Product refining energy-saving device

Abstract

The utility model relates to a product refining energy -conserving device belongs to product refining field, the product refining energy -conserving device includes two parts of primary separation and refining, realizes one -step removal light component and heavy component through separating primary separation tower inner area, realizes three products refining simultaneously through separating refining tower inner area, improves product purity and realizes energy -conserving purpose simultaneously. Utilize compressor to convert primary separation low grade waste heat into the high grade heat source needed for primary separation and refining, convert refining low grade waste heat into the high grade heat source needed for refining, replace using traditional heat medium and refrigerant, realize energy -conserving purpose. The product refining energy -conserving device realizes energy -conserving and consumption reduction simultaneously and reduces the equipment's investment cost, has important significance.

Description

Technical Field

[0001] This utility model relates to product refining, specifically to an energy-saving device for product refining. Background Technology

[0002] In industries such as chemical, petroleum, pharmaceutical, food, and environmental protection, product refining is a crucial step in producing high-purity substances, but the separation processes involved in product refining are typically energy-intensive. Existing separation technologies, such as distillation columns, rely on high-temperature heating and low-temperature cooling, resulting in significant energy waste. Furthermore, the separation and refining of certain near-boiling-point mixtures or ultra-high-purity chemicals often requires numerous columns operating at extremely high reflux ratios for repeated distillation, leading to enormous energy consumption and very high operating and equipment costs.

[0003] In summary, it is evident that developing a highly efficient, low-energy-consumption, and adaptable product refining energy-saving device, integrating a novel separation system with energy recovery and reuse technology, is of great significance for reducing production costs and achieving green manufacturing and production. Utility Model Content

[0004] The purpose of this invention is to overcome the shortcomings of existing technologies and provide an energy-saving device for product refining. On the one hand, it recovers and reuses waste heat in the device, efficiently converting it into the heating source required by the device, thus achieving energy saving. On the other hand, it refines different products in different areas of the separator tower, reducing the number of equipment required for product refining, while further improving the purity of the products and achieving energy saving.

[0005] To achieve the above objectives, this utility model provides the following technical solution: A product refining energy-saving device includes a primary separation tower, a primary separation condenser, a primary separation reboiler, a primary separation heat exchanger, a first buffer tank, a first pressurizing pump, a first compressor, a refining tower, a first reboiler, a second reboiler, a third reboiler, a second buffer tank, a second pressurizing pump, and a second compressor.

[0006] The initial separation tower includes three zones: light component removal (A), purification (B), and heavy component removal (C), while the refining tower includes three zones: refining (D), refining (E), and refining (F).

[0007] The primary condenser's cold side is connected to the middle of the light component removal area A of the primary condenser tower via a material pipeline; the primary condenser's hot side is connected to the top of the light component removal area A of the primary condenser tower via a material pipeline; the primary reboiler's cold side is connected to the bottom of the heavy component removal area C of the primary condenser tower via a material pipeline; the primary heat exchanger's cold side is connected to the heavy component removal area C of the primary condenser tower via a material pipeline; the primary condenser's purification area B, the first compressor, the first reboiler's hot side, the primary heat exchanger's hot side, the first buffer tank, the first pressurizing pump, and the middle of the refining area E of the refining tower via a material pipeline; the refining area D of the refining tower, the second compressor, the second reboiler's hot side, the third reboiler's hot side, the second buffer tank, and the second pressurizing pump via a material pipeline; the refining area E of the refining tower, the first reboiler's cold side, and the second reboiler's cold side via a material pipeline; and the refining area F of the refining tower, the third reboiler's cold side via a material pipeline, forming an energy-saving device.

[0008] Furthermore, a partition plate is installed in the upper middle part of the primary separation tower to divide the primary separation tower into three areas: light removal A, purification B, and heavy removal C. The light removal A area is equipped with a feed inlet in the middle, and the heavy removal C area is equipped with a liquid outlet and a gas return outlet.

[0009] Furthermore, a partition plate is installed in the lower middle part of the refining tower, dividing the refining tower into three areas: refining D, refining E, and refining F. The feed inlet is located in the middle of the refining E area.

[0010] Furthermore, the primary separation tower and the refining tower are equipped with mass transfer packing and tower internals or tower plates.

[0011] Furthermore, a gas distribution device is installed at the top of the deweighting C zone of the primary separation tower.

[0012] Furthermore, a liquid distribution device is installed at the bottom of the refining D zone of the refining tower.

[0013] Furthermore, the first and second buffer tanks are equipped with heat exchange tubes, which are connected to refrigerant.

[0014] Furthermore, the primary condenser consists of one or more components.

[0015] Furthermore, the primary heat exchanger is connected to the deweighting C region of the primary separation tower.

[0016] Furthermore, a distribution device with liquid collection function is installed at the location where the primary separation tower connects to the primary separation heat exchanger.

[0017] The aforementioned product refining and energy-saving device achieves product refining and energy saving through the following steps: After the raw material enters the cold side of the primary condenser and exchanges heat with the gas on the hot side, it enters the middle of the light component removal zone A of the primary separator. The gas at the top of the light component removal zone A enters the hot side of the primary condenser and exchanges heat with the raw material on the cold side, condensing. Part of the condensate returns to the top of the light component removal zone A, and the rest is collected as light components. The gas at the top of the purification zone B of the primary separator is pressurized by the first compressor and enters the hot side of the first reboiler and the hot side of the primary heat exchanger. After exchanging heat with the materials on the cold side of the first reboiler and the cold side of the primary heat exchanger, it liquefies. After passing through the first buffer tank and the first pressurization pump, part of the liquefaction occurs at the top of the purification zone B of the primary separator, and the rest is collected as a purified mixture entering the middle of the purification zone E of the purification tower. The liquid at the bottom of the heavy component removal zone C of the primary separator partially enters the cold side of the primary reboiler and exchanges heat with the heat medium on the hot side, vaporizing before returning to the heavy component removal zone C of the primary separator. At the bottom, some heavy components are extracted; after purification, the mixture enters the middle of the refining zone E of the refining tower. Part of the liquid at the bottom of the refining zone E is extracted as product three, and part enters the cold side of the first and second reboilers. After being heated and vaporized by the hot-side material, it returns to the bottom of the refining zone E. The gas at the top of the refining zone D is pressurized by the second compressor and enters the hot side of the second and third reboilers. After exchanging heat with the materials on the cold sides of the second and third reboilers respectively, it liquefies. After passing through the second buffer tank and the second pressurizing pump, part of it enters the top of the refining zone D, and part is extracted as product one. The liquid at the bottom of the refining zone F enters the cold side of the third reboiler, exchanges heat with the materials on the hot side of the third reboiler, vaporizes, and returns to the bottom of the refining zone F, and part is extracted as product two.

[0018] The product refining and energy-saving device described in this utility model has the following beneficial effects: (1) The present invention discloses a product refining energy-saving device, which achieves the refining of different products by dividing the area in the tower, reducing the number of tower equipment while improving the quality of the products, not only achieving the energy-saving effect, but also reducing the investment cost of the device.

[0019] (2) The present invention discloses a product refining energy-saving device in which the heat at the top of the light A zone of the primary separation tower is used to heat the raw materials, which not only saves the amount of heating medium used in the primary separation tower, but also eliminates the need for refrigerant in the primary separation condenser, thus achieving energy-saving effect.

[0020] (3) The product refining energy-saving device disclosed in this utility model uses the heat from the top of the B zone of the primary separation tower to improve the grade and then use it as the heat source for the first reboiler and the primary separation heat exchanger. This not only saves the amount of heating medium used in the primary separation tower and the refining tower, but also eliminates the need for the refrigerant required for the condensation of the gas at the top of the B zone of the primary separation tower, thus achieving energy-saving effect.

[0021] (4) The present invention discloses a product refining energy-saving device, in which the heat at the top of the refining D zone of the refining tower is used as the heat source for the second and third reboilers after the heat is improved. This not only saves the amount of heating medium used in the refining tower, but also eliminates the need for the refrigerant required for the condensation of the gas at the top of the refining D zone of the refining tower, thus achieving energy-saving effect.

[0022] (5) The present invention discloses a product refining energy-saving device. The entire device only requires a small amount of heat medium heating for the primary separation tower reboiler, which saves more than 80% of the overall energy consumption compared with the prior art. Attached Figure Description

[0023] To further illustrate this utility model, the following figures are provided: Figure 1 This is a schematic diagram of the energy-saving device according to Embodiment 1 of this utility model.

[0024] Figure 2 This is a schematic diagram of the energy-saving device in Embodiment 2 of this utility model.

[0025] Figure 3 This is a schematic diagram of the energy-saving device in Embodiment 3 of this utility model.

[0026] Explanation of reference numerals in the attached diagram: 1 is the initial separation column; 2 is the initial separation condenser; 3 is the initial separation reboiler; 4 is the initial separation heat exchanger; 5 is the first buffer tank; 6 is the first pressurizing pump; 7 is the first compressor; 8 is the refining column; 9 is the first reboiler for refining; 10 is the second reboiler for refining; 11 is the third reboiler for refining; 12 is the second buffer tank; 13 is the second pressurizing pump; 14 is the second compressor; 15 is the mass transfer packing and internal components of the column or the tray; 16 is the partition plate; 17 is the gas distribution device. ; 18 is a liquid distribution device; 19 is a heat exchange tube; 20 is a distribution device with liquid collection function; 21 is the primary separator second condenser; A is the area for separating light components (A) in the primary separator; B is the area for separating and purifying components (B) in the primary separator; C is the area for separating heavy components (C) in the primary separator; D is the area for separating and refining components (D) in the refining tower; E is the area for separating and refining components (E) in the refining tower; F is the area for separating and refining components (F) in the refining tower; HWS is the heat transfer medium inlet; HWR is the heat transfer medium return; RWS is the refrigerant inlet; RWR is the refrigerant return. Detailed Implementation

[0027] The present invention will now be described in further detail with reference to the accompanying drawings and specific embodiments. Example 1

[0028] Reference Figure 1This embodiment provides a product refining energy-saving device, including a primary separation tower 1, a primary separation condenser 2, a primary separation reboiler 3, a primary separation heat exchanger 4, a first buffer tank 5, a first pressurizing pump 6, a first compressor 7, a refining tower 8, a refining first reboiler 9, a refining second reboiler 10, a refining third reboiler 11, a second buffer tank 12, a second pressurizing pump 13, and a second compressor 14.

[0029] The primary separator 1 is equipped with a partition plate 16 in its upper middle section, dividing it into three zones: light component removal (A), purification (B), and heavy component removal (C). The light component removal (A) zone has a feed inlet in its middle, while the heavy component removal (C) zone has a liquid outlet and a gas return outlet. A gas distribution device 17 is installed at the top of the heavy component removal (C) zone, and a distribution device 20 with liquid collection function is installed at the connection point with the primary separator heat exchanger 4.

[0030] The refining tower 8 has a partition plate 16 installed in the lower middle part, dividing the refining tower into three areas: refining D, refining E, and refining F. A feed inlet is set in the middle of the refining E area, and a liquid distribution device 18 is installed at the bottom of the refining D area.

[0031] A material pipeline connects the cold side of the primary condenser 2 to the middle of the light-light removal A zone of the primary separation tower 1. A material pipeline connects the hot side of the primary condenser 2 to the top of the light-light removal A zone of the primary separation tower 1. A material pipeline connects the cold side of the primary reboiler 3 to the bottom of the heavy removal C zone of the primary separation tower 1. A material pipeline connects the cold side of the primary heat exchanger 4 to the heavy removal C zone of the primary separation tower 1. A material pipeline connects sequentially between the top of the purification B zone of the primary separation tower 1, the first compressor 7, the hot side of the first reboiler 9, the hot side of the primary heat exchanger 4, the first buffer tank 5, the first pressurizing pump 6, and the middle of the purification E zone of the purification tower 8. A material pipeline connects sequentially between the top of the purification D zone of the purification tower 8, the second compressor 14, the hot side of the second reboiler 10, the hot side of the third reboiler 11, the second buffer tank 12, and the second pressurizing pump 13. A material pipeline connects sequentially between the bottom of the purification E zone of the purification tower 8 and the first reboiler 9. A material pipeline connects the cold side of the refining second reboiler 10 and the cold side of the refining tower 8 and the refining F zone bottom to the cold side of the refining third reboiler 11, forming an energy-saving device.

[0032] When using the product refining energy-saving device provided in this embodiment for product refining, the following steps are included: After the raw material enters the cold side of the primary condenser 2 and exchanges heat with the gas on the hot side of the primary condenser 2, it enters the middle of the light component removal A zone of the primary separation tower 1. The gas at the top of the light component removal A zone of the primary separation tower 1 enters the hot side of the primary condenser 2 and exchanges heat with the raw material on the cold side of the primary condenser 2, and after condensation, part of it returns to the top of the light component removal A zone of the primary separation tower 1, and part of it is collected as light components. The gas at the top of the purification B zone of the primary separation tower 1 is pressurized by the first compressor 7 and then enters the hot side of the first reboiler 9 and the hot side of the primary heat exchanger 4. After exchanging heat with the materials on the cold side of the first reboiler 9 and the cold side of the primary heat exchanger 4, it is liquefied. After passing through the first buffer tank 5 and the first pressurizing pump 6, part of it enters the top of the purification B zone of the primary separation tower 1, and part of it is collected as the purified mixture enters the middle of the purification E zone of the refining tower 8. The liquid at the bottom of the heavy component removal zone C is partially vaporized by heat exchange between the cold side of the primary reboiler 3 and the heat medium on the hot side of the primary reboiler 3, and then returned to the bottom of the heavy component removal zone C of the primary separator 1. The purified mixture enters the middle of the refining zone E of the refining tower 8. Part of the liquid at the bottom of the refining zone E of the refining tower 8 is product three, and part enters the cold side of the first reboiler 9 and the cold side of the second reboiler 10. After being vaporized by the hot side material, it returns to the bottom of the refining zone E of the refining tower 8. The gas at the top of the refining zone D of the refining tower 8 is pressurized by the second compressor 14 and then enters the hot side of the second reboiler 10 and the hot side of the third reboiler 11. After liquefying by heat exchange with the materials on the cold sides of the second and third reboilers 10 and 11 respectively, part of it enters the refining tower 8 after passing through the second buffer tank 12 and the second pressurizing pump 13. At the top of the refining zone D, part of product one is extracted; at the bottom of the refining zone F of refining tower 8, part of the liquid enters the cold side of the refining third reboiler 11 and exchanges heat with the material on the hot side of the refining third reboiler 11, then returns to the bottom of the refining zone F of refining tower 8, where part of product two is extracted.

[0033] In this embodiment, the raw material is crude phenol from tar, with a processing capacity of 35,000 tons / year. The mass content of the raw material components is as follows: water 0.473%, light phenols 0.473%, phenol 48.424%, o-cresol 10.315%, p-cresol 11.262%, m-cresol 16.4%, o-ethylphenol 0.653%, 2,4-xylenol 1.968%, and slag phenol 10.031%. After processing by the product refining and energy-saving device described in this utility model, the stable output products are: product one, phenol with a mass concentration of 99.99%; product two, o-cresol with a mass concentration of 99.8%; and product three, m-p-cresol with a mass concentration of 97.2%. The light components are water and light phenols, and the heavy components are slag phenols.

[0034] In this embodiment, the number of trays in the light-removal A region of the primary separation tower is 25; the number of trays in the purification B region of the primary separation tower is 38; the number of trays in the heavy-removal C region of the primary separation tower is 22; the number of trays in the purification D region of the refining tower is 48; the number of trays in the purification E region of the refining tower is 48; and the number of trays in the purification F region of the refining tower is 45.

[0035] In this embodiment, the operating pressure of the primary separation column is 15 kPa; the operating pressure of the purification column is 15 kPa.

[0036] In this embodiment, the compression ratio of the first compressor is 2.52; the compression ratio of the second compressor is 2.96.

[0037] In this embodiment, the gas at the top of the heavy removal zone C of the primary separation tower is distributed to the light removal zone A and the purification zone B via the gas distribution device 17 at a ratio of 0.15; the liquid at the bottom of the purification zone D of the purification tower is distributed to the purification zone E and the purification zone F via the liquid distribution device 18 at a ratio of 0.32.

[0038] In this embodiment, the liquid at the top of the C region of the primary separation tower is extracted and enters the cold side of the primary separation heat exchanger to exchange heat with the gas on the hot side of the primary separation heat exchanger.

[0039] In this embodiment, the heat transfer medium can be steam, heat transfer oil, or electric heating, with heat transfer oil being preferred.

[0040] In this embodiment, the operating temperature of the light component removal A zone at the top of the primary separation column is 66.8°C, the operating temperature of the purification B zone at the top of the primary separation column is 132.7°C, and the operating temperature of the heavy component removal C zone at the bottom of the primary separation column is 197.8°C; the operating temperature of the purification D zone at the top of the refining column is 123.8°C, the operating temperature of the purification E zone at the bottom of the refining column is 143.6°C, and the operating temperature of the purification F zone at the bottom of the refining column is 132.1°C.

[0041] In this embodiment, the waste heat is fully utilized by the compressor. The first compressor 7 pressurizes the secondary steam in the purification zone B at the top of the primary separation tower 1 to increase its grade. The outlet temperature of the first compressor is 158.8°C. The steam enters the hot side of the first reboiler 9 and the hot side of the primary separation heat exchanger 4, heating and vaporizing the materials on the cold side of the first reboiler 9 and the cold side of the primary separation heat exchanger 4. At the same time, the steam itself is condensed. This not only saves the heat transfer medium required for the hot side of the first reboiler 9 and the hot side of the primary separation heat exchanger 4, but also saves the refrigerant required for the condensation of the secondary steam in the purification zone B at the top of the primary separation tower 1. The second compressor 14 pressurizes and improves the grade of the secondary steam in the top refining zone D of the refining tower 8. The outlet temperature of the second compressor is 156.1℃. The steam enters the hot side of the second reboiler 10 and the hot side of the third reboiler 11, heating and vaporizing the material on the cold side of both refining zones. Simultaneously, the steam itself is condensed, saving the heat transfer medium required for the hot sides of the second and third reboilers and the refrigerant required for the secondary steam condensation in the top refining zone D of the refining tower 8. The entire unit only requires heat transfer medium on the hot side of the initial reboiler 3; the first buffer tank 5 and the second buffer tank 12 require refrigerant. Compared with existing technology, the production of each ton of phenol can save 228.1 tons of heat transfer oil, which is 89.5% less, and 266.4 tons of refrigerant circulating water, which is 94.6% less. The power consumption of the compressor required to produce each ton of phenol is 117.8 kWh, resulting in a significant reduction in overall energy consumption.

[0042] In this embodiment, the ratio of the top gas from the heavy component removal zone C of the primary separation tower to the light component removal zone A and the purification zone B is adjusted, so that the primary separation tower can simultaneously remove both light and heavy components. Similarly, the ratio of the bottom liquid from the purification zone D of the purification tower to the purification zones E and F is adjusted, so that the purification tower can simultaneously purify products one, two, and three. Compared to existing technologies, this method saves two towers, reduces equipment investment, and also lowers energy consumption. Example 2

[0043] Reference Figure 2 This embodiment provides a product refining energy-saving device. The difference between this embodiment and Embodiment 1 is that the hot side of the first reboiler 9 and the hot side of the primary separation heat exchanger 4 are connected in parallel to the top of the light residue A area of ​​the primary separation tower 1, the first compressor 7, the first buffer tank 5, the first pressurizing pump 6, and the middle of the refining E area of ​​the refining tower 8, and are connected by a material pipeline; the hot side of the second reboiler 10 and the hot side of the third reboiler 11 are connected in parallel to the top of the refining D area of ​​the refining tower 8, the second compressor 14, the second buffer tank 12, and the second pressurizing pump 13, and are connected by a material pipeline.

[0044] When using the product refining energy-saving device provided in this embodiment for product refining, the following steps are included: After the raw material enters the cold side of the primary condenser 2 and exchanges heat with the gas on the hot side of the primary condenser 2, it enters the middle of the light component removal A zone of the primary separation tower 1. The top gas of the light component removal A zone of the primary separation tower 1 enters the hot side of the primary condenser 2 and exchanges heat with the raw material on the cold side of the primary condenser 2, and after condensation, part of it returns to the top of the light component removal A zone of the primary separation tower 1, and part of it is collected as light components. The gas at the top of the purification B zone of the primary separation tower 1 is pressurized by the first compressor 7 and enters the hot side of the first reboiler 9 and the hot side of the primary heat exchanger 4 respectively. After exchanging heat with the materials on the cold side of the first reboiler 9 and the cold side of the primary heat exchanger 4 respectively, it is liquefied. After passing through the first buffer tank 5 and the first pressurizing pump 6, part of it enters the top of the purification B zone of the primary separation tower 1, and part of it is collected as the purified mixture enters the middle of the purification E zone of the refining tower 8. The liquid at the bottom of the C-zone of the heavy component removal column is partially vaporized by heat exchange with the heat medium on the cold side of the primary reboiler 3 and then returned to the bottom of the C-zone of the primary column 1. A portion of the heavy component is collected. The purified mixture enters the middle of the E-zone of the refining column 8. Part of the liquid at the bottom of the E-zone of the refining column 8 is collected as product three, and part enters the cold side of the first reboiler 9 and the cold side of the second reboiler 10. After being vaporized by the hot side material, it returns to the bottom of the E-zone of the refining column 8. The gas at the top of the D-zone of the refining column 8 is pressurized by the second compressor 14 and then enters the hot side of the second reboiler 10 and the hot side of the third reboiler 11. After liquefying by heat exchange with the materials on the cold side of the second reboiler 10 and the third reboiler 11, a portion of the gas then enters the refining column 8 via the second buffer tank 12 and the second pressurizing pump 13. At the top of the refining zone D, part of product one is extracted; at the bottom of the refining zone F of refining tower 8, part of the liquid enters the cold side of the refining third reboiler 11 and exchanges heat with the material on the hot side of the refining third reboiler 11, then returns to the bottom of the refining zone F of refining tower 8, where part of product two is extracted.

[0045] The raw materials processed in this embodiment are the same as those in Embodiment 1. The difference is that in Embodiment 1, the gas pressurized by the first compressor 7 enters the hot side of the first reboiler 9 and the hot side of the primary heat exchanger 4 sequentially, and the gas pressurized by the second compressor 14 enters the hot side of the second reboiler 10 and the hot side of the third reboiler 11 sequentially. In this embodiment, the gas pressurized by the first compressor 7 enters the hot side of the first reboiler 9 and the hot side of the primary heat exchanger 4 respectively, and the gas pressurized by the second compressor 14 enters the hot side of the second reboiler 10 and the hot side of the third reboiler 11 respectively.

[0046] In this embodiment, the ratio of the gas pressurized by the first compressor 7 entering the hot side of the first reboiler 9 and the hot side of the primary heat exchanger 4 is 1:13, and the ratio of the gas pressurized by the second compressor 14 entering the hot side of the second reboiler 10 and the hot side of the third reboiler 11 is 2:5.

[0047] This embodiment provides a product refining energy-saving device, whose energy-saving effect is the same as that of Embodiment 1. Example 3

[0048] Reference Figure 3 This embodiment provides a product refining energy-saving device, including a primary separation tower 1, a primary separation condenser 2, a primary separation reboiler 3, a primary separation heat exchanger 4, a first buffer tank 5, a first pressurizing pump 6, a first compressor 7, a refining tower 8, a refining first reboiler 9, a refining second reboiler 10, a refining third reboiler 11, a second buffer tank 12, a second pressurizing pump 13, a second compressor 14, and a primary separation second condenser 21.

[0049] The primary separator 1 is equipped with a partition plate 16 in its upper middle section, dividing it into three zones: light component removal (A), purification (B), and heavy component removal (C). The light component removal (A) zone has a feed inlet in its middle, while the heavy component removal (C) zone has a liquid outlet and a gas return outlet. A gas distribution device 17 is installed at the top of the heavy component removal (C) zone, and a distribution device 20 with liquid collection function is installed at the connection point with the primary separator heat exchanger 4.

[0050] The refining tower 8 has a partition plate 16 installed in the lower middle part, dividing the refining tower into three areas: refining D, refining E, and refining F. A feed inlet is set in the middle of the refining E area, and a liquid distribution device 18 is installed at the bottom of the refining D area.

[0051] A material pipeline connects the cold side of the primary condenser 2 to the middle of the light-weight removal A zone of the primary separation tower 1. A material pipeline connects the hot side of the primary condenser 2 and the hot side of the primary second condenser 21 to the top of the light-weight removal A zone of the primary separation tower 1. A material pipeline connects the cold side of the primary reboiler 3 to the bottom of the heavy-weight removal C zone of the primary separation tower 1. A material pipeline connects the cold side of the primary heat exchanger 4 to the heavy-weight removal C zone of the primary separation tower 1. A material pipeline sequentially connects the top of the purification B zone of the primary separation tower 1, the first compressor 7, the hot side of the first reboiler 9, the hot side of the primary heat exchanger 4, the first buffer tank 5, the first pressurizing pump 6, and the middle of the purification E zone of the purification tower 8. A material pipeline sequentially connects the top of the purification D zone of the purification tower 8, the second compressor 14, the hot side of the second reboiler 10, the hot side of the third reboiler 11, the second buffer tank 12, and the second pressurizing pump 13. Material pipelines connect the bottom of the refining zone E, the cold side of the first reboiler 9, and the cold side of the second reboiler 10. Material pipelines also connect the bottom of the refining zone F of the refining tower 8 and the cold side of the third reboiler 11, forming an energy-saving device.

[0052] When using the product refining energy-saving device provided in this embodiment for product refining, the following steps are included: After the raw material enters the cold side of the primary condenser 2 and exchanges heat with the gas on the hot side of the primary condenser 2, it enters the middle of the light component removal A zone of the primary separation tower 1. The top gas of the light component removal A zone of the primary separation tower 1 enters the hot side of the primary condenser 2 and exchanges heat with the raw material on the cold side of the primary condenser 2, then condenses, with part returning to the top of the light component removal A zone of the primary separation tower 1, and part being collected as water and light components. The uncondensed gas on the hot side of the primary condenser 2 enters the hot side of the primary separation second condenser 21, exchanges heat with the refrigerant on the cold side of the primary separation second condenser 21, and condenses, then returns together with the condensate on the hot side of the primary condenser 2, with part returning to the top of the light component removal A zone of the primary separation tower 1, and part being collected as light components. The gas at the top of the purification B zone of the primary separation tower 1 is pressurized by the first compressor 7 and then enters the hot side of the first reboiler 9 and the hot side of the primary heat exchanger 4, respectively, and exchanges heat with the first reboiler 9. After the material on the cold side and the cold side of the primary heat exchanger 4 is liquefied through heat exchange, it enters the top of the purification zone B of the primary separator 1 after passing through the first buffer tank 5 and the first pressurization pump 6. A portion of the purified mixture is collected and enters the middle of the purification zone E of the refining tower 8. The liquid at the bottom of the heavy component removal zone C of the primary separator 1 is partially vaporized by heat exchange between the cold side and the hot side of the primary reboiler 3 and returns to the bottom of the heavy component removal zone C of the primary separator 1. A portion of the heavy component is collected. After the purified mixture enters the middle of the purification zone E of the refining tower 8, a portion of the liquid at the bottom of the purification zone E of the refining tower 8 is collected as product three, and a portion enters the cold side of the first reboiler 9 and the cold side of the second reboiler 10. After being heated and vaporized by the hot side material, it returns to the bottom of the purification zone E of the refining tower 8. The gas at the top of the purification zone D of the refining tower 8 is pressurized by the second compressor 14 and then enters the second reboiler 10. The materials on the hot side and the hot side of the third reboiler 11 of the refining process exchange heat with the materials on the cold side of the second reboiler 10 and the cold side of the third reboiler 11 of the refining process, respectively. After liquefaction, the liquid then passes through the second buffer tank 12 and the second pressurizing pump 13, and part of it enters the top of the refining D zone of the refining tower 8, where product one is partially collected. The liquid at the bottom of the refining F zone of the refining tower 8 enters the cold side of the third reboiler 11 of the refining process, exchanges heat with the materials on the hot side of the third reboiler 11 of the refining process, and then returns to the bottom of the refining F zone of the refining tower 8, where product two is partially collected.

[0053] In this embodiment, the raw material is crude phenol from tar, with a processing capacity of 10,000 tons / year. The mass content of the raw material components is as follows: water 3.31%, light phenols 0.23%, phenol 35.47%, o-cresol 12.5%, p-cresol 12.53%, m-cresol 23.09%, o-ethylphenol 0.69%, 2,4-xylenol 5.47%, and slag phenol 6.71%. After processing by the product refining and energy-saving device described in this utility model, the stable output products are: product one, phenol with a mass concentration of 99.93%; product two, o-cresol with a mass concentration of 99.5%; and product three, m-p-cresol with a mass concentration of 98%. The light components are water and light phenols, and the heavy components are slag phenol.

[0054] In this embodiment, the number of trays in the light-weight removal zone A of the primary separation tower is 30; the number of trays in the purification zone B of the primary separation tower is 45; the number of trays in the heavy-weight removal zone C of the primary separation tower is 18; the number of trays in the purification zone D of the refining tower is 42; the number of trays in the purification zone E of the refining tower is 55; and the number of trays in the purification zone F of the refining tower is 45.

[0055] In this embodiment, the operating pressure of the light removal zone A in the primary separation tower is 15 kPa, the operating pressure of the purification zone B in the primary separation tower is 10 kPa, and the operating pressure of the purification zone D in the refining tower is 10 kPa.

[0056] In this embodiment, the compression ratio of the first compressor is 2.75; the compression ratio of the second compressor is 3.3.

[0057] In this embodiment, the gas at the top of the heavy removal zone C of the primary separation tower is distributed to the light removal zone A and the purification zone B via the gas distribution device 17 at a ratio of 0.47; the liquid at the bottom of the purification zone D of the purification tower is distributed to the purification zone E and the purification zone F via the liquid distribution device 18 at a ratio of 0.36.

[0058] In this embodiment, the liquid at the top of the C region of the primary separation tower is extracted and enters the cold side of the primary separation heat exchanger to exchange heat with the gas on the hot side of the primary separation heat exchanger.

[0059] In this embodiment, the heat transfer medium can be steam, heat transfer oil, or electric heating, with heat transfer oil being preferred.

[0060] In this embodiment, the operating temperature of the light component removal A zone at the top of the primary separation column is 60.3℃, the operating temperature of the purification B zone at the top of the primary separation column is 122.6℃, and the operating temperature of the heavy component removal C zone at the bottom of the primary separation column is 191.1℃; the operating temperature of the purification D zone at the top of the refining column is 113.9℃, the operating temperature of the purification E zone at the bottom of the refining column is 133.9℃, and the operating temperature of the purification F zone at the bottom of the refining column is 122.2℃.

[0061] In this embodiment, the waste heat is fully utilized by the compressor. The first compressor 7 pressurizes the secondary steam in the purification zone B at the top of the primary separator 1 to increase its grade. The outlet temperature of the first compressor is 149.1°C. The steam enters the hot side of the first reboiler 9 and the hot side of the primary separator heat exchanger 4, heating and vaporizing the material in the cold side of the first reboiler 9 and the cold side of the primary separator heat exchanger 4. At the same time, the material itself is condensed. This not only saves the heat transfer medium required for the hot side of the first reboiler 9 and the hot side of the primary separator heat exchanger 4, but also saves the refrigerant required for the condensation of the secondary steam in the purification zone B at the top of the primary separator 1. The second compressor 14 pressurizes and improves the grade of the secondary steam in the top refining zone D of the refining tower 8. The outlet temperature of the second compressor is 145.4℃. The steam enters the hot side of the second reboiler 10 and the hot side of the third reboiler 11, heating and vaporizing the material on the cold side of both refining zones. Simultaneously, the compressor itself condenses, saving the heat transfer medium required for the hot sides of the second and third reboilers and the refrigerant required for the secondary steam condensation in the top refining zone D of the refining tower 8. The entire unit only requires heat transfer medium for the hot side of the initial reboiler 3, and refrigerant for the initial second condenser 21, the first buffer tank 5, and the second buffer tank 12. Compared with existing technology, the production of each ton of phenol can save 205.8 tons of heat transfer oil, which is 83.4% less, and 239.2 tons of refrigerant circulating water, which is 89.5% less. The power consumption of the compressor required to produce each ton of phenol is 129.9 kWh, resulting in a significant reduction in overall energy consumption.

[0062] Similar to Example 1, in this example, the ratio of the top gas from the heavy component removal zone C of the primary separation tower to the light component removal zone A and the purification zone B is adjusted, so that the primary separation tower can simultaneously remove both light and heavy components; the ratio of the bottom liquid from the purification zone D of the purification tower to the purification zones E and F is adjusted, so that the purification tower can simultaneously purify products one, two, and three. Compared with the prior art, this device saves two towers, reduces equipment investment, and also lowers energy consumption.

[0063] The preferred embodiments of this utility model have been described in detail above. However, the content described is only a preferred embodiment of this utility model and should not be considered as limiting the scope of implementation of this utility model. All equivalent changes and improvements made within the scope of the claims of this utility model should still fall within the scope of this utility model patent.

Claims

1. A product refining and energy-saving device, characterized in that: It includes a primary separation tower, a primary separation condenser, a primary separation reboiler, a primary separation heat exchanger, a first buffer tank, a first pressurizing pump, a first compressor, a refining tower, a first refining reboiler, a second refining reboiler, a third refining reboiler, a second buffer tank, a second pressurizing pump, and a second compressor. The primary separation tower includes three zones: light component removal (A), purification (B), and heavy component removal (C), while the refining tower includes three zones: refining (D), refining (E), and refining (F). Material pipelines are connected to the following locations: between the cold side of the primary condenser and the middle of the light-light removal A area of ​​the primary separation tower; between the hot side of the primary condenser and the top of the light-light removal A area of ​​the primary separation tower; between the cold side of the primary reboiler and the bottom of the heavy removal C area of ​​the primary separation tower; between the cold side of the primary heat exchanger and the heavy removal C area of ​​the primary separation tower; between the top of the purification B area of ​​the primary separation tower, the first compressor, the hot side of the first reboiler, the hot side of the primary heat exchanger, the first buffer tank, the first pressurizing pump, and the middle of the purification E area of ​​the purification tower; between the top of the purification D area of ​​the purification tower, the second compressor, the hot side of the second reboiler, the hot side of the third reboiler, the second buffer tank, and the second pressurizing pump; between the bottom of the purification E area of ​​the purification tower, the cold side of the first reboiler, and the cold side of the second reboiler; and between the bottom of the purification F area of ​​the purification tower and the cold side of the third reboiler. These locations form a product purification energy-saving device.

2. The product refining and energy-saving device as described in claim 1, characterized in that: The primary separator is equipped with a partition plate in the upper middle part of the column, which divides the column into three areas: light component removal A, purification B, and heavy component removal C. The light component removal A area has a feed inlet in the middle, and the heavy component removal C area has a liquid outlet and a gas return outlet.

3. The product refining and energy-saving device as described in claim 1, characterized in that: The lower part of the refining tower is equipped with a partition plate, which divides the refining tower into three areas: refining D, refining E, and refining F. The feed inlet is located in the middle of the refining E area.

4. The product refining and energy-saving device as described in claim 1, characterized in that: The primary separation tower and the refining tower are equipped with mass transfer packing and tower internals or tower plates.

5. The product refining and energy-saving device as described in claim 1, characterized in that: A gas distribution device is installed at the top of the C-zone of the primary separation tower for removing heavy materials.

6. The product refining and energy-saving device as described in claim 1, characterized in that: A liquid distribution device is installed at the bottom of the refining D zone of the refining tower.

7. The product refining and energy-saving device as described in claim 1, characterized in that: The first and second buffer tanks are equipped with heat exchange tubes, which are connected to refrigerant.

8. The product refining and energy-saving device as described in claim 1, characterized in that: The primary condenser consists of one or more components.

9. The product refining and energy-saving device as described in claim 1, characterized in that: The primary heat exchanger is connected to the deweighting C region of the primary separation column.

10. The product refining and energy-saving device as described in claim 1, characterized in that: A distribution device with liquid collection function is installed at the location where the primary separation tower is connected to the primary separation heat exchanger.

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