C9 rectification production device
By designing a carbon nine distillation production device including a delight component tower, a tritoluene tower and an aromatic solvent tower, the carbon nine resources in the prior art are solved by using the thermal energy recovery and multi-stage preheater of the tower steam. The problem of waste and product supply shortage has achieved efficient carbon nine separation and large-scale production of important chemical raw materials, significantly reducing operating costs.
Patent Information
- Application Number
- CN202520030328.1
- Authority / Receiving Office
- CN · China
- Patent Type
- Utility models(China)
- Current Assignee / Owner
- Filing Date
- 2025-01-07
- Publication Date
- 2025-02-25
- Estimated Expiration
- 2035-01-07
AI Technical Summary
The lack of a production device in the prior art that can effectively utilize Carbon Nine raw materials to produce homotrityl and trityl products on a large scale has led to a shortage of these important fine organic chemical raw materials, and Carbon Nine's by-product resources have been wasted, which has brought about the Environmental issues.
A carbon nine-distillation production device was designed, including a delight component tower, a tritoluene tower and an aromatic solvent tower. Through the thermal energy recovery of the top steam and the design of a multi-stage preheater, thermal energy saving and tower conservation are achieved. Reduced cooling water.
Through the heat recovery and multi-stage preheater design, the device significantly saves the use of heat energy and the use of cooling water on the top of the tower, reduces the operating cost, and realizes the efficient separation of carbon 9 and the homotrityl and the monotritylene. Large-scale production.
Smart Images
Figure CN222517760U_ABST
Abstract
Description
Technical Field
[0001] The utility model belongs to the technical field of chemical separation, and specifically relates to a carbon nine distillation production device. Background Art
[0002] C9 aromatics mainly refer to aromatic fractions containing nine carbon atoms that are by-products of catalytic reforming and cracking to produce ethylene. The main components are cumene, n-propylbenzene, ethyltoluene, mesitylene, trimethylol, trimethylol, indene, etc. In recent years, coal chemical industry has developed rapidly. Whether it is coal-to-oil, coal-to-olefins, or coal-to-aromatics, a large amount of C9 aromatics are produced as by-products. According to incomplete statistics, my country's platinum-rhenium catalytic reforming unit alone produces nearly tens of millions of tons of C9 aromatics as by-products each year. Except for a small part of my country's heavy aromatics that are utilized, most of them are added to gasoline and diesel for use as fuel, which is a huge waste of precious resources and also brings many environmental problems. At present, there is no production equipment in China that uses C9 raw materials to produce qualified mesitylene and trimethylol products on a large scale.
[0003] Mesitylene is also a very important fine organic chemical raw material. Since there are no large-scale manufacturers in China, the domestic and foreign markets are in short supply, and the product has great benefits. Mesitylene is mainly used to synthesize M acid and dye intermediate mesitylene idine. It can also be used to produce antioxidant 330, trimesic acid, wheat field herbicide, mesitylene formaldehyde resin, etc. It is also a relatively tight variety in the international dye intermediate market, and has a very broad market in Europe, East Asia and Southeast Asia.
[0004] PMT is an important basic raw material for the development of modern new chemical materials and high value-added fine chemical products. 80% of the PMT produced in the world each year is used to produce trimellitic anhydride (abbreviated as trimellitic anhydride or TMA), which is mainly used in engineering plastics, PVC plastic plasticizers, heat-resistant insulating paints, new powder coatings and other industries; in addition, PMT can also be used as an intermediate for synthesizing vitamin E, producing mesitylene and tetramethylbenzene, etc. In recent years, with the sustained and stable development of my country's economy, the market for PMT and its downstream product trimellitic anhydride has been very hot, and PMT products are in short supply. At the same time, the export of PMT is also quite large. Utility Model Content
[0005] The utility model aims to overcome the deficiencies of the prior art and provide an energy-saving carbon nine distillation production device.
[0006] The utility model is realized by the following technical solutions:
[0007] A carbon nine distillation production device, comprising a light component removal tower, a trimethylolbenzene tower and an aromatic solvent tower, characterized in that the tower top steam outlet of the light component removal tower is connected to the heat source inlet of a first preheater, the heat source outlet of the first preheater is connected to the inlet of a recooler of the light component removal tower, the outlet of the recooler of the light component removal tower is connected to the inlet of a reflux tank of the light component removal tower, and the outlet of the reflux tank of the light component removal tower is connected to the reflux port of the light component removal tower; the material inlet of the first preheater is connected to a raw material feed pipeline, the material outlet of the first preheater is connected to the feed port of the light component removal tower, and the tower bottom discharge port of the light component removal tower is connected to the feed port of the trimethylolbenzene tower;
[0008] The tower top steam outlet of the partial trimethylbenzene tower is connected to the heat source inlet of the light component removal tower reboiler, the heat source outlet of the light component removal tower reboiler is connected to the inlet of the partial trimethylbenzene tower recooler, the outlet of the partial trimethylbenzene tower recooler is connected to the inlet of the partial trimethylbenzene tower reflux tank, the outlet of the partial trimethylbenzene tower reflux tank is connected to the reflux port of the partial trimethylbenzene tower, and the tower bottom discharge port of the partial trimethylbenzene tower is connected to the feed port of the aromatic solvent tower;
[0009] The top steam outlet of the aromatic solvent tower is connected to the heat source inlet of the trimethylol tower reboiler, the heat source outlet of the trimethylol tower reboiler is connected to the inlet of the aromatic solvent tower recooler, the outlet of the aromatic solvent tower recooler is connected to the inlet of the aromatic solvent tower reflux tank, and the outlet of the aromatic solvent tower reflux tank is connected to the reflux port of the aromatic solvent tower. The kettle of the aromatic solvent tower is provided with an aromatic solvent tower reboiler, the heat source inlet of the aromatic solvent tower reboiler is connected to the heat transfer oil inlet pipeline, and the heat source outlet of the aromatic solvent tower reboiler is connected to the heat transfer oil return pipeline.
[0010] In the above technical solution, a second preheater is provided between the material outlet of the first preheater and the feed inlet of the light component removal tower, the material outlet of the first preheater is connected to the material inlet of the second preheater, and the material outlet of the second preheater is connected to the feed inlet of the light component removal tower.
[0011] In the above technical solution, the heat source inlet of the second preheater is connected to the heat transfer oil inlet pipeline, and the heat source outlet of the second preheater is connected to the heat transfer oil return pipeline.
[0012] In the above technical solution, the light component removal tower, the trimethylol tower and the aromatic solvent tower are all packed towers made of carbon steel.
[0013] In the above technical solution, a side line production outlet is provided on the tower body of the aromatic solvent tower.
[0014] The advantages and beneficial effects of the utility model are:
[0015] 1. The carbon nine separation production device of the utility model uses the top steam of the trimethylbenzene tower and the aromatic solvent tower as the heat medium of the tower bottom of the light component removal tower and the trimethylbenzene tower to heat the tower bottom liquid, which saves heat energy and reduces the amount of circulating cooling water at the top of the tower, thereby greatly saving operating costs;
[0016] 2. The utility model is provided with a first preheater to exchange heat between the top steam of the light component removal tower and the raw material, thereby recovering a large amount of waste heat from the top of the tower and making the device more energy-efficient. BRIEF DESCRIPTION OF THE DRAWINGS
[0017] Figure 1 It is a simplified flow chart of Example 1 of the utility model;
[0018] Among them, 1 is a light component removal tower, 2 is a light component removal tower reboiler, 3 is a trimethylolbenzene tower, 4 is a trimethylolbenzene tower reboiler, 5 is an aromatic solvent tower, 6 is an aromatic solvent tower reboiler, 7 is an aromatic solvent tower reflux tank, 8 is an aromatic solvent tower recooler, 9 is a trimethylolbenzene tower reflux tank, 10 is a trimethylolbenzene tower recooler, 11 is a light component removal tower reflux tank, 12 is a light component removal tower recooler, 13 is a first preheater, and 14 is a second preheater. DETAILED DESCRIPTION
[0019] In order to enable those skilled in the art to better understand the solution of the utility model, the technical solution of the utility model is further described below in conjunction with the accompanying drawings and specific embodiments. Example 1
[0020] like Figure 1 As shown, a carbon nine distillation production device includes a light component removal tower 1, a partial trimethylol tower 3 and an aromatic solvent tower 5, the tower top steam outlet of the above-mentioned light component removal tower is connected to the heat source inlet of the first preheater 13, the heat source outlet of the above-mentioned first preheater is connected to the inlet of the light component removal tower subcooler 12, the outlet of the above-mentioned light component removal tower subcooler is connected to the inlet of the light component removal tower reflux tank 11, the outlet of the above-mentioned light component removal tower reflux tank is connected to the reflux port of the light component removal tower, and there is a branch on the pipeline connecting the outlet of the light component removal tower reflux tank and the reflux port of the light component removal tower for extracting the tower top product; the material inlet of the first preheater is connected to the raw material feed pipeline, the material outlet of the above-mentioned first preheater is connected to the material inlet of the second preheater, the material outlet of the second preheater is connected to the feed port of the above-mentioned light component removal tower, the heat source inlet of the above-mentioned second preheater is connected to the heat transfer oil inlet pipeline, and the heat source outlet of the second preheater is connected to the heat transfer oil return pipeline. The discharge port of the bottom of the light component removal tower is connected to the feed port of the trimethylol tower;
[0021] The tower top steam outlet of the above-mentioned trimethylbenzene tower is connected to the heat source inlet of the light component removal tower reboiler 2, the heat source outlet of the above-mentioned trimethylbenzene tower reboiler is connected to the inlet of the trimethylbenzene tower recooler 10, the outlet of the above-mentioned trimethylbenzene tower recooler is connected to the inlet of the trimethylbenzene tower reflux tank 9, the outlet of the above-mentioned trimethylbenzene tower reflux tank is connected to the reflux port of the above-mentioned trimethylbenzene tower, and there is a branch on the connecting pipeline between the outlet of the trimethylbenzene tower reflux tank and the reflux port of the trimethylbenzene tower, which is used to extract the tower top product. The tower bottom discharge port of the above-mentioned trimethylbenzene tower is connected to the feed port of the aromatic solvent tower;
[0022] The tower top steam outlet of the above-mentioned aromatic solvent tower is connected to the heat source inlet of the trimethylol tower reboiler 4, the heat source outlet of the above-mentioned trimethylol tower reboiler is connected to the inlet of the aromatic solvent tower recooler 8, the outlet of the above-mentioned aromatic solvent tower recooler is connected to the inlet of the aromatic solvent tower reflux tank 7, the outlet of the above-mentioned aromatic solvent tower reflux tank is connected to the reflux port of the aromatic solvent tower, and there is a branch on the connecting pipeline between the outlet of the aromatic solvent tower reflux tank and the reflux port of the aromatic solvent tower, which is used to extract the tower top product. The tower kettle of the above-mentioned aromatic solvent tower is provided with an aromatic solvent tower reboiler 6, the heat source inlet of the above-mentioned aromatic solvent tower reboiler is connected to the heat transfer oil inlet pipeline, and the heat source outlet of the aromatic solvent tower reboiler is connected to the heat transfer oil return pipeline. A side line extraction port is provided on the tower body of the above-mentioned aromatic solvent tower for extracting the side line product.
[0023] The above-mentioned light component removal tower, trimethylol tower and aromatic solvent tower are all packed towers made of carbon steel.
[0024] The production device of the present embodiment is a three-tower continuous distillation device, with a raw material processing capacity of 200,000 tons / year, which can produce 80,000 tons / year of trimethylol and 10,000 tons / year of mesitylene products. The C9 raw material reaches a feed temperature of 140°C after passing through the first preheater and the second preheater in turn, and enters the light component removal tower for distillation. The tower top temperature of the light component removal tower is 165°C, the pressure is 100kpaA, and the tower bottom temperature is 172°C. The tower top steam of the tower is exchanged with the raw material through the first heat exchanger, and then cooled by the light component removal tower recooler to reach the reflux temperature, and a part of it is refluxed and a part is extracted. The extracted tower top product is mesitylene enriched liquid and enters the downstream section for further refining. The tower bottom liquid of the light component removal tower is pumped into the trimethylol tower for further distillation. The tower top temperature of the trimethylol tower is 183°C, the pressure is 100kpaA, and the tower bottom temperature is 190°C. The tower top steam of the trimethylol tower enters the light component removal tower reboiler as a heat source to heat the tower bottom. The light component removal tower and the trimethylolbenzene tower are both equipped with a supplementary heat reboiler (not shown in the figure) to use heat transfer oil as a heat source to supplement heat to the distillation tower kettle. After the top steam of the trimethylolbenzene tower is condensed, it enters the trimethylolbenzene tower recooler and is further cooled to the reflux temperature. A part of it is refluxed and a part of it is extracted as the trimethylolbenzene product. The bottom liquid of the trimethylolbenzene tower enters the aromatic solvent tower for further distillation. The top temperature of the aromatic solvent tower is 202°C, the pressure is 100kpaA, and the bottom temperature is 215°C. The top steam of the aromatic solvent tower enters the trimethylolbenzene tower reboiler as a heat source to heat the tower kettle. After the top steam of the aromatic solvent tower is condensed, it enters the aromatic solvent tower recooler and is further cooled to the reflux temperature. Then a part of it is refluxed and a part of it is extracted as the trimethylolbenzene product. The bottom liquid of the aromatic solvent tower is mainly a high-boiling point heavy aromatic solvent, which is pumped into the tank area product tank for storage and sales. The side line extraction outlet of the aromatic solvent tower produces 1000#B solvent.
[0025] In this embodiment, the raw material is heat-exchanged with the top steam of the light component removal tower through the first preheater, and the waste heat of the top of the tower is recovered, making the device more energy-efficient. In addition, the top steam of the trimethylolbenzene tower and the aromatic solvent tower are used as the heat medium of the bottom of the light component removal tower and the trimethylolbenzene tower to heat the bottom liquid, which saves heat energy and reduces the amount of circulating cooling water at the top of the tower, which can greatly save operating costs. By fully recovering the heat energy of the top steam, the carbon nine distillation production device of the utility model can save more than 38% energy compared with the prior art.
[0026] The above is an exemplary description of the present invention. It should be noted that, without departing from the core of the present invention, any simple deformation, modification or other equivalent replacement that can be done by other technical personnel in this field without expending creative labor falls within the protection scope of the present invention.
Claims
1. A carbon nine distillation production device, comprising a light component removal tower (1), a trimethylolbenzene tower (3) and an aromatic solvent tower (5), characterized in that: The top steam outlet of the light component removal tower is connected to the heat source inlet of the first preheater (13), the heat source outlet of the first preheater is connected to the inlet of the light component removal tower recooler (12), the outlet of the light component removal tower recooler is connected to the inlet of the light component removal tower reflux tank (11), and the outlet of the light component removal tower reflux tank is connected to the reflux port of the light component removal tower; the material inlet of the first preheater is connected to the raw material feed pipeline, the material outlet of the first preheater is connected to the feed port of the light component removal tower, and the tower bottom discharge port of the light component removal tower is connected to the feed port of the trimethylol tower; The tower top steam outlet of the trimethylolbenzene tower is connected to the heat source inlet of the light component removal tower reboiler (2), the heat source outlet of the trimethylolbenzene tower reboiler is connected to the inlet of the trimethylolbenzene tower recooler (10), the outlet of the trimethylolbenzene tower recooler is connected to the inlet of the trimethylolbenzene tower reflux tank (9), the outlet of the trimethylolbenzene tower reflux tank is connected to the reflux port of the trimethylolbenzene tower, and the tower bottom discharge port of the trimethylolbenzene tower is connected to the feed port of the aromatic solvent tower; The top steam outlet of the aromatic solvent tower is connected to the heat source inlet of the trimethylolbenzene tower reboiler (4), the heat source outlet of the trimethylolbenzene tower reboiler is connected to the inlet of the aromatic solvent tower recooler (8), the outlet of the aromatic solvent tower recooler is connected to the inlet of the aromatic solvent tower reflux tank (7), the outlet of the aromatic solvent tower reflux tank is connected to the reflux port of the aromatic solvent tower, the kettle of the aromatic solvent tower is provided with an aromatic solvent tower reboiler (6), the heat source inlet of the aromatic solvent tower reboiler is connected to the heat transfer oil inlet pipeline, and the heat source outlet of the aromatic solvent tower reboiler is connected to the heat transfer oil return pipeline.
2. A carbon nine distillation production device according to claim 1, characterized in that: A second preheater (14) is provided between the material outlet of the first preheater and the feed inlet of the light component removal tower, the material outlet of the first preheater is connected to the material inlet of the second preheater, and the material outlet of the second preheater is connected to the feed inlet of the light component removal tower.
3. A carbon nine distillation production device according to claim 2, characterized in that: The heat source inlet of the second preheater is connected to the heat transfer oil inlet pipeline, and the heat source outlet of the second preheater is connected to the heat transfer oil return pipeline.
4. A carbon nine distillation production device according to claim 3, characterized in that: The light component removal tower, the trimethylol tower and the aromatic solvent tower are all packed towers made of carbon steel.
5. A carbon nine distillation production device according to claim 4, characterized in that: The aromatic hydrocarbon solvent tower is provided with a side line extraction outlet on the tower body.