet and inlet lines of the benzene column reboiler is to remove or use the benzene column reboiler from the system. The main function of the outlet valve three and the inlet valve three arranged on the outlet and inlet lines of the toluene column reboiler is to realize the switching of the toluene column reboiler for the reboiling of the benzene column or the toluene column. The main function of the outlet valve one and the inlet valve one arranged on the outlet and inlet cross lines is to realize the parallel or separate use of the toluene column reboiler for the reboiling of the benzene column. The main function of the 1.0 MPa steam cross line valve, the 1.0 MPa condensate cross line valve, the medium pressure steam valve and the medium pressure condensate valve is to realize the switching of the heat source (medium pressure steam, 1.0 MPa steam) of the toluene column reboiler.
[0036] When the 1.0 MPa steam network is abundant, the inlet valve three and the outlet valve three are closed, the toluene column reboiler is steam purged, after the purging is completed, the system is purged clean of water by using nitrogen. The inlet valve one is slowly opened, the oil is gradually introduced to the toluene column reboiler and is vented and exhausted, after the exhausting is completed, the outlet valve one is slowly opened, the oil is gradually introduced into the system. The medium pressure steam valve and the medium pressure condensate valve of the toluene column reboiler are closed, the 1.0 MPa steam cross line valve is opened, the 1.0 MPa steam is introduced to the tube bundle of the toluene column reboiler, after the steam is seen, the 1.0 MPa condensate cross line valve is gradually opened. Preferably, the condensate regulating valve can also be put into use, the indoor operator adjusts the condensate regulating valve gradually according to the real-time temperature change, gradually increases the temperature according to the temperature increase requirement, and completes the parallel use of the toluene column reboiler. The benzene column reboiler gradually reduces the amount of heat conducting oil to full closing according to the steam abundance, completes the switching of the toluene column reboiler as the heat source for the reboiling of the benzene column, and thus realizes the purpose of stopping using the benzene column reboiler heat conducting oil or adjusting the operation in parallel with the toluene column reboiler.
[0037] In order to compare the fuel gas consumption before and after the reform of the benzene column reboiler, the device fuel gas heat value before the reform is selected as 54.34 MJ / m³; the heat value after the reform is 57.83 MJ / m³, and the processing capacity and the statistical time are basically the same before and after the reform. The total amount of fuel gas before the reform is 1199 Nm 3 / h, the total amount of fuel gas after the reform is 1089 Nm 3 / h, and the fuel gas consumption before and after the reform is reduced by 110 Nm 3 / h. Under the premise that the 1.0 MPa steam of the whole plant is abundant in summer, according to the market price of liquefied natural gas (LNG) of 3.24 yuan / Nm³, the heat value of 36.46 MJ / m³, the heat value of the self-produced fuel gas of the device of 57.83 MJ / m³, the conversion price is about 5.14 yuan / Nm³, and the annual operation is 5120 hours (subtracting the steam insufficient time of 4 months in winter, which is 2880 hours), the annual fuel gas fee is about 2.89 million yuan.
[0038] Example 2
[0039] On the basis of the embodiment 1, the outlet valve 8, the outlet valve 5, the outlet valve 10, the inlet valve 7, the inlet valve 6, the inlet valve 9 of the two benzene production device of the embodiment 2 are all gate valves.
[0040] When the toluene tower 3 is planned to be stopped for a long time, in order to completely isolate the pipeline and realize the complete cut-off without leakage, a blind plate is installed on the side close to the toluene tower 3 of the outlet valve 10, and a blind plate is installed on the side close to the toluene tower reboiler 4 of the inlet valve 9.
[0041] A blind plate is installed on the side close to the toluene tower reboiler 4 of the medium-pressure steam valve, and a blind plate is installed on the side close to the medium-pressure condensate water storage tank of the medium-pressure condensate water valve.
[0042] The above description of the disclosed embodiments enables a person skilled in the art to implement or use the present application. Various modifications to these embodiments will be apparent to those skilled in the art, and the general principles defined herein can be implemented in other embodiments without departing from the spirit or scope of the application. Therefore, the present application will not be limited to these embodiments shown herein, but will accord with the widest scope consistent with the principles and novel features disclosed herein.
Claims
1. A benzene and toluene production apparatus with switchable reboilers, comprising a benzene tower and a toluene tower, wherein the material outlet at the bottom of the benzene tower is connected to the material inlet at the bottom of the toluene tower, a benzene reboiler is provided at the bottom of the benzene tower, and a toluene reboiler is provided at the bottom of the toluene tower, characterized in that, The outlet line of the toluene column reboiler is communicated with the outlet line of the benzene column reboiler through an outlet cross line, and the inlet line of the toluene column reboiler is communicated with the inlet line of the benzene column reboiler through an inlet cross line, an outlet valve one is arranged on the outlet cross line, an inlet valve one is arranged on the inlet cross line, the shell side inlet pipe of the toluene column reboiler is communicated with a 1.0 MPa steam source, and the shell side outlet pipe of the toluene column reboiler is communicated with a 1.0 MPa condensate water storage tank; An outlet valve two is arranged on the outlet line of the benzene column reboiler, and the outlet valve two is located between the communication position of the outlet of the benzene column reboiler to the outlet cross line and the outlet line of the benzene column reboiler; An inlet valve two is arranged on the inlet line of the benzene column reboiler, and the inlet valve two is located between the communication position of the inlet of the benzene column reboiler to the inlet cross line and the inlet line of the benzene column reboiler; An outlet valve three is arranged on the outlet line of the toluene column reboiler, and the outlet valve three is located between the communication position of the outlet cross line and the outlet line of the toluene column reboiler to the toluene column; An inlet valve three is arranged on the inlet line of the toluene column reboiler, and the inlet valve three is located between the communication position of the inlet cross line and the inlet line of the toluene column reboiler to the toluene column.
2. The biphenyl production apparatus according to claim 1, wherein The shell side inlet pipe and the shell side outlet pipe of the benzene column reboiler are respectively communicated with a heat conducting oil storage tank.
3. The biphenyl production apparatus according to claim 1, wherein The shell side inlet pipe of the toluene column reboiler is further communicated with a medium pressure steam source, and the shell side outlet pipe of the toluene column reboiler is further communicated with a medium pressure condensate water storage tank.
4. The biphenyl production apparatus according to claim 3, wherein Valves are respectively arranged on the communication pipelines of the shell side inlet pipe of the toluene column reboiler and the 1.0 MPa steam source and the medium pressure steam source, and valves are respectively arranged on the communication pipelines of the shell side outlet pipe of the toluene column reboiler and the 1.0 MPa condensate water storage tank and the medium pressure condensate water storage tank.
5. The biphenyl production apparatus according to claim 1, wherein Blind plates are installed on the side of the outlet valve three close to the toluene column and the side of the inlet valve three close to the toluene column reboiler; Blind plates are installed on the side of the valve on the communication pipeline of the shell side inlet pipe of the toluene column reboiler and the medium pressure steam source close to the toluene column reboiler and the side of the valve on the communication pipeline of the shell side outlet pipe of the toluene column reboiler and the medium pressure condensate water storage tank close to the medium pressure condensate water storage tank.
6. The biphenyl production apparatus according to claim 1, wherein The outlet valve one, the outlet valve two, the outlet valve three, the inlet valve one, the inlet valve two and the inlet valve three are all gate valves.