CN116948685A - Composite solvent, method and device for simultaneously separating naphthenes and aromatic hydrocarbons from naphtha - Google Patents
Composite solvent, method and device for simultaneously separating naphthenes and aromatic hydrocarbons from naphtha Download PDFInfo
- Publication number
- CN116948685A CN116948685A CN202210401203.6A CN202210401203A CN116948685A CN 116948685 A CN116948685 A CN 116948685A CN 202210401203 A CN202210401203 A CN 202210401203A CN 116948685 A CN116948685 A CN 116948685A
- Authority
- CN
- China
- Prior art keywords
- naphtha
- naphthenes
- composite solvent
- aromatics
- simultaneously separating
- 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.)
- Pending
Links
- 239000002904 solvent Substances 0.000 title claims abstract description 56
- 239000002131 composite material Substances 0.000 title claims abstract description 47
- 150000004945 aromatic hydrocarbons Chemical class 0.000 title claims abstract description 41
- 238000000034 method Methods 0.000 title claims abstract description 29
- 238000000605 extraction Methods 0.000 claims abstract description 42
- IAZDPXIOMUYVGZ-UHFFFAOYSA-N Dimethylsulphoxide Chemical compound CS(C)=O IAZDPXIOMUYVGZ-UHFFFAOYSA-N 0.000 claims abstract description 28
- MSBXTPRURXJCPF-DQWIULQBSA-N cucurbit[6]uril Chemical compound N1([C@@H]2[C@@H]3N(C1=O)CN1[C@@H]4[C@@H]5N(C1=O)CN1[C@@H]6[C@@H]7N(C1=O)CN1[C@@H]8[C@@H]9N(C1=O)CN([C@H]1N(C%10=O)CN9C(=O)N8CN7C(=O)N6CN5C(=O)N4CN3C(=O)N2C2)C3=O)CN4C(=O)N5[C@@H]6[C@H]4N2C(=O)N6CN%10[C@H]1N3C5 MSBXTPRURXJCPF-DQWIULQBSA-N 0.000 claims abstract description 23
- UFWIBTONFRDIAS-UHFFFAOYSA-N Naphthalene Chemical compound C1=CC=CC2=CC=CC=C21 UFWIBTONFRDIAS-UHFFFAOYSA-N 0.000 claims abstract description 13
- 238000000926 separation method Methods 0.000 claims abstract description 11
- XDZAFZVZTAGZHI-UHFFFAOYSA-N 1-ethyl-3-methyl-1,2-dihydroimidazol-1-ium;ethyl sulfate Chemical compound CCOS([O-])(=O)=O.CC[NH+]1CN(C)C=C1 XDZAFZVZTAGZHI-UHFFFAOYSA-N 0.000 claims abstract description 9
- 239000000203 mixture Substances 0.000 claims description 20
- 230000003068 static effect Effects 0.000 claims description 18
- 238000004821 distillation Methods 0.000 claims description 13
- 238000002156 mixing Methods 0.000 claims description 9
- 239000000706 filtrate Substances 0.000 claims description 3
- JFYNWAHGEKCOGV-UHFFFAOYSA-N 2-ethyl-3-methyl-1h-imidazol-3-ium;ethyl sulfate Chemical compound CCOS([O-])(=O)=O.CCC1=NC=C[NH+]1C JFYNWAHGEKCOGV-UHFFFAOYSA-N 0.000 claims description 2
- 229910052799 carbon Inorganic materials 0.000 claims description 2
- 238000004891 communication Methods 0.000 claims description 2
- 150000001923 cyclic compounds Chemical class 0.000 abstract description 4
- 230000000694 effects Effects 0.000 abstract description 3
- -1 naphthenes Chemical class 0.000 abstract description 2
- 238000013329 compounding Methods 0.000 abstract 2
- 239000002608 ionic liquid Substances 0.000 description 12
- 238000005292 vacuum distillation Methods 0.000 description 12
- 239000000463 material Substances 0.000 description 10
- 101000623895 Bos taurus Mucin-15 Proteins 0.000 description 8
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 description 8
- 239000005977 Ethylene Substances 0.000 description 8
- 239000002994 raw material Substances 0.000 description 7
- 238000005336 cracking Methods 0.000 description 6
- 230000000052 comparative effect Effects 0.000 description 5
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 3
- 239000004215 Carbon black (E152) Substances 0.000 description 3
- 150000001875 compounds Chemical class 0.000 description 3
- 238000005086 pumping Methods 0.000 description 3
- KAKZBPTYRLMSJV-UHFFFAOYSA-N Butadiene Chemical compound C=CC=C KAKZBPTYRLMSJV-UHFFFAOYSA-N 0.000 description 2
- RAKJBKORKMXGSJ-UHFFFAOYSA-N S(=O)(=O)(O)O.C(C)C1N(C=CN1C)CC Chemical compound S(=O)(=O)(O)O.C(C)C1N(C=CN1C)CC RAKJBKORKMXGSJ-UHFFFAOYSA-N 0.000 description 2
- 150000001336 alkenes Chemical class 0.000 description 2
- 238000001833 catalytic reforming Methods 0.000 description 2
- 150000001924 cycloalkanes Chemical class 0.000 description 2
- 229930195733 hydrocarbon Natural products 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 238000000197 pyrolysis Methods 0.000 description 2
- 238000001179 sorption measurement Methods 0.000 description 2
- XDTMQSROBMDMFD-UHFFFAOYSA-N Cyclohexane Chemical compound C1CCCCC1 XDTMQSROBMDMFD-UHFFFAOYSA-N 0.000 description 1
- 241001372564 Piona Species 0.000 description 1
- 125000003118 aryl group Chemical group 0.000 description 1
- 239000013064 chemical raw material Substances 0.000 description 1
- 239000000571 coke Substances 0.000 description 1
- 238000005520 cutting process Methods 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000002283 diesel fuel Substances 0.000 description 1
- 238000004090 dissolution Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- 238000000622 liquid--liquid extraction Methods 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 239000012188 paraffin wax Substances 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 description 1
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 description 1
- 238000002407 reforming Methods 0.000 description 1
- 238000000638 solvent extraction Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- HXJUTPCZVOIRIF-UHFFFAOYSA-N sulfolane Chemical compound O=S1(=O)CCCC1 HXJUTPCZVOIRIF-UHFFFAOYSA-N 0.000 description 1
Classifications
-
- 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
-
- 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
-
- 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
- C10G2300/20—Characteristics of the feedstock or the products
- C10G2300/201—Impurities
- C10G2300/202—Heteroatoms content, i.e. S, N, O, P
Landscapes
- Chemical & Material Sciences (AREA)
- 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)
Abstract
The invention discloses a composite solvent, a method and a device suitable for separating naphthene and aromatic hydrocarbon from naphtha, wherein the composite solvent is formed by compounding dimethyl sulfoxide (I), cucurbituril (II) and 1-ethyl-3-methylimidazole ethyl sulfate salt (III), the mass compounding ratio of the three is I: II: III= (85-96): (3-14): 1, the selectivity of the composite solvent to the naphthene can reach 6.27, and the mass removal rate of the naphthene can reach 71.34%; the selectivity to aromatic hydrocarbon can reach 36.16, and the mass removal rate of aromatic hydrocarbon is 91.51%. The invention is characterized in that cyclic compounds such as naphthenes, aromatic hydrocarbons and the like in naphtha are enriched at the bottom of a reactor by utilizing the special structure and characteristics of cucurbiturils, and the effect of rapid separation is achieved by arranging a filter at the bottom of an extraction tower.
Description
Technical Field
The invention relates to the technical field of separating naphthenes and aromatic hydrocarbons from naphtha, in particular to a composite solvent for simultaneously separating naphthenes and aromatic hydrocarbons from naphtha, and a method and a device for using the composite solvent.
Background
In the petrochemical production process, naphtha is an important chemical raw material, and mainly consists of normal paraffins, isoparaffins, naphthenes, aromatic hydrocarbons and the like, wherein the yield of ethylene produced by cracking the normal paraffins and isoparaffins is high, and the naphtha is an ideal ethylene cracking raw material. Propylene and butadiene with higher yield can be obtained after cycloparaffin pyrolysis, but the ethylene yield is not high, and the proportion of the cycloparaffin in the ethylene pyrolysis raw material needs to be controlled well; in addition, naphthenes are also easily converted into aromatics under reforming conditions, and therefore, naphthenes are suitable for use as both an ethylene cracking feedstock and a catalytic reforming feedstock; the arene has no contribution to the yield of ethylene and the like during cracking, is easy to coke, shortens the production period of the device, and is not suitable for being used as an ethylene cracking raw material.
At present, the method mainly adopts a light and heavy cutting mode to separate the carbon-hydrocarbon mixture in industry, and has the defect that the method cannot effectively separate the carbon-hydrocarbon mixture according to the components, and cannot realize aromatic character and alkene character, so that the raw materials cannot be fully utilized.
In addition, the prior art has studied adsorption and extraction separations of naphtha, CN1476474A, CN1710030a discloses a method for selectively separating normal paraffins from naphtha by adsorption separation. Although these methods can obtain ethylene cracking raw materials rich in normal paraffins, they mainly separate normal paraffins or aromatic hydrocarbons from naphtha, and cannot separate naphthenes/aromatic hydrocarbons from naphtha at the same time.
CN104945328A discloses a method for separating aromatic hydrocarbon from diesel oil by using an ionic liquid, CN101265152A discloses a method for separating cyclohexane and benzene by using an ionic liquid, CN102405084A discloses a method for separating aromatic hydrocarbon isomers by using an ionic liquid, and the above technology shows that it is feasible to develop a composite solvent containing an ionic liquid for separating naphthene/aromatic hydrocarbon from naphtha simultaneously according to the composition characteristics of naphtha by using a mixture of ionic liquid separation substances, and therefore CN110229692A discloses a method for separating naphthene/aromatic hydrocarbon from naphtha simultaneously by using a composite solvent containing an ionic liquid, but in actual operation, it is found that part of ionic liquid is still entrained in raffinate oil, so that loss of ionic liquid may occur in the subsequent separation process.
Disclosure of Invention
Based on the problems existing in the prior art, the invention aims to provide a composite solvent, a method and a device for simultaneously separating naphthenes/aromatic hydrocarbons from naphtha, wherein the composite solvent is formed by adding cucurbituril, ionic liquid and the like, and cyclic compounds such as naphthenes and aromatic hydrocarbons in the naphtha are enriched by utilizing the special structure and characteristics of the cucurbituril, so that the effect of simultaneously separating naphthenes/aromatic hydrocarbons from the naphtha is enhanced, and the problems of loss and loss possibly caused by the ionic liquid entering a subsequent separation process are avoided to the greatest extent.
In order to achieve the aim, the invention provides a composite solvent for simultaneously separating naphthenes and aromatic hydrocarbons from naphtha, which consists of dimethyl sulfoxide, cucurbituril and 1-ethyl-3-methylimidazole ethyl sulfate salt, wherein the mass ratio of the dimethyl sulfoxide to the cucurbituril to the ethyl-3-methylimidazole ethyl sulfate salt is 85-96:3-14:1. The composite solvent for simultaneously separating naphthenes/aromatic hydrocarbons from naphtha disclosed by the invention takes dimethyl sulfoxide (component I) as a main solvent, and the main function of the composite solvent is to separate aromatic hydrocarbons from naphtha. The cucurbituril (component II) and the ethyl 1-ethyl-3-methylimidazole sulfate salt (component III) are added into the dimethyl sulfoxide (component I) in proper proportion, and the main functions are to separate naphthenes/aromatic hydrocarbons from naphtha at the same time, and the separation proportion of the naphthenes can be flexibly adjusted. The composite solvent has adjustable characteristic, namely, the extraction performance of separating naphthene and arene is adjusted through the preparation proportion of the components. The compound solvent is prepared at constant temperature within the range of 40-100 ℃. The composite solvent can extract and separate naphtha at 60-100 ℃ and 0.01-1.0 MPa, and separate part or all of naphthene/arene from naphtha according to the requirement.
The present invention also provides a process for simultaneously separating naphthenes and aromatics from naphtha, the process comprising the steps of: the composite solvent is mixed with naphtha and then filtered, and the filtered product stream is rich in naphthenes and aromatics.
In the process of the present invention, the mass ratio of the complex solvent to the naphtha is 2 to 8:1, preferably 2 to 6:1.
In the method of the invention, the temperature of the mixing is 60-100 ℃ and the pressure is 0.01-1.0 MPa.
In the method of the invention, the temperature of the mixing is 70-90 ℃ and the pressure is 0.02-0.5 MPa.
The method of the invention further comprises the following steps: and separating naphthene and aromatic hydrocarbon from the filtrate flow through reduced pressure distillation to obtain regenerated composite solvent, wherein the regenerated composite solvent is recycled.
In the method of the present invention, the reduced pressure distillation is carried out at a temperature of 60 to 100 ℃, preferably 70 to 90 ℃, and a pressure of-0.01 to-0.08 MPa, preferably-0.02 to-0.06 MPa.
The invention also provides a device for simultaneously separating naphthene and aromatic hydrocarbon from naphtha, which is characterized by comprising an extraction tower and a reduced pressure distillation tower, wherein a raffinate oil outlet and a discharge port are respectively arranged at the top and the bottom of the extraction tower, a filter is arranged above the discharge port, a composite solvent inlet and a raw oil inlet are respectively arranged at the upper part and the lower part of the extraction tower, an extract oil outlet and a regenerated composite solvent outlet are respectively arranged at the top and the bottom of the reduced pressure distillation tower, a mixed material inlet is arranged at the middle part of the reduced pressure distillation tower, and the mixed material inlet is communicated with the discharge port.
The device of the invention further comprises a mixer, wherein the outlet of the mixer is communicated with the composite solvent inlet or the regenerated composite solvent outlet.
In the device of the invention, the mixer is a static mixer, and the operation temperature of the static mixer is constant at 40-100 ℃.
According to the composite solvent, the cucurbituril is added to form the composite solvent with the ionic liquid and the like, and cyclic compounds such as naphthenes and aromatic hydrocarbons in naphtha are enriched by utilizing the special structure and characteristics of the cucurbituril, so that the effect of separating naphthenes/aromatic hydrocarbons from naphtha simultaneously is enhanced, and the problems of loss and loss possibly caused by the ionic liquid entering a subsequent separation process are avoided to the greatest extent. The selectivity and the mass removal rate of the composite solvent for the naphthenes in the naphtha can reach 6.27 and 71.34 percent respectively, and the selectivity and the mass removal rate for the aromatics in the naphtha can reach 36.16 and 91.51 percent.
Drawings
FIG. 1 is a schematic diagram of an apparatus for simultaneously separating naphthenes and aromatics from naphtha according to the present invention.
Wherein,,
1. an extraction tower is arranged on the bottom of the extraction tower,
11. a raffinate oil outlet is arranged on the bottom of the oil tank,
12. composite solvent inlet
13. A naphtha feed inlet and a gas oil feed inlet,
14. the filter is used for the filter,
2. a reduced pressure distillation tower,
21. an oil outlet for the oil to be pumped out,
22. a material inlet rich in naphthenes,
3. the mixing device of the static mixer is provided with a mixing device,
31. an inlet of the dimethyl sulfoxide is arranged on the bottom of the container,
32. an inlet of the cucurbituril,
33. an inlet for ethyl 1-ethyl-3-methylimidazole sulfate salt.
Detailed Description
The following describes embodiments of the present invention in detail: the present example is implemented on the premise of the technical scheme of the present invention, and detailed implementation modes and processes are given, but the protection scope of the present invention is not limited to the following examples, and experimental methods without specific conditions are not noted in the following examples, and generally according to conventional conditions.
Referring to fig. 1, fig. 1 is a schematic view of an apparatus for simultaneously separating naphthenes and aromatics from naphtha according to the present invention. The device comprises an extraction tower 1 and a reduced pressure distillation tower 2, wherein a raffinate oil outlet 11 and a composite solvent inlet 12 are respectively arranged at the top of the extraction tower 1, a filter 14 is arranged at the bottom of the extraction tower, and a naphtha feed inlet 13 is arranged at the lower part of the extraction tower. The top of the vacuum distillation tower 2 is provided with an extracted oil outlet 21, the middle of the vacuum distillation tower is provided with a naphthene-rich material inlet 22, and the naphthene-rich material inlet 22 is communicated with a discharge port of the extraction tower 1. The apparatus further comprises a static mixer 3, the outlet of the static mixer 3 being in communication with the complex solvent inlet 12.
Referring to fig. 1, the method for simultaneously separating naphthenes and aromatic hydrocarbons from naphtha provided by the invention comprises the following steps: dimethyl sulfoxide (component I) enters the static mixer 3 from a dimethyl sulfoxide inlet 31, cucurbituril (component II) enters the static mixer from a cucurbituril inlet 32 and 1-ethyl-3-methylimidazole ethyl sulfate salt (component III) enters the static mixer 33 respectively, and after being fully mixed, the mixture is introduced into the extraction tower 1 from a composite solvent inlet 12 at the upper part of the extraction tower 1 and is in countercurrent contact with a carbon hydrocarbon mixture raw material entering from a naphtha feed inlet 13 at the lower part of the extraction tower 1; after liquid-liquid extraction and extraction, the top material flow of the extraction tower 1 is raffinate oil from which part of naphthenes and aromatic hydrocarbons are removed, and most of naphthenes, aromatic hydrocarbons and all of the compound solvents are enriched at the lower part of the extraction tower 1, unlike the traditional process, a filter 14 is designed and installed above a discharge hole at the bottom of the extraction tower 1, the bottom of the extraction tower 1 can be divided into two areas, a cucurbituril-rich area is arranged above the filter 14, a cucurbituril-lean area is arranged below the filter 14, and the arrangement of the cucurbituril-rich area and the cucurbituril-lean area can prevent cucurbituril from entering a reduced pressure distillation tower to cause unnecessary blockage. The material flow of the cucurbituril-lean zone below the bottom filter 14 of the extraction tower 1 is rich in naphthenes and aromatic hydrocarbons, the material flow is led out to the vacuum distillation tower 2 through a discharge port, after vacuum distillation in the vacuum distillation tower 2, the material flow (regenerated composite solvent) flowing out from the bottom of the vacuum distillation tower 2 is circulated to the composite solvent inlet 12 of the extraction tower 1, and is mixed with fresh composite solvent from the static mixer 3, and then enters the extraction tower 1, the top material flow of the vacuum distillation tower 2 is extracted oil (naphthenes and aromatic hydrocarbon mixture), and the extracted oil can be used as catalytic reforming raw materials or other purposes.
The extraction separation performance of the composite solvent refers to the dissolution performance of the composite solvent on the naphthenes and the aromatic hydrocarbons in naphtha under the condition of a certain solvent-to-oil ratio, and is characterized by using selectivity and removal rate parameters.
The selectivity was calculated using the following formula:
wherein S represents selectivity, C i Pumping out oil And C j Pumping out oil Respectively representing the mass concentration of the i and j components in the extracted oil, C i Raffinate oil And C j Raffinate oil The mass concentrations of the i and j components in the raffinate are shown, respectively.
The removal rate is calculated by the following formula:
wherein P% represents the removal rate, C i Pumping out oil Represents the mass concentration of component i in the extracted oil, C i Raw oil Indicating the mass concentration of component i in the feed oil and beta indicates the yield of raffinate oil.
Example 1
Mixing dimethyl sulfoxide (component I), cucurbituril (component II) and 1-ethyl-3-methylimidazole ethyl sulfate salt (component III) in a static mixer 3, wherein the ratio of component I to component II to component III=85:14:1 (mass), extracting and separating naphtha according to the flow of FIG. 1, and the mass ratio of the composite solvent to naphtha raw oil is 2:1; the operating conditions of the static mixer 3 are: the temperature is 60 ℃; the operating conditions of the extraction column 1 are: the temperature is 80 ℃ and the pressure is 0.20MPa; the operating conditions of the vacuum distillation column 2 were: the temperature is 70 ℃ and the pressure is 0.04MPa.
The naphtha composition used is shown in Table 1, the extraction operating parameters are shown in Table 2, and the raffinate oil and extract oil compositions are shown in Table 3.
Example 2
Mixing dimethyl sulfoxide (component I), cucurbituril (component II) and 1-ethyl-3-methylimidazole ethyl sulfate salt (component III) in a static mixer 3, wherein the ratio of component I to component II to component III=91:8:1 (mass), extracting and separating naphtha according to the flow of FIG. 1, and the mass ratio of the composite solvent to naphtha raw oil is 2:1; the operating conditions of the static mixer 3 are: the temperature is 60 ℃; the operating conditions of the extraction column 1 are: the temperature is 80 ℃ and the pressure is 0.20MPa; the operating conditions of the vacuum distillation column 2 were: the temperature is 70 ℃ and the pressure is 0.04MPa.
The naphtha composition used is shown in Table 1, the extraction operating parameters are shown in Table 2, and the raffinate oil and extract oil compositions are shown in Table 3.
Example 3
Mixing dimethyl sulfoxide (component I), cucurbituril (component II) and 1-ethyl-3-methylimidazole ethyl sulfate salt (component III) in a static mixer 3, wherein the ratio of component I to component II to component III=96:3:1 (mass), extracting and separating naphtha according to the flow of FIG. 1, and the mass ratio of the composite solvent to naphtha raw oil is 2:1; the operating conditions of the static mixer 3 are: the temperature is 60 ℃; the operating conditions of the extraction column 1 are: the temperature is 80 ℃ and the pressure is 0.20MPa; the operating conditions of the vacuum distillation column 2 were: the temperature is 70 ℃ and the pressure is 0.04MPa.
The naphtha composition used is shown in Table 1, the extraction operating parameters are shown in Table 2, and the raffinate oil and extract oil compositions are shown in Table 3.
Comparative example 1
This comparative example is substantially the same as example 2, except that:
the compound solvent is compounded by dimethyl sulfoxide (component I) and 1-ethyl-3-methylimidazole ethyl sulfate salt (component III), wherein the proportion is that the component I is that the component III=99:1 (mass). Wherein the mass ratio of the composite solvent to the naphtha raw oil is 2:1; the operating conditions of the static mixer 3 are: the temperature is 60 ℃; the operating conditions of the extraction column 1 are: the temperature is 80 ℃ and the pressure is 0.30MPa; the operating conditions of the vacuum distillation column 2 were: the temperature is 70 ℃ and the pressure is 0.04MPa.
The composition of the naphtha used is shown in Table 1, the extraction parameters are shown in Table 2, and the raffinate oil and extract oil compositions are shown in Table 3.
Comparative example 2
This comparative example is substantially the same as example 2, except that:
sulfolane (component I) and 1-ethyl-3-methylimidazole ethyl sulfate salt (component III) are compounded in a ratio of I to II=99 to 1 (mass), wherein the mass ratio of the composite solvent to the naphtha raw oil is 2 to 1; the operating conditions of the static mixer 3 are: the temperature is 60 ℃; the operating conditions of the extraction column 1 are: the temperature is 100 ℃ and the pressure is 0.30MPa; the operating conditions of the vacuum distillation column 2 were: the temperature is 80 ℃ and the pressure is 0.05MPa.
The composition of the naphtha used is shown in Table 1, the extraction parameters are shown in Table 2, and the raffinate oil and extract oil compositions are shown in Table 3.
Table 1 naphtha composition
| Project | Paraffin hydrocarbons | Cycloalkane (CNS) | Olefins | Aromatic hydrocarbons |
| PIONA value, mass% | 55.4 | 30.4 | 0.1 | 14.1 |
TABLE 2 extraction process conditions
TABLE 3 extraction results
As shown by the results in Table 3, the invention utilizes the special structure and characteristics of cucurbituril to enrich cyclic compounds such as naphthenes and aromatic hydrocarbons in naphtha at the bottom of a reactor so as to realize rapid separation, and compared with the comparative example without cucurbituril, the selectivity of the composite solvent to naphthenes can reach 6.27, and the quality removal rate of naphthenes can reach 71.34%; meanwhile, the selectivity of the composite solvent to the aromatic hydrocarbon can reach 36.16, and the mass removal rate of the aromatic hydrocarbon can reach 91.51%.
In addition, the filter is additionally arranged above the lower outlet of the extraction tower 1, so that the possibility of blockage of heavy components in subsequent equipment pipelines is reduced to a certain extent on the premise of ensuring the normal operation of the extraction tower.
Of course, the present invention is capable of other various embodiments and its several details are capable of modification and variation in light of the present invention by one skilled in the art without departing from the spirit and scope of the invention.
Claims (10)
1. The composite solvent is characterized by comprising dimethyl sulfoxide, cucurbituril and 1-ethyl-3-methylimidazole ethyl sulfate salt, wherein the mass ratio of the dimethyl sulfoxide to the cucurbituril to the ethyl-3-methylimidazole ethyl sulfate salt is 85-96:3-14:1.
2. A process for simultaneously separating naphthenes and aromatics from naphtha comprising the steps of: the composite solvent of claim 1 is mixed with naphtha and then filtered, and the filtrate stream is enriched in naphthenes and aromatics.
3. The method for simultaneously separating naphthenes and aromatics from naphtha according to claim 2, wherein the mass ratio of said complex solvent to said naphtha is 2-8:1, preferably 2-6:1.
4. The method for simultaneously separating naphthenes and aromatics from naphtha according to claim 2, wherein said mixing is at a temperature of 60-100 ℃ and a pressure of 0.01-1.0 MPa.
5. The method for simultaneously separating naphthenes and aromatics from naphtha according to claim 4, wherein said mixing is performed at a temperature of 70-90 ℃ and a pressure of 0.02-0.5 MPa.
6. The method for simultaneously separating naphthenes and aromatics from naphtha according to claim 2, further comprising the steps of: and separating naphthene and aromatic hydrocarbon from the filtrate flow through reduced pressure distillation to obtain regenerated composite solvent, wherein the regenerated composite solvent is recycled.
7. The process for simultaneous separation of naphthenes and aromatics from naphtha according to claim 6, wherein said reduced pressure distillation is carried out at a temperature of 60-100 ℃, preferably 70-90 ℃, and at a pressure of-0.01 to-0.08 MPa, preferably-0.02 to-0.06 MPa.
8. The device for simultaneously separating naphthene and aromatic hydrocarbon from naphtha comprises an extraction tower and a reduced pressure distillation tower, wherein a raffinate oil outlet and a discharge port are respectively arranged at the top and the bottom of the extraction tower, a filter is arranged above the discharge port, a composite solvent inlet and a raw oil inlet are respectively arranged at the upper part and the middle part of the extraction tower, an extract oil outlet and a regenerated composite solvent outlet are respectively arranged at the top and the bottom of the reduced pressure distillation tower, a mixture inlet is arranged at the middle part of the reduced pressure distillation tower, and the mixture inlet is communicated with the discharge port.
9. The apparatus for simultaneously separating naphthenes and aromatics from naphtha according to claim 8, further comprising a mixer, an outlet of said mixer being in communication with said complex solvent inlet or said regenerated complex solvent outlet.
10. The apparatus for simultaneously separating naphthenes and aromatics from naphtha according to claim 9, wherein said mixer is a static mixer whose operating temperature is constant at 40-100 ℃.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202210401203.6A CN116948685A (en) | 2022-04-15 | 2022-04-15 | Composite solvent, method and device for simultaneously separating naphthenes and aromatic hydrocarbons from naphtha |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202210401203.6A CN116948685A (en) | 2022-04-15 | 2022-04-15 | Composite solvent, method and device for simultaneously separating naphthenes and aromatic hydrocarbons from naphtha |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN116948685A true CN116948685A (en) | 2023-10-27 |
Family
ID=88447837
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202210401203.6A Pending CN116948685A (en) | 2022-04-15 | 2022-04-15 | Composite solvent, method and device for simultaneously separating naphthenes and aromatic hydrocarbons from naphtha |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN116948685A (en) |
-
2022
- 2022-04-15 CN CN202210401203.6A patent/CN116948685A/en active Pending
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN111954654B (en) | Method for separating aromatic hydrocarbon by extractive distillation | |
| WO2006048098A1 (en) | Device for removing oxygen-containing organic compounds from mixtures of various hydrocarbon compounds | |
| KR101700986B1 (en) | Fractional extraction of butadiene | |
| RU2615160C2 (en) | Method of producing olefins and aromatic hydrocarbons | |
| CN110229692B (en) | Compound solvent for separating cycloparaffin and arene from naphtha and preparation method and application thereof | |
| US3660016A (en) | Removal of carbon dioxide and/or hydrogen sulfide from gases containing olefines and acetylenes | |
| KR20230086707A (en) | Recovery of aliphatic hydrocarbons | |
| US3864245A (en) | Solvent extraction with increased polar hydrocarbon purity | |
| US8696871B2 (en) | Apparatus for removing a contaminant from a solvent separation process | |
| EP1650287B1 (en) | A method for recombining catalytic hydrocarbons | |
| CN116948685A (en) | Composite solvent, method and device for simultaneously separating naphthenes and aromatic hydrocarbons from naphtha | |
| CN108504382B (en) | Compound solvent for separating cyclane and arene from naphtha, preparation method and application thereof | |
| CN108329946B (en) | Method for separating gasoline fraction and gasoline desulfurization method | |
| CN108424786B (en) | Separation method of gasoline fraction and gasoline desulfurization method | |
| RU2203306C2 (en) | Method of preparing feedstock for catalytic cracking and hydrocracking | |
| CN112795397B (en) | Composite solvent for separating cyclane and aromatic hydrocarbon from naphtha | |
| CN115634470B (en) | Method for separating naphthene and aromatic hydrocarbon from naphtha and composite solvent used in method | |
| RU2221836C1 (en) | Vacuum gas oil purification process associated with production of carbon black manufacture feedstock | |
| US2248067A (en) | Solvent extraction process | |
| RU2785840C2 (en) | Method for separation of aromatic hydrocarbons, using extraction distillation | |
| US2401758A (en) | Elimination of acetylenes from diolefins | |
| CN114350402A (en) | Preparation method of high aromatic oil | |
| CN117923589A (en) | Method for extracting aromatic hydrocarbon in sewage by using dual-purpose extractant | |
| CN116286084A (en) | Method for dearomatizing straight-run diesel oil fraction | |
| JPS6327441A (en) | Method for separating hydrocarbon blend |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination |