CN108997077B - Composite solvent and method for extracting, rectifying and separating aromatic hydrocarbon from hydrocarbon mixture - Google Patents

Composite solvent and method for extracting, rectifying and separating aromatic hydrocarbon from hydrocarbon mixture Download PDF

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CN108997077B
CN108997077B CN201710420938.2A CN201710420938A CN108997077B CN 108997077 B CN108997077 B CN 108997077B CN 201710420938 A CN201710420938 A CN 201710420938A CN 108997077 B CN108997077 B CN 108997077B
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高思亮
田龙胜
唐文成
赵明
杨楠
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Sinopec Research Institute of Petroleum Processing
China Petroleum and Chemical Corp
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China Petroleum and Chemical Corp
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    • C07C7/04Purification; Separation; Use of additives by distillation
    • C07C7/05Purification; Separation; Use of additives by distillation with the aid of auxiliary compounds
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Abstract

A composite solvent for extracting, rectifying and separating aromatic hydrocarbon from hydrocarbon mixture comprises 40-80 mass% of sulfolane and 20-60 mass% of cosolvent, wherein the cosolvent is a sulfone derivative with a structure shown in a formula (I),
Figure DDA0001314907640000011
in the formula (I), R1And R2Are respectively selected from C1~C4Alkyl, cycloalkyl or aryl. The composite solvent has stable property, no corrosion, higher selectivity to aromatic hydrocarbon, easy regulation and control in the using process and capability of reducing material consumption and energy consumption of the extraction and rectification operation.

Description

Composite solvent and method for extracting, rectifying and separating aromatic hydrocarbon from hydrocarbon mixture
Technical Field
The invention relates to a composite solvent for separating aromatic hydrocarbon from petroleum fluid, in particular to a composite solvent for separating high-purity aromatic hydrocarbon from petroleum hydrocarbon raw materials by using extractive distillation and an application method thereof.
Background
There are two main processes for separating aromatic hydrocarbon from hydrocarbon mixture such as catalytically reformed gasoline and hydrocracked gasoline. One is liquid-liquid extraction, which is essentially a combined process of liquid-liquid extraction and extractive distillation and is suitable for separating aromatic hydrocarbon from wide-cut raw materials, and the used solvents are glycol solvents, sulfolane and the like. The liquid-liquid extraction process can obtain high-purity benzene, toluene and xylene (BTX) products with high yield, but the content of aromatic hydrocarbon in the raw materials cannot be too high, otherwise, an extraction tower is not easy to operate. Another type is the Extractive Distillation (ED) process, which is a process that takes advantage of the differences in the effect of solvent on the relative volatility of the hydrocarbon components to separate aromatics from the feedstock. In contrast, the extractive distillation process has low energy consumption and simple flow, is more suitable for processing raw materials with high aromatic hydrocarbon content and narrow fraction, uses solvents such as glycerol, sulfolane, N-methylpyrrolidone, N-formylmorpholine and the like, and obtains products such as benzene or benzene and toluene.
The reason why the ED technology cannot be used for separating and purifying benzene, toluene and xylene is that the selectivity and the solubility of the currently used solvent are difficult to be compatible. Pyrolysis hydrogenated gasoline C6-C8In the fraction, the aromatic hydrocarbon having the lowest boiling point was benzene (80.1 ℃ C.), and the cycloalkane having the highest boiling point was ethylcyclohexane (131.8 ℃ C.). In the ED column, benzene is present in the rich solvent in the bottom of the column, while the ethyl cyclohexane is distilled to the top of the column, so that the interaction between the solvent and the benzene is strong, and the non-aromatic substances such as the ethyl cyclohexane are relatively excluded. Solvents with high selectivity tend to be less soluble in non-aromatics and tend to phase separate in the upper portion of the column, especially between the solvent feed location and the feedstock feed location, thereby making the ED column difficult to operate.
The addition of at least one co-solvent to the high selectivity solvent makes it possible to increase the selectivity of the solvent and to increase the overall efficiency of the main solvent.
CN1430660A discloses a method for purifying aromatic hydrocarbons from petroleum liquid, which uses sulfolane as main solvent, and cosolvent is selected from one of 3-methyl sulfolane, N-methyl-2 pyrrolidone (NMP), acetophenone, isophorone and morpholine, and the composite solvent is used in a system for separating benzene/N-heptane, so as to obtain an effect superior to pure sulfolane.
CN104058916A discloses a morpholine mixed solvent for separating aromatic hydrocarbon by extractive distillation and a use method thereof, wherein the mixed solvent is N-formyl morpholine and N-acetyl morpholine, and the separation object is N-formyl morpholine and N-acetyl morpholinePetroleum benzene C6-C8And (5) distilling to obtain an aromatic hydrocarbon product which still contains a solvent with the concentration of more than 1mg/L, and in practical application, denitrification treatment is still needed subsequently.
CN1272408C discloses a composite solvent for separating aromatic hydrocarbon by extractive distillation, wherein the main solvent is sulfone compound, glycol compound, N-formyl morpholine or N-methyl pyrrolidone; the cosolvent is a hydrocarbon compound with two benzene rings. The composite solvent is used for separating and reforming the depentanized oil C6-C7The high-purity benzene/toluene mixed aromatic hydrocarbon product can be obtained in high yield by distillation.
Disclosure of Invention
The invention aims to provide a composite solvent and a method for extracting, rectifying and separating aromatic hydrocarbon from a hydrocarbon mixture.
The composite solvent for extracting and rectifying the aromatic hydrocarbon from the hydrocarbon mixture comprises 40-80 mass percent of sulfolane and 20-60 mass percent of cosolvent, wherein the cosolvent is a sulfone derivative with a structure shown in a formula (I),
Figure BDA0001314907620000021
in the formula (I), R1And R2Are respectively selected from C1~C4Alkyl, cycloalkyl or aryl.
According to the method, a proper amount of sulfone derivatives with two substituents shown in the formula (I) is added into a sulfolane solvent to serve as a cosolvent, so that when aromatic hydrocarbon in a raw material containing cycloalkane is separated by extraction and rectification, the solvent ratio can be effectively reduced, the energy consumption is saved, the separated product does not contain nitrogen, the sulfur content is less than 1mg/L, and subsequent refining treatment is not needed.
Drawings
FIG. 1 is a schematic flow chart of the extractive distillation using a composite solvent according to the present invention.
Detailed Description
The composite solvent provided by the invention comprises a main solvent sulfolane and a cosolvent, namely sulfone derivatives with two substituents, wherein the main solvent determines the main properties of the composite solvent, and the cosolvent and the main solvent act synergistically to improve the selectivity of the solvent to aromatic hydrocarbons, increase the solubility of the solvent to non-aromatic hydrocarbons and improve the gas-liquid mass transfer performance. The composite solvent has the advantages of high boiling point, stable property and good solubility to raw materials, and on the basis of ensuring high selectivity, the overall efficiency of extraction and rectification is better than that of a single solvent, so that the quality of aromatic hydrocarbon obtained by separation can be improved, and the yield of the aromatic hydrocarbon is increased.
The composite solvent of the present invention preferably comprises 45 to 78 mass% of sulfolane and 22 to 55 mass% of a co-solvent.
The cosolvent is a sulfone derivative with two substituents shown in formula (I), wherein the substituent R is1And R2Can be the same or different and are respectively selected from C1~C4Alkyl, cycloalkyl or aryl. Said cycloalkyl is preferably C4~C6The aryl group is preferably phenyl.
Preferably, R in the cosolvent1And R2In a different sense, R1And R2Are respectively selected from C1~C4Alkyl of (a), said C1~C4The alkyl group of (a) may be methyl, ethyl, propyl, isopropyl, butyl, isobutyl.
R in the cosolvent1And R2In a different case R may also be1Is selected from C1~C4Alkyl of R2Selected from cyclohexane or phenyl.
The cosolvent of the invention can be: methyl ethyl sulfone, methyl isopropyl sulfone, ethyl isopropyl sulfone, methyl cyclopentyl sulfone, methyl phenyl sulfone, ethyl phenyl sulfone, diphenyl sulfone.
The invention provides a method for separating aromatic hydrocarbon from a hydrocarbon mixture by extractive distillation, which comprises the steps of introducing the hydrocarbon mixture into the middle part of an extractive distillation tower, introducing a composite solvent into the upper part of the extractive distillation tower, carrying out extractive distillation, discharging non-aromatic hydrocarbon from the top of the tower, returning one part of the composite solvent back to the extractive distillation tower as the reflux of the top of the tower, discharging the other part of the composite solvent out of a system, discharging a rich solvent rich in the aromatic hydrocarbon from the bottom of the extractive distillation tower into the middle part of a solvent recovery tower, discharging the aromatic hydrocarbon from the top of the tower, and returning a poor solvent to the extractive distillation tower for recycling after discharging the poor solvent from the bottom of the tower.
In the method, the mass ratio of the composite solvent entering the extractive distillation column to the hydrocarbon mixture raw material, namely the solvent ratio, is preferably 1-20, more preferably 3-10, the theoretical plate number of the extractive distillation column is 30-80, the reflux ratio is 0.2-5, the temperature of the composite solvent entering the column is preferably 70-90 ℃, the temperature of the bottom of the column is preferably 120-150 ℃, and the pressure of the top of the column is preferably 0.1-0.3 MPa.
The theoretical plate number of the solvent recovery column is preferably 5 to 30, the reflux ratio is preferably 0.5 to 2.0, the overhead pressure is preferably 0.01 to 0.05MPa, and the bottom temperature is preferably 155-190 ℃.
The hydrocarbon mixture of the invention is pyrolysis hydrogenated gasoline C6-C8Distillate, condensate, reformate C6-C8Distillate or coal tar C6The aromatic hydrocarbon content of the fraction is preferably 20 to 88 mass%.
The composite solvent and the extractive distillation method provided by the invention are particularly suitable for hydrogenation of gasoline C from cracking6-C8Separating and recovering benzene, toluene and xylene from the fraction.
In the present invention, the selectivity of the solvent for the two components to be separated is characterized by the relative volatility (α), which is defined as:
α=(Y2/X2)/(Y1/X1) (1)
in the formula (1), X1And X2Respectively represents the mass fractions of component 1 and component 2 in the liquid phase, Y1And Y2Respectively, the mass fractions of component 1 and component 2 in the gas phase. The larger the alpha value is, the easier the extractive distillation process is, and the product with higher purity can be obtained by using less distillation steps and less reflux quantity.
The invention is further described below with reference to the accompanying drawings.
In fig. 1, the hydrocarbon mixture enters a heat exchanger 101 through a pipeline 1, enters the middle part of an extractive distillation column 102 after exchanging heat with the lean solvent, and the composite solvent enters the extractive distillation column 102 from the upper part through a pipeline 2. The two are in countercurrent contact for extractive distillation, the non-aromatic hydrocarbon is discharged from the top of the extractive distillation tower, enters a condenser 103 for condensation, a part of the non-aromatic hydrocarbon flows back to the extractive distillation tower 102 through a pipeline 4, and the rest of the non-aromatic hydrocarbon is discharged from the device through a pipeline 3 as a non-aromatic product. The rich solvent rich in aromatic hydrocarbon is discharged from the bottom of the extractive distillation tower, enters the solvent recovery tower 104 through a pipeline 5, is subjected to reduced pressure distillation, is discharged from the top of the tower, enters a condenser 105 for condensation, returns a part of the aromatic hydrocarbon to the solvent recovery tower 104 through a pipeline 6, and is extracted as an aromatic hydrocarbon product through a pipeline 7. The lean solvent is discharged from the bottom of the solvent recovery tower, a small part of the lean solvent is sent to a regeneration device through a pipeline 8, and the rest of the lean solvent is returned to the extractive distillation tower 102 for recycling through a pipeline 9. The heating source at the bottom of the extraction rectifying tower and the solvent recovery tower is a reboiler, namely, one part of the effluent at the bottom of the tower is heated by the reboiler to reach the required temperature and then is sent to the bottom of the tower.
The invention is further illustrated below by way of examples, without being limited thereto.
Example 1
This example examines the separation performance of a complex solvent with methyl ethyl sulfone as a cosolvent on aromatic hydrocarbons/non-aromatic hydrocarbons.
90 mass percent of benzene and 10 mass percent of ethylcyclohexane are mixed as raw materials and added into prepared composite solvents with different contents of methyl ethyl sulfone, and the mass ratio of the composite solvents to the raw materials, namely the solvent ratio, is 3.3.
Shaking the whole mixture, heating to 100 deg.C, standing for 30min, analyzing gas phase composition by gas chromatography, and calculating relative volatility alpha of ethyl cyclohexane to benzene by formula (1), wherein ethyl cyclohexane is component 2, benzene is component 1, and the results are shown in Table 1.
TABLE 1
Figure RE-GDA0002864173740000011
As can be seen from Table 1, the relative volatility of ethylcyclohexane to benzene without solvent is only 0.14, much less than 1, due to the boiling point of ethylcyclohexane being 131.8 ℃ much higher than that of benzene. Pure sulfolane can increase relative volatility to 1.426 at a solvent ratio of 3.3, and the two can be separated by extractive distillation. The relative volatility of the composite solvent containing 10 mass percent of methyl ethyl sulfone is slightly reduced compared with that of sulfolane, but the relative volatility is improved along with the increase of the content of methyl ethyl sulfone in the composite solvent, and can be up to 1.565 percent and is improved by about 10 percent compared with pure sulfolane.
Example 2
This example examines the separation performance of aromatic/non-aromatic hydrocarbons in a complex solvent with methyl isopropyl sulfone as a co-solvent.
The relative volatility of the composite solvent was determined as in example 1, except that the co-solvent in the composite solvent was methyl isopropyl sulfone. The relative volatility α of ethylcyclohexane to benzene for each solvent, calculated from formula (1), is shown in table 2.
TABLE 2
Figure BDA0001314907620000051
As can be seen from table 2, the addition of methyl isopropyl sulfone as a cosolvent to sulfolane is also effective in improving the relative volatility α of ethyl cyclohexane to benzene.
Example 3
This example examines the separation performance of a complex solvent with methyl phenyl sulfone as a cosolvent on aromatic/non-aromatic hydrocarbons.
The relative volatility of the composite solvent was determined as in example 1, except that the co-solvent in the composite solvent was methyl phenyl sulfone. The relative volatility α of ethylcyclohexane to benzene for each solvent, calculated from formula (1), is shown in table 3.
TABLE 3
Figure BDA0001314907620000052
As can be seen from table 3, the addition of methyl phenyl sulfone as a cosolvent to sulfolane can also effectively improve the relative volatility α of ethyl cyclohexane to benzene.
Comparative example 1
This comparative example examines the effect of the disclosed co-solvent on the relative volatility of the benzene/ethylcyclohexane system.
The effect of adding different co-solvents to sulfolane and co-solvent content on relative volatility of ethylcyclohexane/benzene was evaluated at different solvent ratios as in example 1 starting from a mixture of 90 mass% benzene and 10 mass% ethylcyclohexane, the results of which are shown in table 4, where NMP is N-methylpyrrolidone.
TABLE 4
Figure BDA0001314907620000061
From table 4, in the process of separating benzene/ethylcyclohexane system, 3-methyl sulfolane or NMP is added into sulfolane as a cosolvent, and under the condition of the same solvent ratio, the selectivity of the composite solvent is not higher than that of pure sulfolane; and the selectivity of the composite solvent is reduced along with the increase of the adding amount of the cosolvent.
Example 4
By cracking hydrogenated gasoline C6-C8The fraction is a raw material, the composition of which is shown in table 5, alkane and aromatic hydrocarbon are separated by extractive distillation according to the flow chart of fig. 1, the used composite solvent contains 50 mass% of methyl ethyl sulfone and 50 mass% of sulfolane, the operation conditions of the extractive distillation tower and the solvent recovery tower are shown in table 6, and the separation result is shown in table 7.
TABLE 5
Figure BDA0001314907620000071
TABLE 6
Figure BDA0001314907620000072
TABLE 7
Item Example 4 Comparative example 2
Mixed aromatic products
Purity, quality% 99.90 99.65
Yield, mass% 99.9 99.5
Non-aromatic hydrocarbons
Cosolvent content, ppm 25 30
Aromatic hydrocarbon content, mass% 0.7 2.5
Comparative example 2
Using 90 mass% of sulfolane and 10 mass% of sulfolane% of the composite solvent consisting of 3-methyl sulfolane is an extractive distillation solvent, and the method of example 4 is used for extractive distillation separation of pyrolysis hydrogenated gasoline C6-C8The aromatic hydrocarbons and non-aromatic hydrocarbons in the distillate, the operating conditions of the extractive distillation column and the solvent recovery column are shown in Table 6, and the results are shown in Table 7.
The result shows that compared with the composite solvent of the comparative example 2, the composite solvent of the invention has higher purity and yield of the separated mixed aromatic hydrocarbon product under the conditions of smaller solvent and basically same other operating conditions.

Claims (8)

1. A composite solvent for extracting, rectifying and separating aromatic hydrocarbon from hydrocarbon mixture is composed of sulfolane (40-50 wt.%) and cosolvent (50-60 wt.%), which is the sulfone derivative with structure of formula (I),
Figure FDF0000014825260000011
in the formula (I), R1And R2Different, are respectively selected from C1~C4Alkyl of (C)4~C6The hydrocarbon mixture is cracked hydrogenated gasoline C6-C8Distillate, condensate or reformate C6-C8And (6) cutting.
2. The composite solvent according to claim 1, wherein the composite solvent consists of 45 to 50 mass% of sulfolane and 50 to 55 mass% of a co-solvent.
3. The composite solvent according to claim 1 or 2, wherein R in the co-solvent is1And R2Are respectively selected from C1~C4Alkyl group of (1).
4. The composite solvent according to claim 1 or 2, wherein R in the co-solvent is1Is selected from C1~C4The alkyl group of (a) is,R2selected from cyclohexane or phenyl.
5. A process for extracting, rectifying and separating arylhydrocarbon from hydrocarbon mixture includes such steps as introducing the hydrocarbon mixture to the middle of extracting-rectifying tower, introducing the composite solvent as defined in claim 1 to the upper part of extracting-rectifying tower, extracting and rectifying, discharging non-arylhydrocarbon from tower top, returning part of the solvent back to extracting-rectifying tower, discharging the rest part of the solvent back to system, discharging the rich solvent rich in arylhydrocarbon from tower bottom of extracting-rectifying tower to the middle of solvent recovering tower, discharging arylhydrocarbon from tower top, discharging poor solvent from tower bottom, returning the poor solvent back to extracting-rectifying tower for cyclic use, and cracking hydrogenated gasoline C6-C8Distillate, condensate or reformate C6-C8And (6) cutting.
6. The method as claimed in claim 5, wherein the mass ratio of the composite solvent to the hydrocarbon mixture raw material entering the extractive distillation column is 1 to 20, the number of theoretical plates of the extractive distillation column is 30 to 80, the reflux ratio is 0.2 to 5, the temperature of the composite solvent entering the extractive distillation column is 70 to 90 ℃, the temperature of the bottom of the extractive distillation column is 120-.
7. The process as claimed in claim 5, characterized in that the theoretical plate number of the solvent recovery column is from 20 to 50, the reflux ratio is from 0.5 to 2.0, the pressure at the top of the column is from 0.01 to 0.05MPa and the temperature at the bottom of the column is from 155 ℃ to 190 ℃.
8. A process according to claim 5, characterized in that the aromatic content of the hydrocarbon mixture is from 20 to 88 mass%.
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