CN112795397B - Composite solvent for separating cyclane and aromatic hydrocarbon from naphtha - Google Patents
Composite solvent for separating cyclane and aromatic hydrocarbon from naphtha Download PDFInfo
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- CN112795397B CN112795397B CN201911111969.5A CN201911111969A CN112795397B CN 112795397 B CN112795397 B CN 112795397B CN 201911111969 A CN201911111969 A CN 201911111969A CN 112795397 B CN112795397 B CN 112795397B
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G29/00—Refining of hydrocarbon oils, in the absence of hydrogen, with other chemicals
- C10G29/20—Organic compounds not containing metal atoms
- C10G29/205—Organic compounds not containing metal atoms by reaction with hydrocarbons added to the hydrocarbon oil
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G53/00—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more refining processes
- C10G53/02—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more refining processes plural serial stages only
- C10G53/04—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more refining processes plural serial stages only including at least one extraction step
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/10—Feedstock materials
- C10G2300/1037—Hydrocarbon fractions
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/10—Feedstock materials
- C10G2300/1037—Hydrocarbon fractions
- C10G2300/1044—Heavy gasoline or naphtha having a boiling range of about 100 - 180 °C
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
- C10G2400/30—Aromatics
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- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
A composite solvent suitable for separating cyclane and arene from naphtha is prepared from N, N-dimethyl formamide, cyclodextrin and 1-butyl-3-methylimidazole dicyanamide salt through mixing, and mixing in the ratio of N, N-dimethyl formamide to cyclodextrin to 1-butyl-3-methylimidazole dicyanamide salt = 80-90 to 10-20 to 1. Compared with sulfolane, the compound solvent has the selectivity of 3.2 to the cycloparaffin, and the removal rate of the cycloparaffin can reach more than 62 percent; the selectivity of the compound solvent to aromatic hydrocarbon can reach 37.2, and the removal rate of the aromatic hydrocarbon can reach more than 95%.
Description
Technical Field
The invention relates to a composite solvent suitable for separating naphthenic hydrocarbon and aromatic hydrocarbon from naphtha.
Background
Naphtha consists of normal paraffin, isoparaffin, cycloparaffin, aromatic hydrocarbon and the like, and is an important raw material for catalytic reforming and ethylene cracking. Among them, the yield of ethylene produced by cracking normal paraffin and isoparaffin is high, and the ethylene cannot be converted into aromatic hydrocarbon in the reforming process, so that the ethylene cracking raw material is an ideal ethylene cracking raw material. The cycloparaffins can obtain propylene and butadiene with higher yield after cracking, and can be easily converted into aromatic hydrocarbons under reforming conditions, so the cycloparaffins are suitable for raw materials of ethylene cracking and catalytic reforming. The aromatic hydrocarbon does not contribute to the yield of ethylene and the like during cracking, is easy to coke, and shortens the production period of the device. Thus, aromatics are not suitable as ethylene cracking feedstocks.
As crude oil becomes heavier, naphtha yields decrease, and the market demand for olefins and aromatics continues to increase, the problem of catalytic reforming and ethylene cracking unit feedstock configurations becomes more pronounced. At present, naphtha is separated mainly by adopting a light-heavy cutting mode in industry, and the method has the defects that the naphtha can not be effectively separated according to components, so that aromatic hydrocarbon is preferred, olefinic hydrocarbon is preferred, and raw materials can not be fully utilized. In addition, in the prior art, methods such as adsorption separation and extraction separation of naphtha have been studied, but they are mainly used for separating normal paraffins from naphtha.
CN1476474A discloses a method for selectively separating normal paraffin from naphtha by adsorption separation, and CN1710030A discloses a method for obtaining desorption oil rich in normal paraffin from naphtha by using molecular sieve as adsorbent. CN1292050C discloses a method for separating aromatic hydrocarbon and normal alkane from naphtha by using two-step method.
CN1277907C discloses a naphtha extraction separation method. The sulfolane is used as an extracting agent, and the alkane and the arene are obtained by separating naphtha under the conditions of the agent-oil ratio of 5-11, 95-128 ℃ and 0.6-1.0 MPa.
Although the ethylene cracking raw material rich in n-alkane can be obtained by the technology, the ethylene yield is improved, but the n-alkane or the aromatic hydrocarbon is mainly separated from the naphtha, and the cycloparaffin and the aromatic hydrocarbon cannot be flexibly separated at the same time, so the cycloparaffin in the naphtha is not well utilized.
Disclosure of Invention
The invention aims to provide a composite solvent suitable for simultaneously separating naphthenes and aromatic hydrocarbons from naphtha, which can enhance the separation effect of the naphthenes and the aromatic hydrocarbons from the naphtha, effectively separate the aromatic hydrocarbons contained in the naphtha by adjusting the compounding ratio of components, and adapt to the requirements of different ethylene cracking devices on the performance of naphtha raw materials by flexibly adjusting the proportion of the naphthenes in the naphtha.
In order to achieve the technical purpose, the invention adopts the following technical scheme:
the invention provides a composite solvent for separating cyclane and aromatic hydrocarbon from naphtha, which consists of N, N-dimethylformamide, cyclodextrin and 1-butyl-3-methylimidazolium dicyanamide salt.
The composite solvent provided by the invention is preferably as follows: the composition comprises the following components in parts by weight:
80-90 parts by weight of N, N-dimethylformamide;
10-20 parts of cyclodextrin;
1 part by weight of 1-butyl-3-methylimidazolium dicyanamide salt.
The invention provides a preparation method of the composite solvent, which is the preparation method of the composite solvent and specifically comprises the following steps: weighing N, N-dimethylformamide, keeping the set temperature of a reaction kettle constant at a preset temperature, sequentially and slowly adding cyclodextrin and 1-butyl-3-methylimidazol dicyanamide salt under the stirring condition, and continuously stirring until the mixture is uniformly mixed after the addition is finished to obtain the composite solvent.
The preparation method of the composite solvent provided by the invention is preferably as follows: the predetermined temperature is 60-80 ℃.
Finally, the invention provides a process for separating naphthenes and aromatics from naphtha, using the above-mentioned complex solvent, carried out on an extraction plant comprising:
one end of the static mixer M1 is connected with an N, N-dimethylformamide, cyclodextrin and 1-butyl-3-methylimidazolium dicyanamide storage tank, and the other end is respectively connected with the top of the extraction tower T1 and the bottom of the reduced pressure distillation tower T2; the bottom of the extraction tower T1 is connected with the inlet of the reduced pressure distillation tower T2;
the method for separating naphthenic hydrocarbon and aromatic hydrocarbon from naphtha comprises the following steps:
step (1): respectively leading N, N-dimethylformamide, cyclodextrin and 1-butyl-3-methylimidazolium dicyanamide salt out of respective storage tanks, and entering a static mixer M1; after fully mixing, introducing the mixture into a reduced pressure distillation tower T1 from the top of an extraction tower T1, and carrying out countercurrent contact with naphtha entering from the bottom of the T1, after liquid-liquid extraction, flowing raffinate oil out of the top of the reduced pressure distillation tower T1, and leading most of naphthenic hydrocarbon, aromatic hydrocarbon and all composite solvents out of the bottom of the reduced pressure distillation tower T1 to a reduced pressure distillation tower T2;
step (2): after the reduced pressure distillation, the composite solvent flows out from the bottom of the reduced pressure distillation tower T2 and circulates to the top of the reduced pressure distillation tower T1, the composite solvent and the fresh composite solvent are mixed and then enter the reduced pressure distillation tower T1, and the mixture of the naphthenic hydrocarbon and the aromatic hydrocarbon flows out from the top of the reduced pressure distillation tower T2.
The present invention provides a process for separating naphthenes and aromatics from naphtha, wherein it is preferred that: the mass ratio of the composite solvent to the naphtha is 2 to 10, preferably 2 to 6.
The present invention provides a process for separating naphthenes and aromatics from naphtha, wherein it is preferred that: the operating temperature of the static mixer is constantly between 60 and 80 ℃.
The present invention provides a process for separating naphthenes and aromatics from naphtha, wherein it is preferred that: the operating temperature of the extraction column T1 is between 30 and 120 ℃, preferably between 50 and 80 ℃, and the operating pressure of the extraction column T1 is between 0.01 and 2.0MPa, preferably between 0.1 and 1.0MPa.
The present invention provides a process for separating naphthenes and aromatics from naphtha, wherein it is preferred that: the operating temperature of the reduced pressure distillation tower T2 is 20-100 ℃, preferably 20-50 ℃; the operating pressure of the vacuum distillation column T2 is 0.01 to 0.08MPa, preferably 0.02 to 0.06MPa.
According to some embodiments of the invention, the invention may be further stated as follows:
a composite solvent suitable for separating cyclane and arene from naphtha and the main steps and method for compounding the solvent are detailed as follows:
1. the aromatic hydrocarbon is separated from the naphtha by taking N, N-dimethylformamide (I) as a main solvent.
2. The cyclodextrin (II) is added into the N, N-dimethylformamide (I) in a proper proportion to form a composite solvent, so that the effect of simultaneously separating aromatic hydrocarbon and naphthenic hydrocarbon from naphtha is further improved, and the selectivity of separating the naphthenic hydrocarbon is improved.
3. The ionic liquid 1-butyl-3-methylimidazole dicyanamide salt (III) is added into a composite solvent consisting of N, N-dimethylformamide (I) and cyclodextrin (II), so that the composite solvent has the effect of flexibly adjusting the proportion of naphthenes in naphtha.
4, compounding of solvents: firstly, weighing a certain amount of N, N-dimethylformamide (I), keeping the temperature constant within the range of 60-80 ℃, slowly adding cyclodextrin (II) and 1-butyl-3-methylimidazolium dicyanamide salt (III) according to a certain proportion in the stirring process, and continuing stirring until the solvent is uniformly mixed after the addition is finished.
According to the raw material characteristics of naphtha, the preparation temperature is constant within the range of 60-80 ℃.
According to the characteristics of the raw materials of naphtha, the mixing ratio of N, N-dimethylformamide (I), cyclodextrin (II) and 1-butyl-3-methylimidazol dicyanamide salt (III) is I: II: III = (80-90): 10-20): 1 (mass).
The composite solvent can extract naphtha at the temperature range of 30-80 ℃ and the pressure range of 0.01-2.0 MPa to separate arene and part or all of naphthenes as required.
The extraction performance of the composite solvent refers to the solubility of the composite solvent to the naphthenic hydrocarbon and the aromatic hydrocarbon in the naphtha under the condition of a certain solvent-oil ratio, and is characterized by using selectivity and removal rate parameters.
The selectivity was calculated using the formula:
in which S represents selectivity, C i Extracted oil Denotes the concentration of component i in the extract oil, C i Raffinate oil Indicating the concentration of the i component in the raffinate oil.
The removal rate was calculated using the following formula:
in which P% represents selectivity, C i Extracted oil Denotes the concentration of i component in the extract oil, C i Raw oil The concentration of the i component in the feed oil is shown, and β represents the yield of the raffinate oil.
The selectivity and the removal rate of the composite solvent to the naphthenic hydrocarbon in the naphtha can respectively reach 3.2 percent and 62 percent.
The selectivity and the removal rate of the composite solvent to the aromatic hydrocarbon in the naphtha can reach 37.0 percent and 95 percent.
The composite solvent has the adjustable characteristic that the extraction performance of the naphthenic hydrocarbon and the aromatic hydrocarbon in naphtha can be adjusted through the preparation proportion of the components.
The composite solvent provided by the invention is used for extracting and separating naphthenes and aromatics in naphtha, and the flow chart is shown in figure 1. Respectively leading N, N-dimethylformamide (I), cyclodextrin (II) and ionic liquid 1-butyl-3-methylimidazol dicyanamide salt (III) out of respective storage tanks, entering a static mixer M1, fully mixing, leading into an extraction tower T1 from the top of the tower, and carrying out countercurrent contact with naphtha entering from the bottom of the T1 tower; after liquid-liquid extraction, the material flow at the top of the T1 tower is naphtha (raffinate oil) with partial naphthenic hydrocarbon and aromatic hydrocarbon removed, and most of the naphthenic hydrocarbon, the aromatic hydrocarbon and all the composite solvents are led out to a reduced pressure distillation tower T2 from the bottom of the T1 tower; after reduced pressure distillation, the composite solvent flows out from the bottom of the T2 tower and circulates to the top of the T1 tower, the composite solvent and the fresh composite solvent are mixed and then enter the T1 tower, and the material flow at the top of the T2 tower is a mixture (extract oil) of naphthenic hydrocarbon and aromatic hydrocarbon and can be used as a catalytic reforming raw material or other purposes.
In the method, the ratio of N, N-dimethylformamide (I), cyclodextrin (II) and ionic liquid 1-butyl-3-methylimidazolium dicyanamide salt (III) in the composite solvent is I: II: III = (80-90): 10-20): 1 (mass).
In the above method, the mass ratio of the composite solvent to naphtha is (2 to 10): 1, preferably (2 to 6): 1.
In the above method, the operating temperature of the static mixer is constantly 60 to 80 ℃.
In the above process, the operating temperature of the extraction column T1 is 40 to 120 ℃ and preferably 50 to 80 ℃.
In the above method, the operating pressure of the extraction column T1 is 0.01 to 2.0MPa, preferably 0.1 to 1.0MPa.
In the above method, the operating temperature of the vacuum distillation column T2 is 20 to 100 ℃, preferably 20 to 50 ℃.
In the above method, the operating pressure of the reduced pressure distillation column T2 is 0.01 to 0.08MPa, preferably 0.02 to 0.06MPa.
The pressures are absolute pressures.
Drawings
Fig. 1 is a schematic view of the most basic flow scheme of an extraction and extraction apparatus, in which valves, pumps, reboilers, condensers, etc. are not involved, but are well known to those skilled in the art.
Detailed Description
The invention provides a composite solvent for separating cyclane and arene from naphtha and a preparation and use method thereof.
Example 1
The preparation method comprises the following steps of compounding N, N-dimethylformamide (I), cyclodextrin (II) and 1-butyl-3-methylimidazolium dicyanamide salt (III) to prepare a compound solvent, wherein the compounding ratio is I: II: III =80 (mass), extracting and separating naphtha fraction according to the flow of a figure 1, the composition of used naphtha is shown in a table 1, the extraction operation parameters, the used solvent and the like are shown in a table 2, and the composition of raffinate oil and extract oil is shown in a table 3.
Example 2
This embodiment is substantially the same as embodiment 1, and is characterized in that:
the solvent-oil ratio was increased from 2. The naphtha composition used in the distillation column is shown in Table 1, the extraction parameters, the solvent used, etc. are shown in Table 2, and the raffinate oil composition are shown in Table 3.
Example 3
This embodiment is substantially the same as embodiment 2, and is characterized in that:
the preparation method comprises the following steps of compounding N, N-dimethylformamide (I), cyclodextrin (II) and 1-butyl-3-methylimidazol dicyanamide salt (III) to prepare a compound solvent, wherein the compounding ratio is I: II: III = 90. The composition of the used naphtha is shown in Table 1, the extraction parameters, the used solvents and the like are shown in Table 2, and the composition of the raffinate oil and the raffinate oil is shown in Table 3.
Example 4
This embodiment is substantially the same as embodiment 2, and is characterized in that:
the preparation method comprises the following steps of (1) compounding N, N-dimethylformamide (I), cyclodextrin (II) and 1-butyl-3-methylimidazolium dicyanamide salt (III) to prepare a compound solvent, wherein the compounding ratio is I: II: III = 80. The compositions of naphtha used are shown in Table 1, the parameters of extraction operation, the solvents used, etc. are shown in Table 2, and the compositions of raffinate and extract oil are shown in Table 3.
Comparative example 1
This embodiment is substantially the same as embodiment 2, and is characterized in that: the solvent is a mixture of N, N-dimethylformamide (I) and cyclodextrin (II), I: II = 80. The composition of the used naphtha is shown in Table 1, the extraction parameters, the used solvents and the like are shown in Table 2, and the composition of the raffinate oil and the raffinate oil is shown in Table 3.
TABLE 1 naphtha composition
| Item | Alkane hydrocarbons | Cycloalkanes | Olefins | Aromatic hydrocarbons |
| PIONA value, mass% | 54.4 | 32.8 | 0.10 | 12.7 |
TABLE 2 extraction Process conditions
TABLE 3 extraction results
Claims (10)
1. A composite solvent for separating naphthene and aromatic hydrocarbon from naphtha is characterized by comprising the following components:
80-90 parts by weight of N, N-dimethylformamide;
10-20 parts of cyclodextrin; and
1 part by weight of 1-butyl-3-methylimidazolium dicyanamide salt;
wherein the composite solvent is prepared by the following method: weighing N, N-dimethylformamide, keeping the set temperature of a reaction kettle constant at 60-80 ℃, sequentially and slowly adding cyclodextrin and 1-butyl-3-methylimidazol dicyanamide salt under the stirring condition, and continuously stirring until the mixture is uniformly mixed after the addition is finished to obtain the composite solvent.
2. The preparation method of the composite solvent according to claim 1, which comprises the following steps: weighing N, N-dimethylformamide, keeping the set temperature of a reaction kettle constant at a preset temperature, sequentially and slowly adding cyclodextrin and 1-butyl-3-methylimidazolium dicyanamide under the stirring condition, and continuously stirring until the cyclodextrin and the 1-butyl-3-methylimidazolium dicyanamide are uniformly mixed after the addition is finished to obtain the composite solvent;
wherein the predetermined temperature is 60-80 ℃.
3. A process for separating naphthenes and aromatics from naphtha, characterized by using the complex solvent of claim 1, carried out on an extraction apparatus comprising:
one end of the static mixer M1 is respectively connected with an N, N-dimethylformamide storage tank, a cyclodextrin storage tank and a 1-butyl-3-methylimidazol dicyanamide storage tank, and the other end of the static mixer M1 is respectively connected with the top of the extraction tower T1 and the bottom of the reduced pressure distillation tower T2; the bottom of the extraction tower T1 is connected with the inlet of the reduced pressure distillation tower T2;
the method for separating naphthenic hydrocarbon and aromatic hydrocarbon from naphtha comprises the following steps:
step (1): respectively leading N, N-dimethylformamide, cyclodextrin and 1-butyl-3-methylimidazolium dicyanamide salt out of respective storage tanks, and entering a static mixer M1; after fully mixing, introducing the mixture into an extraction tower T1 from a static mixer M1, and carrying out countercurrent contact with naphtha entering from the bottom of the extraction tower T1, after liquid-liquid extraction, flowing raffinate oil out of the top of the extraction tower T1, and leading most of naphthenic hydrocarbon, aromatic hydrocarbon and all composite solvents out of the bottom of the extraction tower T1 to a reduced pressure distillation tower T2;
step (2): after the reduced pressure distillation, the composite solvent flows out from the bottom of the reduced pressure distillation tower T2 and circulates to the top of the extraction tower T1, the composite solvent and the fresh composite solvent enter the extraction tower T1 together, and the naphthenic hydrocarbon and aromatic hydrocarbon mixture flows out from the top of the reduced pressure distillation tower T2.
4. The method of claim 3, wherein the mass ratio of the composite solvent to the naphtha is 2-10.
5. The method of claim 4, wherein the mass ratio of the composite solvent to the naphtha is 2-6.
6. The process for the separation of naphthenic and aromatic hydrocarbons from naphtha as claimed in claim 3, wherein the operating temperature of the static mixer M1 is constantly between 60 and 80 ℃.
7. The method of claim 3, wherein the operating temperature of the extraction column T1 is 30-120 ℃ and the operating pressure of the extraction column T1 is 0.01-2.0 MPa.
8. The method of claim 7, wherein the operating temperature of the extraction column T1 is 50-80 ℃ and the operating pressure of the extraction column T1 is 0.1-1.0 MPa.
9. The method for separating cycloalkanes and aromatics from naphtha as claimed in claim 3, wherein the operating temperature of the vacuum distillation tower T2 is 20 to 100 ℃; the operating pressure of the reduced pressure distillation tower T2 is 0.01-0.08 MPa.
10. The method for separating naphthenes and aromatics from naphtha as claimed in claim 9, wherein the operating temperature of vacuum distillation column T2 is 20 to 50 ℃; the operating pressure of the reduced pressure distillation tower T2 is 0.02-0.06 MPa.
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Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1261395A (en) * | 1997-07-03 | 2000-07-26 | 埃克森化学专利公司 | Removal of benzene from organic streams using cyclodextrins |
| CN106431836A (en) * | 2016-09-19 | 2017-02-22 | 青岛科技大学 | Technology for separating ethyl alcohol-water system by means of extractive distillation and flash coupling |
| CN110229692A (en) * | 2018-03-05 | 2019-09-13 | 中国石油天然气股份有限公司 | The complex solvent and its preparation method and application of cycloalkane and aromatic hydrocarbons is isolated from naphtha |
-
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- 2019-11-14 CN CN201911111969.5A patent/CN112795397B/en active Active
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1261395A (en) * | 1997-07-03 | 2000-07-26 | 埃克森化学专利公司 | Removal of benzene from organic streams using cyclodextrins |
| CN106431836A (en) * | 2016-09-19 | 2017-02-22 | 青岛科技大学 | Technology for separating ethyl alcohol-water system by means of extractive distillation and flash coupling |
| CN110229692A (en) * | 2018-03-05 | 2019-09-13 | 中国石油天然气股份有限公司 | The complex solvent and its preparation method and application of cycloalkane and aromatic hydrocarbons is isolated from naphtha |
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