CN221040270U - Virtual simulation platform for simulating benzene production process - Google Patents
Virtual simulation platform for simulating benzene production process Download PDFInfo
- Publication number
- CN221040270U CN221040270U CN202322638979.2U CN202322638979U CN221040270U CN 221040270 U CN221040270 U CN 221040270U CN 202322638979 U CN202322638979 U CN 202322638979U CN 221040270 U CN221040270 U CN 221040270U
- Authority
- CN
- China
- Prior art keywords
- benzene
- tower
- benzene tower
- heat exchanger
- simulating
- 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.)
- Active
Links
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 title claims abstract description 323
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 22
- 238000010992 reflux Methods 0.000 claims abstract description 54
- 239000002994 raw material Substances 0.000 claims abstract description 15
- 239000007788 liquid Substances 0.000 claims description 49
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 12
- 239000002699 waste material Substances 0.000 claims description 9
- 229910052757 nitrogen Inorganic materials 0.000 claims description 6
- 238000010438 heat treatment Methods 0.000 claims description 4
- 238000000034 method Methods 0.000 abstract description 26
- 150000004945 aromatic hydrocarbons Chemical class 0.000 abstract description 6
- 238000005194 fractionation Methods 0.000 abstract description 3
- 238000003889 chemical engineering Methods 0.000 abstract 3
- YXFVVABEGXRONW-UHFFFAOYSA-N Toluene Chemical compound CC1=CC=CC=C1 YXFVVABEGXRONW-UHFFFAOYSA-N 0.000 description 9
- 238000004088 simulation Methods 0.000 description 9
- URLKBWYHVLBVBO-UHFFFAOYSA-N Para-Xylene Chemical compound CC1=CC=C(C)C=C1 URLKBWYHVLBVBO-UHFFFAOYSA-N 0.000 description 8
- 238000003825 pressing Methods 0.000 description 8
- 239000000463 material Substances 0.000 description 7
- 230000001276 controlling effect Effects 0.000 description 6
- CTQNGGLPUBDAKN-UHFFFAOYSA-N O-Xylene Chemical compound CC1=CC=CC=C1C CTQNGGLPUBDAKN-UHFFFAOYSA-N 0.000 description 5
- 230000009191 jumping Effects 0.000 description 5
- 238000011160 research Methods 0.000 description 5
- 239000000126 substance Substances 0.000 description 5
- 239000008096 xylene Substances 0.000 description 5
- 230000003993 interaction Effects 0.000 description 4
- 238000002360 preparation method Methods 0.000 description 4
- 238000005516 engineering process Methods 0.000 description 3
- 239000000047 product Substances 0.000 description 3
- 239000010865 sewage Substances 0.000 description 3
- 238000012546 transfer Methods 0.000 description 3
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 2
- 238000001311 chemical methods and process Methods 0.000 description 2
- 238000012824 chemical production Methods 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 239000007791 liquid phase Substances 0.000 description 2
- 229910052717 sulfur Inorganic materials 0.000 description 2
- 239000011593 sulfur Substances 0.000 description 2
- 239000012808 vapor phase Substances 0.000 description 2
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 description 1
- 239000005977 Ethylene Substances 0.000 description 1
- 238000004458 analytical method Methods 0.000 description 1
- 125000003118 aryl group Chemical group 0.000 description 1
- 238000001833 catalytic reforming Methods 0.000 description 1
- 239000013064 chemical raw material Substances 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 230000008878 coupling Effects 0.000 description 1
- 230000001808 coupling effect Effects 0.000 description 1
- 238000010168 coupling process Methods 0.000 description 1
- 238000005859 coupling reaction Methods 0.000 description 1
- 238000005336 cracking Methods 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 238000009776 industrial production Methods 0.000 description 1
- 239000013067 intermediate product Substances 0.000 description 1
- 230000016507 interphase Effects 0.000 description 1
- 238000004886 process control Methods 0.000 description 1
- 238000011112 process operation Methods 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 238000012827 research and development Methods 0.000 description 1
- 239000002904 solvent Substances 0.000 description 1
- 238000012549 training Methods 0.000 description 1
- 238000010977 unit operation Methods 0.000 description 1
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The utility model discloses a virtual simulation platform for simulating a benzene production process, which comprises a raw material pump, a benzene tower top pump, a first heat exchanger, a second heat exchanger, a benzene tower, a reboiler, a condenser and a reflux tank; wherein, connected gradually first heat exchanger, second heat exchanger on the pipeline of raw materials pump and benzene tower middle part intercommunication, benzene tower top is equipped with the export and communicates with the reflux drum behind the condenser, and the reflux drum divides two branch roads through the control of benzene tower top pump: the first branch is used for being communicated with the benzene tower, and the second branch is used for being extracted; the bottom of the benzene tower is provided with an outlet: the first outlet is used for flowing into the benzene tower after being heated by the reboiler through a pipeline, and the second outlet is used for sending out tower bottom. The utility model relates to a process for preparing benzene by chemical engineering, which is characterized in that a virtual simulation platform is built by linking the process of a fractionation section for preparing benzene by chemical engineering with the control of chemical engineering process and the like, so that the production efficiency can be improved, the use cost can be reduced, and meanwhile, the process flow for purifying and preparing benzene in the process of fractionating aromatic hydrocarbon can be known more specifically and clearly by groups without experimental conditions.
Description
Technical Field
The utility model relates to a virtual simulation platform for simulating a benzene production process, and belongs to the technical field of chemical process production control.
Background
Benzene is an important organic chemical raw material and solvent, and the main preparation route at home and abroad is PX (para-xylene) process. PX is a key process for preparing important aromatic chemical raw materials such as benzene, toluene, xylene and the like. The main technical route of the process is as follows: the intermediate product naphtha in petrochemical process is used as raw material, after catalytic reforming or ethylene cracking, reformate is obtained, benzene components in the reformate are less, toluene and xylene are high, and then high-purity product can be obtained through aromatic hydrocarbon rectification extraction and aromatic hydrocarbon rectification, the benzene is prepared by adopting the typical process unit operation of rectification, and benzene is extracted from mixed aromatic hydrocarbon obtained in petrochemical process and purified. At present, 40% of benzene products in the world are prepared by adopting the technical route, foreign PX production processes are represented by U.S. UOP company and French IFP technology, and domestic whole-flow process technology is broken through by China petrochemical industry in 2011.
At present, key equipment in the benzene preparation process is a benzene tower, the process and control problems thereof are always focused, but because the traditional process industrial production system has long research and development process period and high risk, and meanwhile, the consumption of infrastructure, manpower and material resources is huge, the research can not be realized by using real equipment, the production process and equipment can not be simulated by using the computer related technology, however, most of the current chemical production simulation devices are poor in construction, and the comprehensive consideration of the chemical process production section level simulation devices can not be realized, so the simulation device for producing benzene by chemical production is urgently needed to meet the research requirement.
Disclosure of Invention
The utility model provides a virtual simulation platform for simulating a benzene production process, which is used for simulating the benzene production process conforming to an actual process and providing a virtual environment for an experimenter.
The technical scheme of the utility model is as follows: a virtual simulation platform for simulating a benzene production process comprises a raw material pump 1-1, a benzene tower top pump 1-2, a first heat exchanger 2-1, a second heat exchanger 2-2, a benzene tower 5, a reboiler, a condenser 7 and a reflux tank 10; wherein, the pipeline that raw materials pump 1-1 and benzene tower 5 middle part communicate has connected gradually first heat exchanger 2-1, second heat exchanger 2-2 on, and benzene tower 5 top is equipped with the export and communicates with reflux drum 10 behind the condenser 7, reflux drum 10 divides two branch roads through the control of benzene tower top pump 1-2: the first branch is used for being communicated with the benzene tower 5, and the second branch is used for being extracted; the bottom of the benzene tower 5 is provided with an outlet: for heating through a reboiler via a pipe and flowing into benzene column 5 for sending out the bottoms.
The reboiler is provided with two groups, specifically a first reboiler 4-1 and a second reboiler 4-2, wherein the first reboiler 4-1 controls the inflow amount through a first pneumatic valve 3.
The tower bottom of the benzene tower 5 is provided with a first thermometer 6-1, and the tower top is provided with a second thermometer 6-2.
The reflux drum 10 is provided with a nitrogen input end, an air output end and a waste liquid output end, the nitrogen input end is provided with a second pneumatic valve 8, the air output end is provided with a third pneumatic valve 9, and the waste liquid output end of the benzene tower reflux drum 10 discharges waste liquid through a gate valve 13.
The first liquid level meter 12-1 and the second flowmeter 16-2 arranged on the reflux tank 10 are matched to jointly control the valve opening of the fifth pneumatic valve 15 on the second branch.
The second liquid level meter 12-2 is arranged on the benzene tower 5 and is used for displaying the liquid level of the benzene tower, and the liquid level of the benzene tower 5 is controlled by matching with the sixth pneumatic valve 17 and the flowmeter 16-3.
The beneficial effects of the utility model are as follows: according to the utility model, the virtual simulation platform is built by linking the process of the fractionation section for preparing benzene in chemical industry with the process control of chemical industry, so that the production efficiency can be improved, the use cost can be reduced, meanwhile, the population without experimental conditions can know the process flow of benzene purification and preparation in the aromatic hydrocarbon fractionation process more specifically and clearly, the remarkable beneficial effects are brought in the aspects of training and education, and the development of the chemical industry towards more sustainable and innovative directions can be promoted.
Drawings
FIG. 1 is a schematic diagram of the overall process of the present utility model;
FIG. 2 is a main interface of a simulation experiment platform;
FIG. 3 is a benzene column liquid level control interface of the simulation experiment platform;
FIG. 4 is a reflux drum liquid level control interface of a simulation experiment platform;
FIG. 5 is a reflux drum pressure control interface of a simulation experiment platform;
FIG. 6 is a top/bottom temperature control interface of a simulation experiment platform;
FIG. 7 is a historical trend curve interface in a simulation experiment platform;
FIG. 8 is a simplified diagram of an overall build model of the underlying control module;
The reference numerals in the figures are: 1-1-raw material pump, 2-1-first heat exchanger, 2-2-second heat exchanger, 3-first pneumatic valve, 4-1-first reboiler, 4-2-second reboiler, 5-benzene tower, 6-1-first thermometer, 6-2-second thermometer, 7-condenser, 8-second pneumatic valve, 9-third pneumatic valve, 10-reflux tank, 11-manometer, 12-1-first liquid level meter, 12-2-second liquid level meter, 13-gate valve, 1-2-benzene tower top pump, 14-fourth pneumatic valve, 15-fifth pneumatic valve, 16-1-first flowmeter, 16-2-second flowmeter, 16-3-third flowmeter, 1-3 benzene tower bottom pump, 17-sixth pneumatic valve.
Detailed Description
The utility model will be further described with reference to the drawings and examples, but the utility model is not limited to the scope.
Example 1: 1-8, a virtual simulation platform for simulating a benzene production process comprises a raw material pump 1-1, a benzene tower top pump 1-2, a first heat exchanger 2-1, a second heat exchanger 2-2, a benzene tower 5, a reboiler, a condenser 7 and a reflux tank 10; wherein, the pipeline that raw materials pump 1-1 and benzene tower 5 middle part communicate has connected gradually first heat exchanger 2-1, second heat exchanger 2-2 on, and benzene tower 5 top is equipped with the export and communicates with reflux drum 10 behind the condenser 7, reflux drum 10 divides two branch roads through the control of benzene tower top pump 1-2: the first branch is used for being communicated with the benzene tower 5, and the second branch is used for being extracted; the bottom of the benzene tower 5 is provided with an outlet: for heating by a reboiler through a pipe and flowing into the benzene column 5 for sending the bottom to the next process.
Further, two groups of reboilers, specifically a first reboiler 4-1 and a second reboiler 4-2, are arranged, wherein the first reboiler 4-1 controls the inlet amount through a first pneumatic valve 3.
Further, a first thermometer 6-1 is arranged at the tower bottom of the benzene tower 5, and a second thermometer 6-2 is arranged at the tower top.
Further, the reflux tank 10 is provided with a nitrogen input end, an air output end and a waste liquid output end, the nitrogen input end is provided with a second pneumatic valve 8, the air output end is provided with a third pneumatic valve 9, the benzene tower reflux tank 10 is provided with a pressure gauge 11 for measuring the pressure in the tank, so that the opening of the second pneumatic valve 8 and the third pneumatic valve 9 is controlled to realize the pressure control of the benzene tower reflux tank 10, and the waste liquid output end of the benzene tower reflux tank 10 discharges the waste liquid through a gate valve 13.
Further, the first liquid level meter 12-1 and the second flowmeter 16-2 arranged on the reflux drum 10 cooperate to jointly control the valve opening of the fifth pneumatic valve 15 on the second branch.
Further, a second liquid level meter 12-2 is arranged on the benzene tower 5 and is used for displaying the liquid level of the benzene tower, and the liquid level of the benzene tower 5 is controlled by matching with a sixth pneumatic valve 17 and a flowmeter 16-3.
The technological principle of the utility model is as follows: the second heat exchanger 2-2 and the first heat exchanger 2-1 are sequentially introduced into a xylene tower top product generated in a subsequent working section to exchange heat with a raw material which is conveyed through a pipeline after being acted by a raw material pump 1-1, the raw material is fed from the middle part of a benzene tower after being preheated, two thermometers are respectively arranged at the tower bottom and the tower top of the benzene tower 5 and used for measuring the temperature of the tower bottom and the tower top in the benzene tower 5 and regulating and controlling the temperature change process in the tower (the opening of a first air valve 3 is controlled by a first thermometer 6-1 on the benzene tower 5 so as to regulate the steam feeding amount and thus achieve the aim of controlling the temperature of the tower bottom, and the opening of a valve of a fourth air valve 14 is controlled by a second thermometer 6-2 on the benzene tower 5 so as to achieve the aim of controlling the reflux amount and controlling the temperature of the tower top); after entering the benzene tower 5, the vapor phase material and the liquid phase material flow in the tower in a countercurrent way, the heat transfer of the inter-phase material occurs, the non-volatilized light component in the liquid phase is transferred into the vapor phase, the light component is further concentrated by the rectifying section, the top of the benzene tower 5 is provided with an outlet which is communicated with the reflux tank 10 after passing through the condenser 7, sulfur-containing sewage can be removed in the reflux tank 10, the components after removing the sulfur-containing sewage are controlled by the pump 1-2 at the top of the benzene tower, one part of the components are returned into the tower after passing through the control of the fourth pneumatic valve 14, the first flowmeter 16-1 is arranged on a pipeline through which the components flow can display the reflux quantity in real time, the other part of the components are extracted as distillate after passing through the fifth pneumatic valve 15 and the control of the second flowmeter 16-2, the difficult volatile substances enter the tower kettle after heat transfer and mass transfer, and the reflux tank 10 is also provided with a sewage outflow outlet which is controlled by the gate valve 13; the first liquid level meter 12-1 on the reflux tank 10 is matched with the second flowmeter 16-2 to jointly control the valve opening of the fifth pneumatic valve 15, so that the control of the liquid level of the reflux tank is realized, the pressure meter 11 on the reflux tank 10 measures the pressure in the tank and simultaneously controls the valve opening of the second pneumatic valve 8 and the third pneumatic valve 9 to realize the control of the pressure in the reflux tank of the benzene tower, and the first flowmeter 16-1 can display the reflux quantity; part of the bottom material of the benzene tower 5 flows into the benzene tower 5 through a pipeline for treatment after passing through two reboilers (the first reboiler 4-1 adopts 1.0Mpa steam for heating, the first pneumatic valve 3 is used for controlling the amount of the introduced steam, the second reboiler 4-2 takes the top material of the xylene tower in the subsequent working section as hot fluid, the comprehensive recovery and utilization of heat are realized), and the part of the bottom material is sent to the rectifying tower of the subsequent working section to purify toluene and xylene under the control of the bottom pump 1-3 of the benzene tower through the sixth pneumatic valve 17 and the third flowmeter 16-3, meanwhile, the second liquid level meter 12-2 on the benzene tower 5 is used for displaying the liquid level of the benzene tower, and the liquid level of the benzene tower is controlled by matching with the sixth pneumatic valve 17 and the third flowmeter 16-3, so that the closed loop control of the liquid level of the benzene tower is finally realized.
According to the virtual simulation platform, a man-machine interaction operation page is developed through KINGSCADA, the building of a bottom control system is completed by using Simulink, the built model can enable measured data to be closer to a true value, a high-efficiency and safe scheme is provided for related research of the section of benzene preparation, and meanwhile, historical experimental data measured by the platform can be stored in a KINGSCADA self-contained database for analysis and research.
The man-machine interaction control interface provides a convenient operation interface, so that an operator can control the process flow and develop research more conveniently; the man-machine interaction control interface comprises a main interface, a benzene tower liquid level control interface, a reflux tank pressure control interface, a tower top/tower kettle temperature control interface and a historical trend curve interface, wherein each interface is provided with a button, and the jump among the interfaces can be realized through the main interface. As shown in fig. 2-7, the main interface comprises a working section process flow for preparing benzene by rectifying aromatic hydrocarbon and buttons for jumping to the other five interfaces,
The method comprises the steps that a raw material pump switch is pressed by a left mouse button in a main interface, the operation of the whole process flow is started, the whole flow and the flow directions of all components can be clearly seen from the operation, a benzene tower liquid level control interface can be jumped by pressing a benzene tower liquid level control button in the main interface, the interface comprises a benzene tower liquid level curve display interface and a PID controller parameter adjustment interface, and after the operation of the interface is finished, the main interface can be returned by pressing a return button; pressing a 'reflux tank liquid level control' button in a main interface, jumping to the reflux tank liquid level control interface, setting the interface to be the same as the benzene tower liquid level control interface, and pressing a return button to return to the main interface after the page operation is completed; pressing a 'reflux tank branch control' button from a main interface, and jumping to a loop tank pressure control interface, wherein the interface can display a reflux tank pressure curve and adjust parameters of a controller in real time, and can set upper and lower pressure limits at the same time, so that the change condition of the reflux tank pressure curve is observed when the upper and lower pressure limits change, and the reflux tank pressure curve is closer to a real process operation system; pressing a 'tower top/tower bottom temperature control' button in a main interface, jumping to the tower top/tower bottom temperature control interface, and setting a 'decoupling/non-decoupling' button besides displaying a real-time curve of the temperature of the tower top and the tower bottom to adjust two controller parameters, wherein a user can select different control modes during operation; the method comprises the steps of pressing a history trend curve button in a main interface, jumping to the history trend curve interface, arranging a plurality of function buttons in the interface, selecting a curve type to be inquired in the multi-selection frame parameter button, pressing the history curve inquiry button, inquiring trend curves of the type of curves in different time periods, selecting an acquisition curve maximum value to obtain the maximum value of the curves in the time period, selecting an acquisition curve minimum value button to obtain the curve minimum value, selecting an acquisition curve average value button to calculate the average value of the curves, and finally selecting a return button to return to the main interface, wherein the operation of a human-computer interaction operation interface in the virtual simulation platform is completed.
As shown in fig. 8, the bottom layer control includes cascade control, decoupling control and split control, and according to the actual requirements of the process, the benzene column liquid level control and the reflux tank liquid level control use control schemes of cascade control, reflux tank pressure use split control and benzene column/tower bottom temperature use decoupling control, and the coupling relationship exists among the control schemes. Specifically, in the temperature control of the tower top/tower bottom, as the temperature of the tower top and the tower bottom has high coupling property, the temperature correlation is strong when the temperature of the tower top and the tower bottom is controlled, so that the decoupling control of the temperature of the tower top and the tower bottom is realized by using a decoupling control scheme; because the fluctuation of the flow rate can cause larger fluctuation of the liquid level, in the liquid level control of the liquid level of the benzene tower 5 and the reflux tank 10, the cascade control scheme is used for controlling the liquid level, so that the influence of the flow rate fluctuation on the liquid level can be effectively reduced; in the case of pressure control of the reflux drum 10, since it is necessary to control the opening of two valves to control the pressure, the reflux drum pressure control uses a control scheme of the split control; the temperature of the top of the benzene tower is determined by the reflux amount which flows into the tower, meanwhile, the reflux amount influences the liquid level of the reflux tank and the change of the liquid level of the benzene tower, the pressure control of the reflux tank is related to the liquid level in the reflux tank, and the pressure in the reflux tank is directly related to the liquid level.
While the present utility model has been described in detail with reference to the drawings, the present utility model is not limited to the above embodiments, and various changes can be made without departing from the spirit of the present utility model within the knowledge of those skilled in the art.
Claims (6)
1. The virtual simulation platform for simulating the benzene production process is characterized by comprising a raw material pump (1-1), a benzene tower top pump (1-2), a first heat exchanger (2-1), a second heat exchanger (2-2), a benzene tower (5), a reboiler, a condenser (7) and a reflux tank (10); wherein, connect gradually first heat exchanger (2-1), second heat exchanger (2-2) on the pipeline that raw materials pump (1-1) and benzene tower (5) middle part communicate, benzene tower (5) top is equipped with the export and communicates with reflux drum (10) behind condenser (7), reflux drum (10) divide two branch roads through the control of benzene tower overhead pump (1-2): the first branch is used for being communicated with the benzene tower (5), and the second branch is used for being extracted; the bottom of the benzene tower (5) is provided with an outlet: for heating through a reboiler via a pipe and flowing into a benzene column (5) for sending out the bottom product.
2. A virtual simulation platform for simulating a benzene production process according to claim 1, wherein two groups of reboilers are provided, in particular a first reboiler (4-1) and a second reboiler (4-2), wherein the first reboiler (4-1) controls the feed through a first pneumatic valve (3).
3. The virtual simulation platform for simulating a benzene production process according to claim 1, wherein a first thermometer (6-1) is arranged at the tower bottom of the benzene tower (5), and a second thermometer (6-2) is arranged at the tower top.
4. The virtual simulation platform for simulating a benzene production process according to claim 1, wherein the reflux drum (10) is provided with a nitrogen input end, an air output end and a waste liquid output end, the nitrogen input end is provided with a second pneumatic valve (8), the air output end is provided with a third pneumatic valve (9), and the waste liquid output end of the benzene tower reflux drum (10) discharges waste liquid through a gate valve (13).
5. A virtual simulation platform for simulating a benzene production process according to claim 1, wherein the first liquid level meter (12-1) arranged on the reflux drum (10) is matched with the second flowmeter (16-2) to jointly control the valve opening of the fifth pneumatic valve (15) on the second branch.
6. A virtual simulation platform for simulating a benzene production process according to claim 1, wherein the benzene tower (5) is provided with a second liquid level meter (12-2) for displaying the liquid level of the benzene tower, and the liquid level of the benzene tower (5) is controlled by matching with a sixth pneumatic valve (17) and a flowmeter (16-3).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202322638979.2U CN221040270U (en) | 2023-09-27 | 2023-09-27 | Virtual simulation platform for simulating benzene production process |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202322638979.2U CN221040270U (en) | 2023-09-27 | 2023-09-27 | Virtual simulation platform for simulating benzene production process |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN221040270U true CN221040270U (en) | 2024-05-28 |
Family
ID=91172696
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202322638979.2U Active CN221040270U (en) | 2023-09-27 | 2023-09-27 | Virtual simulation platform for simulating benzene production process |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN221040270U (en) |
-
2023
- 2023-09-27 CN CN202322638979.2U patent/CN221040270U/en active Active
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101986320B (en) | Modeling method for heterogeneous azeotropic rectification solvent dehydrating tower of industrial purified terephthalic acid (PTA) device | |
| CN102183892B (en) | Load change energy consumption optimizing control method of three-column methanol distillation system | |
| CN103946191B (en) | For method and system prepared by alkene | |
| CN221040270U (en) | Virtual simulation platform for simulating benzene production process | |
| Xie et al. | Experimental and simulation of the reactive dividing wall column based on ethyl acetate synthesis | |
| CN104370740A (en) | Production method of isobornyl acetate | |
| KR20240136980A (en) | High-efficiency production device and method for methyl methacrylate | |
| CN103611328B (en) | Process for extracting naphthalene by continuously rectifying heavy benzol | |
| CN104765926A (en) | Energy optimization analysis method for chemical engineering device | |
| CN208414288U (en) | A kind of differential pressure thermocouple propylene refining separation system in production of propylene oxide | |
| CN102890639B (en) | Optimal simulation system for methanol rectification process | |
| CN106916050A (en) | For the piece-rate system and its application method of MAS | |
| CN206666416U (en) | Piece-rate system for low carbon mixed alcohol | |
| CN108586185A (en) | A kind of differential pressure thermocouple propylene refining piece-rate system and separation method | |
| CN205288361U (en) | Production heat transfer device for furfuryl alcohol | |
| CN209636167U (en) | A kind of process units of modified coal tar pitch | |
| CN103755515B (en) | A kind of toluene disproportionation produces benzene and the method for dimethylbenzene and equipment thereof | |
| CN203768266U (en) | Continuous hydrogenation and isomerization hanging tetrahydrodicyclopentadiene synthesizing device | |
| CN101840220B (en) | Internal thermally coupled distillation column equilibrium stage energy saving control system and method | |
| CN201965842U (en) | Oil and gas storage and transportation combination station simulation system | |
| CN105435484B (en) | Factory-level process control system design method of multi-unit reactive distillation device based on top-down | |
| Citro et al. | Widening the applicability of reactive distillation technology by using concurrent design | |
| CN205537296U (en) | Hot load distribution device of steam direct contact heating method piece -rate system | |
| Edreder et al. | Simulation of middle vessel batch reactive distillation column: application to hydrolysis of methyl lactate | |
| CN209348149U (en) | A kind of biodiesel rectifier unit |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant |