CN210765173U - Aromatic extraction combination device - Google Patents
Aromatic extraction combination device Download PDFInfo
- Publication number
- CN210765173U CN210765173U CN201921733652.0U CN201921733652U CN210765173U CN 210765173 U CN210765173 U CN 210765173U CN 201921733652 U CN201921733652 U CN 201921733652U CN 210765173 U CN210765173 U CN 210765173U
- Authority
- CN
- China
- Prior art keywords
- tower
- liquid
- extraction
- temperature
- pressure
- 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
Images
Landscapes
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The utility model discloses an aromatic extraction combination device, belonging to the technical field of petrochemical industry, comprising a raw material cutting tower, an extraction distillation tower, a recovery tower, a liquid-liquid extraction tower and a stripping tower; the top of the raw material cutting tower is connected with the middle part of the extraction distillation tower, the bottom of the raw material cutting tower is connected with the middle part of the liquid-liquid extraction tower, and the top of the extraction distillation tower is sequentially connected with an air cooling device, a water cooling device and a water washing device; the bottom of the extraction distillation tower is connected with the middle part of the recovery tower; heavy raffinate oil products are discharged from the top of the liquid-liquid extraction tower, and the bottom of the liquid-liquid extraction tower is connected with the middle part of the stripping tower; the top of the stripping tower is connected with the bottom of the liquid-liquid extraction tower through a pipeline; the bottom of the stripping tower is connected with the middle part of the recovery tower through a pipeline; the bottom of the recovery column is connected to the upper part of the extractive distillation column and/or the upper part of the liquid-liquid extraction column via a pipeline, respectively. The utility model discloses an aromatics extraction composite set low cost, low energy consumption, process flow are short, pollution-free, product quality is high.
Description
Technical Field
The utility model relates to an aromatic extraction composite set belongs to petrochemical technical field.
Background
Aromatic hydrocarbons are important basic raw materials for petrochemical industry, and the aromatic hydrocarbons contain various components, the most important of which are benzene, toluene and xylene.
With the development of the oil refining industry and the increase in the demand for aromatics, petroleum aromatics have become the major source of aromatics. In addition, as environmental requirements become more stringent, the standards for petroleum products (fuels) also become more stringent. Taking gasoline as an example, new gasoline standards have been successively implemented in recent years in the united states, europe, japan, and the like. The content of benzene is less than 1.0 percent (V) and the total content of aromatic hydrocarbon is not more than 40 percent (V) which are definitely specified in the current gasoline standard in China. In this case, the separation of aromatic hydrocarbons is particularly important, and benzene, toluene and xylene are important chemical raw materials.
The existing aromatic extraction method has the disadvantages of high energy consumption, long process flow and large occupied area, thereby leading to higher investment cost and operation cost.
Therefore, the technical problem which needs to be solved urgently in the technical field is to provide the aromatic hydrocarbon extraction combination device and the process which have the advantages of low cost, low energy consumption, short process flow, no pollution and high product quality.
SUMMERY OF THE UTILITY MODEL
One of the purposes of the utility model is to provide an aromatic extraction combination device with low cost, low energy consumption, short process flow, no pollution and high product quality.
The above object of the utility model is achieved through the following technical scheme:
an aromatics extraction composite set, its characterized in that: comprises a raw material cutting tower, an extraction distillation tower, a recovery tower, a liquid-liquid extraction tower and a stripping tower; the top of the raw material cutting tower is connected with the middle part of the extraction distillation tower, the bottom of the raw material cutting tower is connected with the middle part of the liquid-liquid extraction tower, and the top of the extraction distillation tower is sequentially connected with an air cooling device, a water cooling device and a water washing device; the bottom of the extraction distillation tower is connected with the middle part of the recovery tower; heavy raffinate oil products are discharged from the top of the liquid-liquid extraction tower, and the bottom of the liquid-liquid extraction tower is connected with the middle part of the stripping tower; the top of the stripping tower is connected with the bottom of the liquid-liquid extraction tower through a pipeline; the bottom of the stripping tower is connected with the middle part of the recovery tower through a pipeline; the bottom of the recovery tower is respectively connected with the upper part of the extractive distillation tower, the upper part of the stripping tower and/or the upper part of the liquid-liquid extraction tower through pipelines.
Preferably, the operating pressure of the extractive distillation column is 0.05 to 0.35MPa, and the operating pressure of the liquid-liquid extraction column is 0.30 to 0.90 MPa.
Preferably, the extractive distillation column is a non-liquid contact extraction column, and the liquid-liquid extraction column is a liquid-liquid contact extraction column.
Preferably, the mass ratio of the solvent in the extractive distillation column is 1.2-6.5, and the mass ratio of the solvent in the liquid-liquid extraction column is 1.2-6.5.
Preferably, the operating pressure of the raw material cutting tower is 0.03-0.08MPa, the tower top temperature is 102-121 ℃, the reflux ratio is 2-4, and the tower bottom temperature is 185-198 ℃.
Preferably, the extractive distillation column has a temperature of 88 to 108 deg.C (preferably 98 deg.C), a pressure of 0.05 to 0.15MPa (preferably 0.08MPa), a solvent ratio of 2 to 4 (preferably 3), and sulfolane as the solvent.
Preferably, the recovery column has an overhead temperature of 58 to 78 deg.C (preferably 68 deg.C), a bottom temperature of 155 deg.C and 195 deg.C (preferably 175 deg.C), an overhead pressure of 0.02 to 0.06MPa (preferably 0.04MPa), and a bottom pressure of 0.045 to 0.105MPa (preferably 0.065 MPa).
Preferably, the liquid-liquid extraction column has a temperature of 70 to 110 ℃ (preferably 90 ℃), a pressure of 0.2 to 0.8MPa (preferably 0.5MPa), and a solvent ratio of 2 to 4 (preferably 3).
Preferably, the operating temperature of the stripping column is 110-150 ℃ (preferably 130 ℃), the operating pressure is 0.13-0.53MPa (preferably 0.33MPa), and the backflushing ratio is 0.4-0.5 (preferably 0.44).
The utility model also aims to provide the arene extraction combined process with low cost, low energy consumption, short process flow, no pollution and high product quality.
The above object of the utility model is achieved through the following technical scheme:
an aromatic extraction combined process comprises the following steps:
(1) adding component gasoline and a solvent into a raw material cutting tower, cutting a material flow containing C6-C7 aromatic hydrocarbon components from the top of the raw material cutting tower, extracting in an extractive distillation tower to obtain light raffinate oil at the top of the extractive distillation tower, and discharging the light raffinate oil at the top of the extractive distillation tower out of the device after air cooling, water cooling and water washing;
(2) the bottom of the extraction distillation tower obtains a light rich solvent, the light rich solvent enters a recovery tower, and an aromatic hydrocarbon product is extracted from the top of the recovery tower and directly discharged out of the device; the solvent extracted from the bottom of the recovery tower flows back to the upper part of the liquid-liquid extraction tower and/or the upper part of the stripping tower and/or the upper part of the extractive distillation tower;
(3) cutting a material flow containing C8-C9 aromatic hydrocarbon components from the bottom of the raw material cutting tower, entering a liquid-liquid extraction tower for liquid-liquid extraction, and extracting heavy raffinate oil from the top of the liquid-liquid extraction tower;
(4) heavy rich solvent rich in heavy aromatic hydrocarbon and solvent is extracted from the bottom of the liquid-liquid extraction tower and enters a stripping tower, and backwash liquid is extracted from the top of the stripping tower and flows back to the liquid-liquid extraction tower.
Preferably, the operation pressure of the raw material cutting tower in the step (1) is 0.03-0.08MPa, the tower top temperature is 102-121 ℃, the reflux ratio is 2-4, and the tower bottom temperature is 185-198 ℃.
Preferably, the extractive distillation column in step (1) is operated at a pressure of 0.05 to 0.35MPa, and the liquid-liquid extraction column is operated at a pressure of 0.30 to 0.90 MPa.
Preferably, the extractive distillation column in the step (1) is a non-liquid contact extraction column, and the liquid-liquid extraction column is a liquid-liquid contact extraction column.
Preferably, the mass ratio of the solvent in the extractive distillation column in the step (1) is 1.2 to 6.5, and the mass ratio of the solvent in the liquid-liquid extraction column is 1.2 to 6.5.
Preferably, the extractive distillation column in step (1) has a temperature of 88 to 108 ℃ (preferably 98 ℃), a pressure of 0.05 to 0.15MPa (preferably 0.08MPa), a solvent ratio of 2 to 4 (preferably 3), and the solvent used is sulfolane.
Preferably, the temperature of the top of the recovery column in step (2) is 58 to 78 ℃ (preferably 68 ℃), the temperature of the bottom of the recovery column is 155 ℃ to 195 ℃ (preferably 175 ℃), the pressure of the top of the recovery column is 0.02 to 0.06MPa (preferably 0.04MPa), and the pressure of the bottom of the recovery column is 0.045 to 0.105MPa (preferably 0.065 MPa).
Preferably, the temperature of the liquid-liquid extraction column in steps (2) and (3) is 70 to 110 ℃ (preferably 90 ℃), the pressure is 0.2 to 0.8MPa (preferably 0.5MPa), and the solvent ratio is 2 to 4 (preferably 3).
Preferably, the operation temperature of the stripping column in the step (4) is 110-150 ℃ (preferably 130 ℃), the operation pressure is 0.13-0.53MPa (preferably 0.33MPa), and the back-washing ratio is 0.4-0.5 (preferably 0.44).
Preferably, the light raffinate oil in step (1) has an aromatics content of 0.3% and a solvent content of 2 ppm.
Preferably, the solvent extracted from the bottom of the recovery tower in the step (2) is mixed in a ratio of 1: 4 into the bottom of the liquid-liquid extraction column and the bottom of the extractive distillation column, respectively.
Preferably, the heavy raffinate in step (3) has an aromatics content of 0.5% and a solvent content of 2 ppm.
Preferably, the backwash liquid is taken from the top of the stripping column in step (4) in a ratio of 1: 4, feeding the mixture into the feeding and the bottom of the liquid-liquid extraction tower respectively as backwashing; or all of the liquid is fed to the bottom of the liquid-liquid extraction column.
Has the advantages that:
compared with the conventional aromatic extraction, the utility model adopts different extraction modes for light and heavy components, adopts an extraction distillation mode for light components, and sends the light aromatic into a downstream fractionation system after extraction to fractionate high-purity light aromatic products; the liquid-liquid extraction mode is adopted for heavy components, the energy consumption is reduced to the maximum extent, the extracted heavy aromatic hydrocarbon is directly sent into a heavy aromatic hydrocarbon fractionation system, and a high-purity heavy aromatic hydrocarbon product is fractionated; the light distillate oil extraction and the heavy distillate oil extraction share a recovery tower.
The utility model discloses make up again each component to the oil fluid, require different choices to go different according to the product, synthesize effectual utilization to each component.
The present invention is further illustrated by the following figures and specific embodiments, which are only used to explain the present invention and are not used to limit the protection scope of the present invention.
Drawings
FIG. 1 is a schematic structural diagram of an aromatics extraction unit of example 1 of the present invention.
Names of main parts:
1 raw material cutting tower 2 extraction distillation tower
3 recovery column 4 liquid-liquid extraction column
5 stripping tower
Detailed Description
Example 1
As shown in fig. 1, which is a schematic structural diagram of an aromatics extraction combination unit according to embodiment 1 of the present invention, some auxiliary devices such as a tank, a pump, a heat exchanger, a condenser, etc. are not shown in the figure, but are well known to those skilled in the art; wherein, 1 is a raw material cutting tower, 2 is an extraction distillation tower, 3 is a recovery tower, 4 is a liquid-liquid extraction tower, and 5 is a stripping tower; the utility model discloses arene extraction composite set of embodiment 1 includes a raw material cutting tower 1, an extraction distillation tower 2, a recovery tower 3, a liquid-liquid extraction tower 4 and a stripping tower 5; the top of the raw material cutting tower 1 is connected with the middle part of the extraction distillation tower 2, the bottom of the raw material cutting tower 1 is connected with the middle part of the liquid-liquid extraction tower 4, and the top of the extraction distillation tower 2 is sequentially connected with an air cooling device, a water cooling device and a water washing device (not shown in the figure); the bottom of the extraction distillation tower 2 is connected with the middle part of the recovery tower 3; the product is discharged from the top of the liquid-liquid extraction tower 4, and the bottom of the liquid-liquid extraction tower 4 is connected with the middle part of the stripping tower 5; the top of the stripping tower 5 is connected with the bottom of the liquid-liquid extraction tower 4 through a pipeline; the bottom of the stripping tower 5 is connected with the middle part of the recovery tower 3 through a pipeline; the bottom of the recovery column 3 is connected to the upper part of the extractive distillation column 2 and the upper parts of the liquid-liquid extraction column 4 and the stripping column 5, respectively, via pipes.
The utility model discloses embodiment 1's aromatics extraction composite set's process flow as follows:
C6-C9 component gasoline with aromatic hydrocarbon content of 70.65% (the raw material property is shown in a table 1-1) enters a raw material cutting tower 1 at a flow rate of 100 tons/hour, the operating pressure of the raw material cutting tower 1 is 0.08MPa, the tower top temperature is 121 ℃, the reflux ratio is 2, the tower bottom temperature is 198 ℃, a material flow containing C6-C7 aromatic hydrocarbon components is cut at the top of the raw material cutting tower 1 and enters an extraction distillation tower 2 for extraction distillation, the temperature of the extraction distillation tower 2 is 98 ℃, the pressure is 0.08MPa, the solvent ratio is 3, the used solvent is sulfolane, light raffinate oil is obtained at the top of the extraction distillation tower 2, the aromatic hydrocarbon content of the obtained light raffinate oil is not higher than 0.3 percent, the solvent content is not higher than 2ppm, and the light raffinate oil at the top of the extraction distillation tower 2 is directly discharged out of the device at a flow rate of 20 tons/hour after air cooling, water washing; the bottom of the extraction distillation tower 2 is used for obtaining a light rich solvent, the light rich solvent enters a recovery tower 3 at the flow rate of 171 tons/hour, the top temperature of the recovery tower 3 is 68 ℃, the bottom temperature of the recovery tower is 175 ℃, the top pressure of the recovery tower is 0.04MPa, the bottom pressure of the recovery tower is 0.065MPa, and an aromatic hydrocarbon product extracted from the top of the recovery tower 3 directly exits the device at the flow rate of 71.04 tons/hour; the solvent withdrawn from the bottom of the recovery column 3 was mixed at a flow rate of 300 tons/hr in a ratio of 1: 2: 2 are fed into the bottom of a stripping tower 5 and a liquid-liquid extraction tower 4 and the bottom of an extraction distillation tower 2 respectively; cutting a material flow containing C8-C9 aromatic hydrocarbon components from the bottom of a raw material cutting tower 1, entering a liquid-liquid extraction tower 4 for liquid-liquid extraction, wherein the temperature of the liquid-liquid extraction tower 4 is 90 ℃, the pressure is 0.5MPag, the solvent ratio is 3, heavy raffinate oil is extracted from the top of the liquid-liquid extraction tower 4, the aromatic hydrocarbon content of the obtained heavy raffinate oil is not higher than 0.5%, and the solvent content is not higher than 2 ppm; the heavy raffinate oil is sent out of the device at a flow rate of 22 tons/hour; a heavy rich solvent rich in heavy aromatics and solvent is extracted from the bottom of the liquid-liquid extraction tower 4; the heavy rich solvent obtained from the bottom of the liquid-liquid extraction tower 4 enters the middle part of a stripping tower 5 at a flow rate of 191 tons/hour, and a backwashing liquid of 20 tons/hour is extracted from the top of the stripping tower 5 and is completely sent to the bottom of the liquid-liquid extraction tower 4; the operation temperature of the stripping tower 5 was 130 ℃, the operation pressure was 0.33MPa, and the back-wash ratio was 0.44.
The compositional properties of the resulting light raffinate product are shown in tables 1-2, the compositional properties of the resulting heavy raffinate product are shown in tables 1-3, and the compositional properties of the resulting aromatic hydrocarbon product are shown in tables 1-4.
TABLE 1-1 Properties of the raw materials
TABLE 1-2 light raffinate product compositional Properties
TABLE 1-3 compositional Properties of heavy raffinate oil products
TABLE 1-4 aromatic product compositional Properties
The composition analysis of the raw material and the product is respectively tested by using SH/T0166-92 or GB/T11132-2008 methods, and the determination standard of the sulfolane content is UOP 660.
Example 2
The utility model discloses arene extraction composite set's of embodiment 2 process flow as follows:
C6-C9 component gasoline with the aromatic hydrocarbon content of 40.44% (the properties of the raw materials are shown in a table 2-1) enters a raw material cutting tower 1 at the flow rate of 100 tons/hour, the operating pressure of the raw material cutting tower 1 is 0.03MPa, the tower top temperature is 102 ℃, the reflux ratio is 4, and the tower bottom temperature is 185 ℃; cutting a material flow containing C6-C7 aromatic hydrocarbon components from the top of a raw material cutting tower 1, extracting in an extraction distillation tower 2, wherein the temperature of the extraction distillation tower 2 is 98 ℃, the pressure is 0.05MPa, the solvent ratio is 1.2, the used solvent is sulfolane, light raffinate oil is obtained from the top of the extraction distillation tower 2, the aromatic hydrocarbon content of the obtained light raffinate oil is not higher than 0.3 percent, the solvent content is not higher than 2ppm, and the light raffinate oil at the top of the extraction distillation tower 2 is directly discharged out of the device at a flow rate of 20 tons/hour after air cooling, water cooling and water washing; the bottom of the extraction distillation tower 2 is used for obtaining a light rich solvent, the light rich solvent enters a recovery tower 3 at a flow rate of 65 tons/hour, the top temperature of the recovery tower 3 is 68 ℃, the bottom temperature of the recovery tower is 175 ℃, the top pressure of the recovery tower is 0.04MPa, the bottom pressure of the recovery tower is 0.065MPa, and 39.94 tons/hour of aromatic hydrocarbon products are extracted from the top of the recovery tower 3 and directly discharged out of the device; the solvent withdrawn from the bottom of the recovery column 3 was mixed at a flow rate of 120 tons/hr in a ratio of 1: 4 respectively enter the bottom of the liquid-liquid extraction tower 4 and the bottom of the extraction distillation tower 2; cutting a material flow containing C8-C9 aromatic hydrocarbon components from the bottom of a raw material cutting tower 1, entering a liquid-liquid extraction tower 4 for liquid-liquid extraction, wherein the temperature of the liquid-liquid extraction tower 4 is 90 ℃, the pressure is 0.9MPa, the solvent ratio is 5, heavy raffinate oil is extracted from the top of the liquid-liquid extraction tower 4, the aromatic hydrocarbon content of the obtained heavy raffinate oil is not higher than 0.5%, and the solvent content is not higher than 2 ppm; delivering the product at a flow rate of 31 tons/hour; a heavy rich solvent rich in heavy aromatics and solvent is extracted from the bottom of the liquid-liquid extraction tower 4; the heavy rich solvent obtained from the bottom of the liquid-liquid extraction column 4 enters the stripping column 5 at a flow rate of 140.4 tons/hour, and a backwash liquid of 26.4 tons/hour is withdrawn from the top of the stripping column 5, and the ratio of the flow rate of the heavy rich solvent to the flow rate of the backwash liquid is 1: 4, feeding the mixture into the feeding and the bottom of the liquid-liquid extraction tower 4 in proportion respectively to be used as backwashing; the operation temperature of the stripping tower 5 was 130 ℃, the operation pressure was 0.33MPa, and the back-wash ratio was 0.44.
The compositional properties of the resulting light raffinate product are shown in tables 2-2, the compositional properties of the resulting heavy raffinate product are shown in tables 2-3, and the compositional properties of the resulting aromatic hydrocarbon product are shown in tables 2-4.
TABLE 2-1 Properties of the starting materials
TABLE 2-2 light raffinate oil product compositional Properties
TABLE 2-3 compositional Properties of heavy raffinate oil products
TABLE 2-4 aromatic product compositional Properties
The composition analysis of the raw material and the product is respectively tested by using SH/T0166-92 or GB/T11132-2008 methods, and the determination standard of the sulfolane content is UOP 660.
Example 3
The utility model discloses arene extraction composite set's of embodiment 3 process flow as follows:
C6-C9 component gasoline with the aromatic hydrocarbon content of 90.12 percent (the raw material property is shown in a table 3-1) enters a raw material cutting tower 1 at the flow rate of 100 tons/hour, the operating pressure of the raw material cutting tower 1 is 0.08MPa, the top temperature of the tower is 121 ℃, the reflux ratio is 4, the bottom temperature of the tower is 198 ℃, a material flow containing C6-C7 aromatic hydrocarbon components is cut at the top of the raw material cutting tower 1 and enters an extraction distillation tower 2 for extraction, the temperature of the extraction distillation tower 2 is 98 ℃, the pressure is 0.05MPa, the solvent ratio is 6.5, the used solvent is sulfolane, light raffinate oil is obtained at the top of the extraction distillation tower 2, the aromatic hydrocarbon content of the obtained light raffinate oil is not higher than 0.3 percent, the solvent content is not higher than 2ppm, and the light raffinate oil at the top of the extraction distillation tower 2 is directly discharged out of the device at the flow rate of 5 tons/hour after air cooling, water washing; extracting the bottom of the distillation tower 2 to obtain a light rich solvent, wherein the light rich solvent enters a recovery tower 3 at a flow rate of 266 tons/hour, the top temperature of the recovery tower 3 is 71 ℃, the bottom temperature of the recovery tower is 175 ℃, the top pressure of the recovery tower is 0.04MPa, the bottom pressure of the recovery tower is 0.065MPa, and 89.91 tons/hour of aromatic hydrocarbon products are extracted from the top of the recovery tower 3 and directly discharged out of the device; the solvent withdrawn from the bottom of the recovery column 3 was mixed at a flow rate of 650 tons/hr in a ratio of 2: 3 are respectively fed into the bottom of the liquid-liquid extraction tower 4 and the bottom of the extractive distillation tower 2; cutting a material flow containing C8-C9 aromatic hydrocarbon components from the bottom of a raw material cutting tower 1, entering a liquid-liquid extraction tower 4 for liquid-liquid extraction, wherein the temperature of the liquid-liquid extraction tower 4 is 90 ℃, the pressure is 0.9MPa, the solvent ratio is 6.5, heavy raffinate oil is extracted from the top of the liquid-liquid extraction tower 4, the aromatic hydrocarbon content of the obtained heavy raffinate oil is not higher than 0.5%, and the solvent content is not higher than 2 ppm; the device was fed at a flow rate of 4.8 tons/hour; a heavy rich solvent rich in heavy aromatics and solvent is extracted from the bottom of the liquid-liquid extraction tower 4; the heavy rich solvent obtained from the bottom of the liquid-liquid extraction column 4 enters the stripping column 5 at a flow rate of 414 tons/hour, and the back washing liquid of 18 tons/hour is extracted from the top of the stripping column 5, and the ratio of the back washing liquid to the heavy rich solvent is calculated according to the following formula 1: 4, feeding the mixture into the feeding and the bottom of the liquid-liquid extraction tower 4 in proportion respectively to be used as backwashing; the operation temperature of the stripping tower 5 is 130 ℃, the operation pressure is 0.33MPa, and the back washing ratio is 0.3.
The compositional properties of the resulting light raffinate product are shown in Table 3-2, the compositional properties of the resulting heavy raffinate product are shown in Table 3-3, and the compositional properties of the resulting aromatic hydrocarbon product are shown in Table 3-4.
TABLE 3-1 Properties of the raw materials
TABLE 3-2 light raffinate product compositional Properties
TABLE 3-3 compositional Properties of heavy raffinate oil products
TABLE 3-4 aromatic product compositional Properties
The composition analysis of the raw material and the product is respectively tested by using SH/T0166-92 or GB/T11132-2008 methods, and the determination standard of the sulfolane content is UOP 660.
Claims (10)
1. An aromatics extraction composite set, its characterized in that: comprises a raw material cutting tower, an extraction distillation tower, a recovery tower, a liquid-liquid extraction tower and a stripping tower; the top of the raw material cutting tower is connected with the middle part of the extraction distillation tower, the bottom of the raw material cutting tower is connected with the middle part of the liquid-liquid extraction tower, and the top of the extraction distillation tower is sequentially connected with an air cooling device, a water cooling device and a water washing device; the bottom of the extraction distillation tower is connected with the middle part of the recovery tower; heavy raffinate oil products are discharged from the top of the liquid-liquid extraction tower, and the bottom of the liquid-liquid extraction tower is connected with the middle part of the stripping tower; the top of the stripping tower is connected with the bottom of the liquid-liquid extraction tower through a pipeline; the bottom of the stripping tower is connected with the middle part of the recovery tower through a pipeline; the bottom of the recovery tower is respectively connected with the upper part of the extractive distillation tower, the upper part of the stripping tower and/or the upper part of the liquid-liquid extraction tower through pipelines.
2. The aromatics extraction complex of claim 1, characterized in that: the operating pressure of the extraction distillation tower is 0.05MPa-0.35 MPa.
3. The aromatics extraction complex of claim 2, characterized in that: the operating pressure of the liquid-liquid extraction tower is 0.30MPa to 0.90 MPa.
4. The aromatics extraction complex of claim 3, wherein: the extraction distillation tower is a non-liquid contact extraction tower, and the liquid-liquid extraction tower is a liquid-liquid contact extraction tower.
5. The aromatics extraction complex of claim 4, wherein: the mass ratio of the solvent of the extraction distillation tower is 1.2-6.5, and the mass ratio of the solvent of the liquid-liquid extraction tower is 1.2-6.5.
6. The aromatics extraction complex of claim 5, wherein: the operating pressure of the raw material cutting tower is 0.03MPa-0.08MPa, the tower top temperature is 102-121 ℃, the reflux ratio is 2-4, and the tower bottom temperature is 185-198 ℃.
7. The aromatics extraction complex of claim 6, characterized in that: the temperature of the extraction distillation tower is 88-108 ℃, the pressure is 0.05MPa-0.15MPa, the solvent ratio is 2-4, and the used solvent is sulfolane.
8. The aromatics extraction complex of claim 7, wherein: the tower top temperature of the recovery tower is 58-78 ℃, the tower bottom temperature is 155-195 ℃, the tower top pressure is 0.02-0.06MPa, and the tower bottom pressure is 0.045-0.105 MPa.
9. The aromatics extraction complex of claim 8, wherein: the temperature of the liquid-liquid extraction tower is 70-110 ℃, the pressure is 0.2-0.8MPa, and the solvent ratio is 2-4; the operation temperature of the stripping tower is 110-150 ℃, the operation pressure is 0.13-0.53MPa, and the back washing ratio is 0.4-0.5.
10. The aromatics extraction complex of claim 9, wherein: the operating pressure of the raw material cutting tower is 0.05MPa, the tower top temperature is 116 ℃, the reflux ratio is 3, and the tower bottom temperature is 192 ℃; the temperature of the extraction distillation tower is 98 ℃, the pressure is 0.08MPa, the solvent ratio is 3, and the used solvent is sulfolane; the tower top temperature of the recovery tower is 68 ℃, the tower bottom temperature is 175 ℃, the tower top pressure is 0.04MPa, and the tower bottom pressure is 0.065 MPa; the temperature of the liquid-liquid extraction tower is 90 ℃, the pressure is 0.5MPa, and the solvent ratio is 3; the operation temperature of the stripping tower is 130 ℃, the operation pressure is 0.33MPa, and the back washing ratio is 0.44.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201921733652.0U CN210765173U (en) | 2019-10-15 | 2019-10-15 | Aromatic extraction combination device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201921733652.0U CN210765173U (en) | 2019-10-15 | 2019-10-15 | Aromatic extraction combination device |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN210765173U true CN210765173U (en) | 2020-06-16 |
Family
ID=71066288
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201921733652.0U Active CN210765173U (en) | 2019-10-15 | 2019-10-15 | Aromatic extraction combination device |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN210765173U (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110628459A (en) * | 2019-10-15 | 2019-12-31 | 北京宝晨能源工程技术有限公司 | Aromatic hydrocarbon extraction combined device and process |
-
2019
- 2019-10-15 CN CN201921733652.0U patent/CN210765173U/en active Active
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110628459A (en) * | 2019-10-15 | 2019-12-31 | 北京宝晨能源工程技术有限公司 | Aromatic hydrocarbon extraction combined device and process |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN106588579B (en) | A method of extracting phenolic compound from carbolic oil | |
| EP3747854A1 (en) | Method for separating aromatic hydrocarbon using extractive distillation | |
| CN106478379B (en) | A kind of coal tar oil ingredient continuous separation technology and device | |
| CN106178571B (en) | Azeotrope separation process | |
| CN106278827A (en) | A kind of method and device of extract and separate phenolic compound from coal derived oils | |
| CN103664446A (en) | Technology for separating n-hexane-methylcyclopentane through extractive distillation | |
| CN103215058A (en) | Method for extracting and separating light component from coal tar at low temperature | |
| CN113201364A (en) | Multi-stage countercurrent extraction device and method for catalyzing diesel polycyclic aromatic hydrocarbon by using ionic liquid | |
| CN106753546A (en) | F- T synthesis light fraction oil refining new technology | |
| CN210765173U (en) | Aromatic extraction combination device | |
| CN109646980B (en) | Fusel-free oil dividing wall tower coupled methanol multi-effect rectification energy-saving device and method | |
| CN104557382B (en) | The method of separating-purifying firpene from turps | |
| CN203648128U (en) | Rectification device capable of reducing energy consumption of azeotropic distillation in sec-butyl acetate separating process | |
| CN103194253B (en) | Method for pre-treating coal tar by using mixed solvent | |
| CN110628459A (en) | Aromatic hydrocarbon extraction combined device and process | |
| CN114989856A (en) | Method and device for separating aromatic hydrocarbon or sulfur-containing compound from gasoline fraction | |
| CN104370696A (en) | Novel method for separating ethylene glycol and 1,2-pentanediol | |
| CN103951604A (en) | Method for separation and purification of indole | |
| CN111377801B (en) | Method and system for refining low carbon alcohol | |
| CN108264931A (en) | For producing the separator of refined bitumen tempered oil | |
| CN216236869U (en) | Multi-stage countercurrent extraction device for catalyzing diesel polycyclic aromatic hydrocarbon by using ionic liquid | |
| CN102876359A (en) | System and method for processing condensate oil | |
| CN205549690U (en) | A device for separating sour hydrocarbon mixture | |
| CN212504657U (en) | System for hydrogenation and extractive distillation of crude benzene | |
| CN113789190A (en) | Multi-stage countercurrent-cross-flow combined extraction device and method for catalyzing diesel polycyclic aromatic hydrocarbon by using ionic liquid |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant |