CN111996029A - C6~C10Method for purifying mixed aromatic hydrocarbon - Google Patents
C6~C10Method for purifying mixed aromatic hydrocarbon Download PDFInfo
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- CN111996029A CN111996029A CN202010798498.6A CN202010798498A CN111996029A CN 111996029 A CN111996029 A CN 111996029A CN 202010798498 A CN202010798498 A CN 202010798498A CN 111996029 A CN111996029 A CN 111996029A
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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
- C10G25/00—Refining of hydrocarbon oils in the absence of hydrogen, with solid sorbents
- C10G25/06—Refining of hydrocarbon oils in the absence of hydrogen, with solid sorbents with moving sorbents or sorbents dispersed in the oil
- C10G25/08—Refining of hydrocarbon oils in the absence of hydrogen, with solid sorbents with moving sorbents or sorbents dispersed in the oil according to the "moving bed" method
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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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Abstract
The invention relates to a compound C6～C10A process for the purification of mixed aromatics, the process comprising: c is to be6～C10The mixed aromatic hydrocarbon passes through a simulated moving bed device to adsorb and separate aromatic hydrocarbon components in the raw materials to obtain high-purity C6～C10Aromatic hydrocarbon component and high-purity non-aromatic hydrocarbon component. The adsorption columns of the simulated moving bed are connected end to end side by side through a multi-position valve and are connected through a circulating pump to form a closed loop, the flow of the four regions is periodically regulated and controlled through program switching of the multi-position valve, so that the adsorbent bed layers move relatively, the desorption agent can be separated, recovered and recycled by utilizing the rectifying tower, and finally aromatic hydrocarbon and non-aromatic hydrocarbon are obtained. The invention adsorbs and separates mixed aromatic hydrocarbon under the non-hydrogen low-pressure low-temperature mild process condition, the device has low operation energy consumption, the separation purity of aromatic hydrocarbon and non-aromatic hydrocarbon is high, the aromatic hydrocarbon content of aromatic hydrocarbon component reaches more than 99%, and the non-aromatic hydrocarbon content of non-aromatic hydrocarbon component reaches more than 99%.
Description
Technical Field
The invention relates to the technical field of mixed aromatic hydrocarbon purification, and particularly relates to C6～C10A method for purifying mixed aromatic hydrocarbon.
Background
C6～C10The mixed aromatic hydrocarbon is mainly from reformed oil in a catalytic reforming device of a refinery and pyrolysis gasoline which is a byproduct of an ethylene device; separation of high purity C from mixed aromatics by separation techniques6～C10Aromatic hydrocarbon component and non-aromatic component, the aromatic hydrocarbon component is fractionated to produce benzene, toluene, mixed xylene and C9C10The aromatic hydrocarbon product not only provides high-quality raw materials for PX devices and reactions such as toluene disproportionation and alkylation, but also can realize the maximization of the operating benefit of the aromatic hydrocarbon combination device; the separated non-aromatic components are not only high-quality raw materials for ethylene cracking and reduce the load of a device, but also can be directly sold as an organic solvent after being fractionated.
At present, the method for purifying mixed aromatic hydrocarbon mainly takes an aromatic hydrocarbon extraction technology and an adsorption separation technology as main materials, and although the purpose of purifying aromatic hydrocarbon can be realized, the problems of high solvent regeneration energy consumption, large solvent ratio, high operation cost, low aromatic hydrocarbon yield in extract liquid, high aromatic hydrocarbon content in raffinate oil and the like exist; by adopting the traditional aromatic hydrocarbon extraction technology, a large amount of non-aromatic hydrocarbon resources in the mixed aromatic hydrocarbon cannot be utilized, and resource waste is caused. The prior adsorption separation technology has the problems of low purity of aromatic hydrocarbon component and non-aromatic hydrocarbon component products, large consumption of a desorbent, low yield of a target product and the like.
CN106281448A discloses an optimized combined production method of aromatic hydrocarbon, alkane and solvent oil. The method can selectively hydrogenate the pyrolysis gasoline or the reformate through full fraction to remove C in the material6～C10One or more of the components are subjected to liquid-liquid extraction of aromatic hydrocarbon, and then raffinate oil obtained after the extraction of the aromatic hydrocarbon is subjected to hydrogenation and then fractionation to obtain the aromatic hydrocarbon, alkane and solvent oil. The method solves the problems of single processing route of the pyrolysis gasoline and the reformed oil, low added value of products, slight profit of fuel oil markets and the like.
CN1258717 discloses a process for extracting mixed aromatics, the raw material is a hydrocarbon mixture with 20-90 wt% of aromatics, less than 2ppm of sulfur and composition of carbon five to carbon eleven, the raw material is directly subjected to aromatics extraction to separate non-aromatics and mixed aromatics, and the mixed aromatics are further refined and rectified to obtain an aromatics product. Compared with the prior art, the invention has the advantages of reducing the solvent ratio, improving the processing capacity by 10-20 percent, greatly reducing the engineering investment and the operation cost and recovering 30-70 percent of C9An aromatic hydrocarbon.
CN104073285A discloses a method for separating aromatic hydrocarbons in diesel oil by liquid-liquid extraction, which comprises introducing the diesel oil from the middle part of a liquid-liquid extraction tower, introducing a first extraction solvent from the upper part of the liquid-liquid extraction tower, introducing a second extraction solvent from the upper part of the liquid-liquid extraction tower at a position lower than the introduction point of the first extraction solvent, wherein the main solvents in the first extraction solvent and the second extraction solvent are both selected from N, N-dimethylformamide, ethylene glycol monomethyl ether, furfural or morpholine. The method can reduce solvent ratio, overcome the problem of mixing and dissolving of the solvent and the raw materials, improve alkane separation efficiency, and obtain diesel oil products with high cetane number and aromatic hydrocarbons with low alkane content.
CN106244225A discloses a simulated moving bed adsorption separation method for realizing high-efficiency separation of heavy aromatics, wherein a plurality of adsorption beds are arranged in an adsorption tower of the simulated moving bed, each adsorption bed is provided with a material inlet and outlet pipeline, and the adsorption, purification and desorption steps of C9+ heavy aromatics are realized by changing the adsorption beds where different materials enter or are extracted, so as to obtain a component containing high-purity C9+ aromatics, wherein the purity of the C9+ aromatics component is 93.2%, and the purity of the non-aromatics component is 88.8%. The method has the advantages of continuity, high precision, stable operation, low energy consumption and the like. However, the method has the problems of low purity of aromatic hydrocarbon components and non-aromatic hydrocarbon components of the product, low yield of target products and the like.
The existing method for purifying mixed aromatic hydrocarbon mainly takes an aromatic hydrocarbon extraction technology and an adsorption separation technology as main materials, and the aromatic hydrocarbon extraction technology has the problems of high solvent regeneration energy consumption, large solvent ratio, high operation cost, low aromatic hydrocarbon yield of extract liquid, high aromatic hydrocarbon content of raffinate oil, low utilization rate of aromatic hydrocarbon and non-aromatic hydrocarbon and the like. The adsorption separation technology has the problems of low purity of aromatic hydrocarbon components and non-aromatic hydrocarbon components of products, low yield, large dosage of the desorbent and the like.
Disclosure of Invention
The invention aims to overcome the defects of the prior art and provides a C6～C10The method for purifying the mixed aromatic hydrocarbon can effectively adsorb and separate the aromatic hydrocarbon and the non-aromatic hydrocarbon.
The invention provides a compound C6～C10A process for the purification of mixed aromatics comprising the steps of:
c is to be6～C10The method comprises the following steps that a mixed aromatic hydrocarbon raw material enters a simulated moving bed adsorption device, adsorption columns of the simulated moving bed are connected end to end side by side through multi-position valves and are connected through a circulating pump to form a closed loop, the device is divided into four areas, an adsorption I area, an isolation IV area, a desorption III area and a refining II area are sequentially arranged along the material flowing direction, and at least 2 adsorption columns are distributed in each area; periodically regulating and controlling the flow of the four areas by program switching of a multi-position valve, wherein the adsorption I area adopts an aromatic hydrocarbon adsorbent for adsorbing C6～C10Aromatic hydrocarbon to obtain non-aromatic hydrocarbon component, and the reflux ratio of the isolated IV region is negative to play a role in isolating and absorbingThe purpose of the adsorption I area and the desorption III area is that the desorption III area obtains aromatic hydrocarbon components through the regeneration of a desorbent, and the refining II area has the refining and purifying function on non-aromatic hydrocarbon;
each adsorption column of the simulated moving bed device is provided with a multi-position valve, and the multi-position valve comprises four feeding and discharging pipelines and a program control valve and correspondingly comprises a mixed aromatic hydrocarbon raw material AB, a desorbent D, an extract AD and a raffinate BD; the continuous adsorption-regeneration process of the simulated moving bed can be realized by periodically switching material valves, and the separated product is rectified to recover the desorbent, so that aromatic hydrocarbon and non-aromatic hydrocarbon are finally obtained;
the aromatic hydrocarbon adsorbent is made of a metal modified composite mesoporous silica material, and the modified metal is one or more of alkali metal, alkaline earth metal or transition metal, and the content of the modified metal is 0.5-10 wt%;
the composite mesoporous silica material is preferably two of silica gel, MCM-41, MCM-48, SBA-3 and SBA-15 all-silicon mesoporous molecular sieves; the modified metal is preferably one or more of K, Rb, Cs, Mg, Sr, Ba, Cu, Zn, Ag and Cd, and the content is preferably 0.5-3.0 wt%;
wherein the desorbent is n-dodecane, product C10One or more of aromatic hydrocarbon, tetrahydronaphthalene, methylnaphthalene and long-chain alkylbenzene; the preferred desorbent is one or more of n-dodecane, methylnaphthalene and long-chain alkylbenzene.
The invention described for C6～C10The method for purifying the mixed aromatic hydrocarbon comprises the steps of continuously adsorbing and separating by a simulated moving bed, preferably switching for 100-250 s, controlling the temperature of an adsorbent bed layer to be 40-80 ℃, controlling the adsorption pressure to be 0.5-2.5 MPa, controlling the mass flow rate ratio of a raw material to a desorbent to be 1: 1-1: 1.5, and controlling the volume flow rate ratio of the raw material to a circulating volume to be 1: 2.5-1: 3.5.
Compared with the existing aromatic extraction technology and adsorption separation technology, the process has the following advantages:
1) the invention adopts a high-efficiency environment-friendly simulated moving bed process, and can adsorb and separate C6～C10Mixing aromatic hydrocarbons and non-aromatic hydrocarbons in aromatic hydrocarbons;
2) the method of the invention is notHydrogen to C at low pressure and low temperature6～C10Aromatic hydrocarbons and non-aromatic hydrocarbons in the mixed aromatic hydrocarbons are separated, and the process is a multi-tower series process, so that the method has the characteristics of environmental protection, no pollution, mild reaction conditions, low investment, low energy consumption, easy control and the like;
3) the method realizes the high-efficiency separation of aromatic hydrocarbon and non-aromatic hydrocarbon with lower cost and simple process, wherein the aromatic hydrocarbon content in the aromatic hydrocarbon component is more than 99 percent, and the non-aromatic hydrocarbon content in the non-aromatic component is more than 99 percent;
4) the high-purity aromatic hydrocarbon component separated by the method of the invention is fractionated to produce benzene, toluene, mixed xylene and C9And C10The aromatic hydrocarbon product not only provides high-quality raw materials for PX devices and reactions such as toluene disproportionation and alkylation, but also can realize the maximization of the operating benefit of the aromatic hydrocarbon combination device; the separated high-purity non-aromatic components can be used as high-quality raw materials for ethylene cracking, reduce the load of a device, and can also be directly sold as an organic solvent after being fractionated.
Drawings
FIG. 1 is a schematic diagram of a 20-column simulated moving bed adsorption separation unit;
in the figure: Z1-Z20 are adsorption columns; V1-V20 are multi-position valves, and RP is a circulating pump;
FIG. 2 is a schematic diagram of the operation of a multi-position valve in a simulated moving bed adsorptive separation apparatus;
in the figure: the numbers 1 to 8 represent 8 valves of the multi-position valve, wherein the even numbered valves 2, 4, 6 and 8 are dead-plugged; the No. 1 valve is a BD pipeline of raffinate non-aromatic components; the No. 3 valve is a mixed aromatic AB pipeline with the raw materials of C6-C10; the No. 5 valve is an extract aromatic hydrocarbon component AD pipeline; the No. 7 valve is a desorbent D pipeline; the valve inlet and the valve outlet are in a normally open serial state, and the continuous adsorption-regeneration process is realized by periodically switching the valves.
Detailed Description
The technical solution of the present invention is further explained by the following embodiments and the accompanying drawings.
Invention C6～C10Process for the purification of mixed aromatics, wherein C6～C10Mixed aromatic crudeThe material AB and the desorbent D enter simulated moving bed adsorption columns Z1-Z20 by utilizing No. 3 and No. 7 in a multi-position valve, the adsorption columns are connected end to end side by side through the multi-position valves V1-V20 and are connected by a circulating pump RP to form a closed loop, raffinate BD and extract AD are extracted by utilizing No. 1 and No. 5 in the multi-position valve, the device is divided into four areas which are an adsorption I area, an isolation IV area, a desorption III area and a refining II area in sequence along the material flowing direction, and at least 2 adsorption columns are distributed in each area; periodically regulating and controlling the flow of the four areas by program switching of a multi-position valve, wherein the adsorption I area adopts an aromatic hydrocarbon adsorbent for adsorbing C6～C10Aromatic hydrocarbon to obtain non-aromatic hydrocarbon components, keeping the reflux ratio of the isolated IV region negative, isolating and adsorbing the I region and the desorption III region, regenerating the desorption III region by a desorbent to obtain aromatic hydrocarbon components, and purifying the non-aromatic hydrocarbon by the refined II region;
each adsorption column of the simulated moving bed device is provided with a multi-position valve, and the multi-position valve comprises four feeding and discharging pipelines and a program control valve and correspondingly comprises a mixed aromatic hydrocarbon raw material AB, a desorbent D, an extract AD and a raffinate BD; the continuous adsorption-regeneration process of the simulated moving bed can be realized by periodically switching material valves, and the separated product is rectified to recover the desorbent, so that aromatic hydrocarbon and non-aromatic hydrocarbon are finally obtained.
The arene adsorbent adopts a metal modified composite mesoporous silica material, and the composite mesoporous silica material adopts two of silica gel, MCM-41, MCM-48, SBA-3 and SBA-15 all-silicon mesoporous molecular sieves; the modified metal is one or more of K, Rb, Cs, Mg, Sr, Ba, Cu, Zn, Ag and Cd;
c according to the invention6～C10The process for purifying mixed aromatics belongs to the simulated moving bed process and is operated according to the conditional method of the present invention, and the following examples will further illustrate the present invention.
C used in the examples6～C10The composition of the mixed aromatics feed is shown in Table 1, and the simulated moving bed process conditions are shown in Table 2.
C6～C10Yield of aromatic hydrocarbon as product C6～C10Aromatic Mass/feed C6～C10Aromatic hydrocarbons by mass x 100%
Aromatic hydrocarbon component aromatic hydrocarbon content ═ aromatic hydrocarbon component aromatic hydrocarbon mass/total aromatic hydrocarbon component mass x 100%
The non-aromatic content of the non-aromatic component is equal to the non-aromatic mass of the non-aromatic component/the total mass of the non-aromatic component multiplied by 100 percent
Example 1
(1) The aromatic hydrocarbon adsorbent is made of metal modified composite mesoporous silica material, and the modified metal is K, Mg and Cu, wherein K is2The content of O is 1.0 wt%, the content of MgO is 0.5 wt%, and the content of CuO is 0.5 wt%; the composite mesoporous silica material is silica gel and MCM-41 (mass ratio is 1: 1), and the specific surface area is 600m2A g, an average pore diameter of 3.0 to 5.0nm, SiO2The content is more than or equal to 95 wt%, and Na2The content of O is less than or equal to 0.5 wt%; the desorbent used was 20 wt% n-dodecane to 80 wt% methylnaphthalene.
(2) Raw material C6～C10The mass flow rate ratio of the mixed aromatic hydrocarbon to the desorbent is 1:1, and the raw material C6～C10The volume flow rate ratio of the mixed aromatic hydrocarbon to the circulating amount is 1: 2.5.
(3) The aromatic hydrocarbon component and the non-aromatic hydrocarbon component containing the desorbent are obtained by the adsorption separation of the simulated moving bed, and the desorbent can be separated and recovered by utilizing the rectifying tower due to the large difference of the boiling points of the desorbent, the aromatic hydrocarbon component and the non-aromatic hydrocarbon component.
(4) Raw material C6～C10The analysis of the composition of the mixed aromatics is shown in table 1 for # hydrocracking gasoline, the process conditions for adsorption separation by a simulated moving bed are shown in table 2, and the evaluation results are shown in table 3.
Example 2
(1) The aromatic hydrocarbon adsorbent is a metal modified composite mesoporous silica material, and the modified metal is Rb, Sr and Zn, wherein the Rb is Rb2The content of O is 1.0 wt%, the content of SrO is 0.5 wt%, and the content of ZnO is 0.5 wt%; the composite mesoporous silica material is silica gel and SBA-15 (the mass ratio is 1: 1), and the specific surface area is 650m2Per g, average pore diameter of 2.5-5.0 nm, SiO2The content is more than or equal to 95 wt%, and Na2The content of O is less than or equal to 0.5 wt%; the desorbent used was 30 wt% n-dodecane to 70 wt% methylnaphthalene.
(2) Raw material C6～C10The mass flow rate ratio of the mixed aromatic hydrocarbon to the desorbent is 1:1.2, and the raw material C6～C10The volume flow rate ratio of the mixed aromatic hydrocarbon to the circulating amount is 1: 2.8.
(3) Raw material C6～C10The analysis of the composition of the mixed aromatics is shown in table 1 for # hydrocracking gasoline, the process conditions for adsorption separation by a simulated moving bed are shown in table 2, and the evaluation results are shown in table 3.
Example 3
(1) The arene adsorbent is a metal modified composite mesoporous silica material, and the modified metals are Cs, Ba and Ag, wherein Cs is21.0 wt% of O, 0.5 wt% of BaO, and Ag2The content of O is 0.5 wt%; the composite mesoporous silica material is silica gel and MCM-48 (mass ratio is 1: 1), and the specific surface area is 620m2A g, an average pore diameter of 3.0 to 5.0nm, SiO2The content is more than or equal to 95 wt%, and Na2The content of O is less than or equal to 0.5 wt%; the desorbent used was 50% n-dodecane-50% methylnaphthalene.
(2) Raw material C6～C10The mass flow rate ratio of the mixed aromatic hydrocarbon to the desorbent is 1:1.3, and the raw material C6～C10The volumetric flow rate ratio of the mixed aromatics to the recycle was 1:3.
(3) Raw material C6～C10The analysis of the composition of the mixed aromatics is shown in table 1 for # hydrocracking gasoline, the process conditions for adsorption separation by a simulated moving bed are shown in table 2, and the evaluation results are shown in table 3.
Example 4
(1) The aromatic hydrocarbon adsorbent is a metal modified composite mesoporous silica material, and the modified metal is K, Mg and Cd, wherein K is2O content of 1.0 wt%, MgO content of 0.5 wt%, and Cd2O3Is 0.5 wt%; the composite mesoporous silica material is silica gel and SBA-3 (mass ratio is 1: 1), and the specific surface area is 720m2Per g, average pore diameter of 2.8-4.5 nm, SiO2The content is more than or equal to 95 wt%, and Na2The content of O is less than or equal to 0.5 wt%; the desorbent used was 30% n-dodecane-70% long chain alkylbenzene.
(2) Raw material C6～C10The mass flow rate ratio of the mixed aromatic hydrocarbon to the desorbent is 11.4, raw material C6～C10The volume flow rate ratio of the mixed aromatic hydrocarbon to the circulating amount is 1: 3.2.
(3) Raw material C6～C10The analysis of the composition of mixed aromatics is shown in Table 1 for # 2 reformate, the process conditions for simulated moving bed adsorptive separation are shown in Table 2, and the evaluation results are shown in Table 3.
Example 5
(1) The aromatic hydrocarbon adsorbent is made of a metal modified composite mesoporous silica material, and the modified metal is the same as that in the embodiment 3; the composite mesoporous silica material is the same as the embodiment 3; the desorbent used was 50 wt% n-dodecane to 50 wt% long chain alkylbenzene.
(2) Raw material C6～C10The mass flow rate ratio of the mixed aromatic hydrocarbon to the desorbent is 1:1.5, and the raw material C6～C10The volume flow rate ratio of the mixed aromatic hydrocarbon to the circulating amount is 1: 3.5.
(3) Raw material C6～C10The analysis of the composition of mixed aromatics is shown in Table 1 for # 2 reformate, the process conditions for simulated moving bed adsorptive separation are shown in Table 2, and the evaluation results are shown in Table 3.
TABLE 1C6～C10Mixed aromatic feedstock
TABLE 2 simulated moving bed adsorptive separation process conditions
Table 3 evaluation results
| Examples | 1 | 2 | 3 | 4 | 5 |
| C6～C10Yield of aromatic hydrocarbons | 72.26 | 72.08 | 71.96 | 82.90 | 82.71 |
| Aromatic component aromatic content | 99.19 | 99.32 | 99.95 | 99.11 | 99.92 |
| Non-aromatic content of non-aromatic component | 99.27 | 99.16 | 99.01 | 99.31 | 99.42 |
Claims (10)
1. C6～C10The method for purifying the mixed aromatic hydrocarbon is characterized by comprising the following steps: comprises the following steps:
c is to be6～C10The mixed aromatic hydrocarbon enters a simulated moving bed adsorption device, adsorption columns of the simulated moving bed are connected end to end side by side through a multi-position valve and are connected through a circulating pump to form a closed loop, the device is divided into four areas, an adsorption I area, an isolation IV area, a desorption III area and a refining II area are sequentially arranged along the material flowing direction, and at least 2 adsorption columns are distributed in each area; periodically regulating and controlling the flow of the four areas by program switching of a multi-position valve, wherein an aromatic hydrocarbon adsorbent is adopted in an adsorption I area for adsorbing C6～C10Aromatic hydrocarbon to obtain non-aromatic hydrocarbon components, keeping the reflux ratio of the isolated IV region negative, isolating and adsorbing the I region and the desorption III region, regenerating the desorption III region by a desorbent to obtain aromatic hydrocarbon components, and refining and purifying the non-aromatic hydrocarbon in the refining II region;
each adsorption column of the simulated moving bed device is provided with a multi-position valve, and the multi-position valve comprises four feeding and discharging pipelines which are correspondingly a raw material AB, a desorbent D, an extract AD and a raffinate BD; periodically switching material valves of all strands to realize a continuous adsorption-regeneration process of the simulated moving bed, rectifying and recovering a desorbent from a separation product, and finally obtaining an aromatic hydrocarbon component and a non-aromatic hydrocarbon component;
the aromatic hydrocarbon adsorbent is made of a metal modified composite mesoporous silica material, and the modified metal is one or more of alkali metal, alkaline earth metal or transition metal, and the content of the modified metal is 0.5-10 wt%;
the desorbent is n-dodecane and a product C10One or more of aromatic hydrocarbon, tetrahydronaphthalene, methylnaphthalene and long-chain alkylbenzene.
2. The method according to claim 1, wherein the periodic switching valve realizes continuous adsorption separation of the simulated moving bed, and the switching time is 50-1000 s.
3. The method of claim 1, wherein the temperature of the adsorbent bed is 20 to 180 ℃ and the adsorption pressure is 0.1 to 5.0 MPa.
4. The method according to claim 1, wherein the mass flow rate ratio of the raw material to the desorbent is 1: 1-1: 4; the volume flow rate ratio of the raw materials to the circulating amount is 1: 2-1: 5.
5. The method according to claim 2, wherein the periodic switching valve realizes continuous adsorption separation of the simulated moving bed, and the switching time is 100-250 s.
6. The method of claim 3, wherein the temperature of the adsorbent bed is 40 to 80 ℃ and the adsorption pressure is 0.5 to 2.5 MPa.
7. The method according to claim 4, wherein the mass flow rate ratio of the raw material to the desorbent is 1: 1-1: 1.5; the volume flow rate ratio of the raw materials to the circulating amount is 1: 2.5-1: 3.5.
8. The method according to claim 1, wherein the composite mesoporous silica material is two of silica gel, MCM-41, MCM-48, SBA-3, and SBA-15 all-silicon mesoporous molecular sieves.
9. The method according to claim 1, wherein the modified metal is one or more of K, Rb, Cs, Mg, Sr, Ba, Cu, Zn, Ag and Cd; the content is 0.5 to 3.0 wt%.
10. The method of claim 1, wherein the desorbent is one or more of n-dodecane, methylnaphthalene and a long chain alkylbenzene.
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| CN114836235A (en) * | 2022-05-09 | 2022-08-02 | 中海油天津化工研究设计院有限公司 | Method for separating aromatic hydrocarbon by coupling distillate oil adsorption and rectification |
| CN114874065A (en) * | 2022-05-07 | 2022-08-09 | 中海油天津化工研究设计院有限公司 | Method for separating paraxylene and ethylbenzene by sequential simulated moving chromatography |
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| CN110938465A (en) * | 2019-11-19 | 2020-03-31 | 中海油天津化工研究设计院有限公司 | Method for multi-component adsorption separation of gasoline |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN114874065A (en) * | 2022-05-07 | 2022-08-09 | 中海油天津化工研究设计院有限公司 | Method for separating paraxylene and ethylbenzene by sequential simulated moving chromatography |
| CN114874065B (en) * | 2022-05-07 | 2023-09-15 | 中海油天津化工研究设计院有限公司 | Method for separating paraxylene and ethylbenzene by sequential analog mobile chromatography |
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| CN114836235B (en) * | 2022-05-09 | 2023-11-07 | 中海油天津化工研究设计院有限公司 | Method for separating aromatic hydrocarbon by adsorption and rectification coupling of distillate oil |
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