CN109423332B - Separation system and separation method for continuously separating petroleum group components - Google Patents
Separation system and separation method for continuously separating petroleum group components Download PDFInfo
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- CN109423332B CN109423332B CN201710778480.8A CN201710778480A CN109423332B CN 109423332 B CN109423332 B CN 109423332B CN 201710778480 A CN201710778480 A CN 201710778480A CN 109423332 B CN109423332 B CN 109423332B
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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
- C10G53/08—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more refining processes plural serial stages only including at least one sorption 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
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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
- C10G2300/20—Characteristics of the feedstock or the products
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Abstract
The invention discloses a separation system for continuously separating petroleum group components and a separation method thereof. An outlet at the top of a first adsorption tower of the separation system is sequentially connected with a first evaporator and a rectifying tower, and an outlet at the bottom of the first adsorption tower is connected with a material inlet at the lower part of a second adsorption tower; the outlet at the top of the second adsorption tower is sequentially connected with a second evaporator and a rectifying tower; the bottom outlet of the second adsorption tower is connected with a third evaporator, an extractor and a rectifying tower in sequence; the third evaporator is provided with an inlet of a third solvent, and the extractor is provided with an inlet of a fourth solvent; the top outlet of the rectifying tower is connected with the first solvent inlet at the upper part of the first adsorption tower; and the bottom outlet of the rectifying tower is connected with a second material inlet at the lower part of the second adsorption tower and a second solvent inlet at the upper part of the second adsorption tower. The system continuously separates the group components of the crude oil sample with large amount, high purity and low solvent consumption, realizes the recycling of the solvent, and can continuously separate a plurality of samples without a pretreatment step.
Description
Technical Field
The invention relates to a separation system for continuously separating petroleum group components and a separation method thereof.
Background
The petroleum mainly comprises four components of saturated components, aromatic components, colloid and asphaltene. Saturates in petroleum include saturated hydrocarbons such as normal, iso and cyclo-paraffins; the aromatic component comprises aromatic hydrocarbon, polycyclic aromatic hydrocarbon and the like; the gum definition is fuzzy and generally refers to the dark gum mixture containing sulfur, nitrogen and oxygen with higher molecular weight in crude oil; asphaltenes make the viscous heavy components of crude oil, usually insoluble, composed of high molecular weight polycyclic compounds.
Each component in petroleum has a unique molecule, chemical structure and property, and two kinds of crude oil can have distinct quality and effect, so that the analysis and calibration of family components in the crude oil are very important. The crude oil family components are characterized and separated, so that the process optimization can be carried out by combining the properties of crude oil and market demands in refineries, chemical plants and the like, and particularly, the analysis result of the family components can guide the design of a subsequent hydrogenation process aiming at the current crude oil with serious weight. For example, the colloids and asphaltenes in crude oil contain various heteroatoms, such as nitrogen, nickel, vanadium, etc., and if the colloids and asphaltenes cannot be separated and the compositions of the colloids and asphaltenes can be further determined, the subsequent hydrogenation and conversion treatment processes cannot be designed or improved, and the yield and the product quality of the whole refining process are influenced.
The conventional petroleum group component determination method needs to adopt n-heptane, toluene, ethanol and chromatographic columns for dissolution, filtration and adsorption, and comprises the following specific steps: and (3) precipitating the asphaltene from the sample by using n-heptane, filtering, refluxing by using n-heptane to remove the soluble components in the precipitate, and refluxing and dissolving the precipitate by using toluene to obtain the asphaltene. Adsorbing the deasphalted part on an alumina chromatographic column, developing with n-heptane (petroleum ether), toluene and toluene-ethanol in sequence, and washing out the alumina chromatographic column to obtain saturated component, aromatic component and colloid in sequence below the alumina chromatographic column, wherein the specific flow is shown in FIG. 1.
However, the above method has the following problems:
(1) usually, 50-100 g of solvent is needed to treat 1g of oil product sample in each dissolving process, and a large amount of manual operation is needed in the process, so that the content of four group components can only be measured, and the four group components cannot be separated and prepared in a large amount. In the crude oil characterization process, experiments such as BMCI value characterization, distillation range determination, determination of aromatic potential value and the like are generally needed for light saturated components and aromatic components in the crude oil; for asphaltenes with complex compositions, in order to convert impurity components in the asphaltenes, the characteristics of aromatic ring composition distribution and macromolecular hydrocarbon structure distribution of polycyclic aromatic hydrocarbons in the asphaltenes need to be accurately measured. The calibration process needs a large amount of group component samples, usually needs more than 100-500 g of raw materials, and is 100-500 times of the solvent preparation amount of the conventional separation method. Therefore, if the samples are eluted and prepared by a conventional method, a large amount of solvent is needed, and meanwhile, experimental operation needs hundreds of hours, so that the method is extremely high in danger and extremely low in reliability;
(2) the residual solvents of ethanol and toluene in the last test can influence the solubility of the components such as saturated components, aromatic components and colloid in the n-heptane at the next time, and the ethanol enters the saturated components and the aromatic components after separation, and the toluene enters the saturated components and the like, so that the content of the final components is inaccurate to measure. Therefore, the conventional method requires the column to be newly prepared before the next measurement. However, the existing analysis method needs to use 40g of chromatographic packing for testing 1g of oil sample, if more than 100-500 g of raw materials are required to be treated, 100-500 times of packing is usually needed, a large amount of packing causes very expensive testing cost, and a large amount of solvent and hundreds of hours are needed for operation, so that the existing analysis method is difficult to extract more than 100-500 g of group component samples with low cost and high efficiency;
(3) if the column is repeatedly used, a miscible system of n-heptane-ethanol sample, even n-heptane-toluene-ethanol sample, can occur; in the existing analysis method, multiple solvents are eluted successively in the process of separating saturated components, aromatic components and colloid, the separated components can generate miscible solvents in multiple forms, and mixed solvents such as toluene-ethanol and the like are also used, but the existing solvent recovery method is difficult to separate the miscible solvents in multiple forms at high purity, so that the used solvents cannot be recycled, the waste of the solvents is caused, and the cost is high;
(4) the use of multiple solvents also allows for miscibility of saturated and aromatic components.
Therefore, the existing analysis method, repeated use of chromatographic columns and solvent recycling have a mutual conflict relationship, so that the existing analysis method is difficult to extract group component samples with low cost and high efficiency of more than 100-500 g.
For example, CN102527088A discloses a pressure-reducing asphalt four-component separation device, which is formed by connecting a glass adsorption column, a round-bottom flask and a pressure-reducing control device, and is characterized in that the glass adsorption column is provided with a vacuum-pumping device, and an air-pumping hole on the glass adsorption column is sequentially connected with pressure-reducing and flow-dividing control elements such as a vacuum gauge, a protection bottle, a vacuum three-way valve, a four-port flow-dividing valve and a vacuum pump; the lower end is connected with a round-bottom flask to collect components. However, although this analysis and measurement method can semi-automatically measure the contents of four components, the sample mass is only 1g or less, and cannot satisfy the basic mass required for further characterizing the structure of each organic substance in the asphaltene.
CN 101644698A provides a chromatographic analysis method for four family components of crude oil, which can determine the content of the family components in the crude oil by solvent dissolution and chromatographic analysis, but lacks continuous preparation equipment and separation equipment, and cannot process crude oil samples of more than 10g and separate to obtain each family component.
CN 204188437U provides a device for separating soluble organic matters in rocks and organic solvents in crude oil family components. The device can evaporate the solvent through the water bath and the evaporation panel which are connected in series, and the residual group components are used as products. The method only solves the problem of slow solvent volatilization speed in the process of purifying the colloid and the asphaltene, but can not separately add a plurality of solvents to separate different groups of components; in addition, because the solvent volatilization process is not provided with a recycling device, the problems of safety and environmental protection of solvent volatilization cannot be guaranteed when a large number of samples are prepared.
CN 101070495B introduces a mild coal group component separation method based on extraction and back extraction, which is characterized in that the series use of multiple extraction, back extraction, distillation and washing processes is adopted. However, the method is suitable for separating coal such as raw coal and the like, and due to the existence of an extraction method, two solvents are required to be used at the same time, when petroleum is processed, the use of multiple solvents enables the saturated component and the aromatic component to be mixed and dissolved, and the colloid is dissolved in the two solvents to different degrees, so that the measurement result of the mass composition of the separated saturated component and the separated aromatic component is seriously deviated from the actual measurement result, and the method cannot be used for separating and measuring petroleum components.
At present, no method for separating crude oil family components, which has the advantages of low solvent consumption, safety, rapidness and reusable chromatographic column, is reported.
Disclosure of Invention
In view of the shortcomings of the prior art, the present invention provides a separation system for continuously separating petroleum group components and a separation method thereof. The system continuously separates group components of crude oil samples with large quantity, high purity and low solvent consumption, realizes continuous operation, automatic production and recycling of solvent, and can immediately separate the next sample after completing the separation of one sample without pretreatment steps (washing, replacing an adsorption tower and the like).
The invention provides a separation system for continuously separating petroleum group components, which comprises a first adsorption tower, a second adsorption tower, a first evaporator, a second evaporator, a third evaporator, an extractor and a rectifying tower, wherein the first evaporator is connected with the second evaporator;
the first adsorption tower is used for adsorbing and desorbing aromatic components and colloid, a first unadsorbed substance outlet at the top of the first adsorption tower is sequentially connected with the first evaporator and the rectifying tower, and a first desorbed substance outlet at the bottom of the first adsorption tower is connected with a material inlet at the lower part of the second adsorption tower; preferably, the first unadsorbed substance outlet at the top of the first adsorption tower is connected with the inlet of the first evaporator, and the first evaporated solvent outlet of the first evaporator is connected with the inlet of the rectification tower;
the second adsorption tower is used for adsorbing and desorbing the colloid, a second unadsorbed substance outlet at the top of the second adsorption tower is sequentially connected with the second evaporator and the rectifying tower, preferably, the second unadsorbed substance outlet at the top of the second adsorption tower is connected with an inlet of the second evaporator, and a second evaporation solvent outlet of the second evaporator is connected with the rectifying tower;
a second desorbed substance outlet at the bottom of the second adsorption tower is sequentially connected with a third evaporator, an extractor and a rectifying tower, preferably, the second desorbed substance outlet at the bottom of the second adsorption tower is connected with an inlet of the third evaporator, a third evaporation outlet of the third evaporator is connected with an inlet of the extractor, and a top solution outlet of the extractor is connected with the rectifying tower;
the third evaporator is provided with an inlet of a third solvent, and the extractor is provided with an inlet of a fourth solvent;
the top outlet of the rectifying tower is connected with the first solvent inlet at the upper part of the first adsorption tower; and the bottom outlet of the rectifying tower is connected with a second material inlet at the lower part of the second adsorption tower and a second solvent inlet at the upper part of the second adsorption tower.
The separation system further comprises a first elutriator and a second elutriator;
the first elution device is used for dissolving and extracting soluble substances of the petroleum raw materials and separating insoluble substances through a first solvent, a first elution solution outlet of the first elution device is connected with a material inlet of the first adsorption tower, and an insoluble substance outlet of the first elution device is connected with an inlet of the second elution device; preferably, the inlet of the first elution device is connected to a petroleum feedstock supply line;
and the second elution device is used for dissolving the asphaltene in the insoluble substances through a second solvent and separating the solution dissolved with the asphaltene, and preferably, an asphaltene outlet of the second elution device is connected with an asphaltene collection device.
The first elution device is provided with a first mixed dissolving unit, a first solid-liquid separation unit and a first heating unit, an outlet of the first mixed dissolving unit is connected with an inlet of the first solid-liquid separation unit, a liquid outlet of the first solid-liquid separation unit is connected with an inlet of the first adsorption tower, and a solid phase outlet is connected with an inlet of the second elution device; the first heating unit is used for heating the first dissolving kettle and the first rotary drum filter; preferably, the first mixed dissolving unit comprises a first dissolving tank, and the first solid-liquid separation unit comprises a first rotary drum filter;
the second elution apparatus is provided with a second mixing and dissolving unit, a second solid-liquid separation unit and a second heating unit, wherein an outlet of the second mixing and dissolving unit is connected with an inlet of the second solid-liquid separation unit, the second mixing and dissolving unit preferably comprises a second dissolving kettle, the second solid-liquid separation unit preferably comprises a second rotary drum filter, and the second heating unit is used for heating the second dissolving kettle and the second rotary drum filter.
A circulating pipeline is connected between the inlet of the first solid-liquid separation unit and the liquid outlet of the first solid-liquid separation unit, and a valve body is arranged on the circulating pipeline.
The top outlet of the rectifying tower is also connected with the inlet of the first elution device; the outlet at the bottom of the rectifying tower is also connected with the inlet of the second elution device.
The first elution device is provided with a first evaporation unit, an inlet of the first evaporation unit is connected with a liquid outlet of the first solid-liquid separation unit, and a vapor phase outlet of the first evaporation unit is connected with an inlet of the rectifying tower;
the second elution device is provided with a second evaporation unit, an inlet of the second evaporation unit is connected with a liquid outlet of the second solid-liquid separation unit, and a vapor gas phase outlet of the second evaporation unit is connected with an inlet of the rectifying tower.
The first evaporator is an evaporator for evaporating the first solvent, the second evaporator is an evaporator for evaporating the first solvent and the second solvent, and the third evaporator is an evaporator for evaporating the second solvent and the third solvent; preferably, the evaporation residue outlet at the bottom of the first evaporator is connected with the saturation fraction collecting device, the evaporation residue outlet at the bottom of the second evaporator is connected with the fragrance fraction collecting device, and the evaporation residue outlet at the bottom of the third evaporator is connected with the colloid collecting device, and further preferably, the first evaporator, the second evaporator and the third evaporator adopt a single-effect or multi-effect falling-film evaporator.
The extractor is used for separating the second solvent and the third solvent through extraction, preferably, a bottom solution outlet of the extractor is connected with a waste solvent collecting device, and further preferably, the extractor adopts a packing type extractor, a rotating disc type extractor or a centrifugal extractor.
The first solvent comprises one of n-heptane, n-hexane and petroleum ether; the second solvent comprises one of toluene and benzene; the third solvent comprises one of ethanol, methanol and propanol; the fourth solvent is water.
The first adsorption tower and the second adsorption tower are filler adsorption towers, wherein one or more of alumina, 5A molecular sieve, silica gel, macroporous adsorption resin and ion exchange resin are filled in the towers, preferably, the first adsorption tower is filled with macroporous adsorption resin, 5A molecular sieve and alumina filler, and the second adsorption tower is filled with macroporous adsorption resin, 5A molecular sieve and silica gel filler.
The rectifying tower is used for continuously rectifying two components of the first solvent and the second solvent, preferably, the rectifying tower adopts a multi-section rectifying tower, the top outlet of the rectifying tower is a discharge port of the first solvent with a low boiling point, the bottom outlet of the rectifying tower is a discharge port of the second solvent with a high boiling point, and further preferably, a side line of the rectifying tower is provided with a discharge port of the impurity solvent.
The invention provides a separation system for continuously separating petroleum group components and a separation method thereof, and the separation system is used for separating the petroleum group components from petroleum raw materials.
The separation method comprises the following steps:
extracting saturated components, aromatic components and colloid in the petroleum raw material by using a first solvent to obtain an extracting solution;
the extracting solution enters the first adsorption tower from a material inlet at the lower part of the first adsorption tower and is adsorbed, the first solvent and the saturated component which are not adsorbed enter a first evaporator, then a first evaporant containing the first solvent is evaporated, the first evaporant enters a rectifying tower for rectification, and the saturated component is obtained at the bottom of the first evaporator;
a first solvent discharged from an outlet at the top of the rectifying tower enters a first adsorption tower from a first solvent inlet, a first adsorbate in the first adsorption tower is subjected to back flushing and desorption to obtain a first desorbed solution, the first desorbed solution is mixed with a second solvent, and then the first desorbed solution enters a second adsorption tower from a material inlet at the lower part of the second adsorption tower from a first desorbed solution outlet and the second adsorption tower and is adsorbed; the first solvent, the second solvent and the aromatic component which are not adsorbed enter a second evaporator, a second evaporant containing the first solvent and the second solvent is evaporated, and then the second evaporant enters a rectifying tower for rectification, and the aromatic component is obtained at the bottom of the second evaporator; during or after the first solvent enters the second adsorption tower, the second solvent is introduced into a material inlet at the lower part of the second adsorption tower;
a second solvent discharged from an outlet at the bottom of the rectifying tower enters a second adsorption tower from a second solvent inlet, a second adsorbate in the second adsorption tower is subjected to back flushing and desorption to obtain a second desorbed solution, then the second desorbed solution enters a third evaporator from a second desorbed product outlet and a third evaporator inlet, then a third evaporant containing the second solvent and the third solvent is evaporated, then the third evaporant enters an extractor for extraction, and meanwhile, colloid is obtained at the bottom of the third evaporator; during or after the second solvent of the second desorbed solution enters the third evaporator, introducing a third solvent into an inlet of the third evaporator;
before, during or after the third evaporant enters the extraction process, introducing a fourth solvent into the inlet of the extractor, and extracting the third solvent by using the fourth solvent; and after the extractor is finished, the extract containing the second solvent at the upper part of the extractor enters a rectifying tower for rectification.
The method comprises the following steps of extracting saturated components, aromatic components and colloid in the petroleum raw material by using a first solvent: adding the petroleum raw material and a fresh first solvent and/or a first solvent obtained by rectifying in a rectifying tower into a first elution device, and then carrying out first mixed dissolution and first solid-liquid separation to obtain insoluble substances and an extracting solution; preferably, the temperature of the first mixing and dissolving is 25-90 ℃ for 5-30 min, and the temperature of the first solid-liquid separation is 25-90 ℃ for 1-10 min;
then, discharging the insoluble substances into a second elution device, introducing a second solvent into the second elution device, and then performing second mixing dissolution and second solid-liquid separation to obtain a second solvent solution dissolved with the asphaltene; preferably, the temperature of the second mixing and dissolving is 25-110 ℃ for 5-30 min, and the temperature of the second solid-liquid separation is 25-110 ℃ for 1-10 min.
When the first elution device is provided with a first evaporation unit, after first solid-liquid separation, the extracting solution is firstly discharged to the first evaporation unit, the first evaporation unit carries out evaporation concentration on the extracting solution, then the concentrated extracting solution is discharged to a first adsorption tower, and the evaporation gas phase of the first evaporation unit is discharged to a rectification tower for rectification;
when the second elution device is provided with a second evaporation unit, after second solid-liquid separation is carried out, a second solvent solution with dissolved asphaltene is firstly discharged to the second evaporation unit, the second solvent solution of the first evaporation unit is evaporated and concentrated, and the evaporated gas phase of the second evaporation unit is discharged to a rectifying tower for rectification;
the weight ratio of the petroleum raw material and the fresh first solvent added into the first elution device is 1: (0-5), the weight ratio of the petroleum raw material and the fresh second solvent added into the second elution device is 1: (0-3).
The adsorption temperature of the first adsorption tower is 20-40 ℃, and the desorption temperature is 50-80 ℃; the adsorption temperature of the second adsorption tower is 20-40 ℃, and the desorption temperature is 50-80 ℃.
The temperature of the first evaporator for evaporation is 100-105 ℃; the temperature of the second evaporator for evaporation is 105.0-110.6 ℃, and the temperature of the third evaporator for evaporation is 105.0-110.6 ℃.
The weight ratio of the petroleum raw material to the third solvent and the fourth solvent is 1: (0-2): (10-100).
The separation method further comprises: the saturated components at the bottom of the first evaporator are discharged to a saturated component collecting device, the aromatic components at the bottom of the second evaporator are discharged to an aromatic component collecting device, and the colloid at the bottom of the third evaporator is discharged to a colloid collecting device.
The separation method further comprises: the solution containing impurities is extracted from the side line of the rectifying tower.
The petroleum feedstock may be a hydrocarbon feedstock containing four components, such as crude oil, straight run wax oil, coker wax oil, bitumen, atmospheric residue, vacuum residue, and the like.
Compared with the prior art, the separation system of the petroleum family components has the following beneficial effects:
(1) the invention relates to a separation system of petroleum group components, which adopts two adsorption towers connected in series, wherein one adsorption tower is connected with a first evaporator and a rectifying tower, the second adsorption tower is connected with a second evaporator, a third evaporator and a rectifying tower, an extractor is connected with a third evaporator and a rectifying tower, so as to form an integral separation system, and simultaneously, back flushing of n-heptane and toluene is carried out for desorption in the separation process of saturated components and aromatic components, and a second solvent (toluene) and a third solvent (ethanol) are added at proper time, so that new solvent water which is not used in the conventional separation method can be introduced, thus the technical scheme is integrally combined, thereby realizing the repeated use of the adsorption towers, and simultaneously, only the first solvent (n-heptane), the second solvent (toluene) or the mixed solution of the first solvent (n-heptane) and the second solvent (toluene) can enter the rectifying tower all the time, thereby realizing the first solvent (n-heptane) and the second solvent (toluene) or, The second solvent (toluene) is separated in high purity, the aim of recycling is achieved, toluene is prevented from entering saturated components, ethanol is prevented from entering saturated components and/or aromatic components, a mixed-dissolving system of n-heptane-ethanol-samples and n-heptane-toluene-ethanol-samples is avoided, the aim of continuously separating group components of crude oil samples in a large amount with high purity and low solvent consumption is finally achieved, continuous operation, automatic production and recycling of solvents are achieved, and after one sample is separated, the next sample can be immediately separated without pretreatment steps (washing, replacement of an adsorption tower and the like).
(2) The separation system of the petroleum family components is provided with the first elution device and the second elution device, can improve the intermittent and manual extraction process of the asphaltene in the petroleum into the preparation process of continuous operation and automatic production, can fully retain the asphaltene family components in the original residual oil sample without introducing chemical modification or increasing the yield of the asphalt, does not influence other family components, and can ensure the accurate measurement of the content of the asphaltene family components in the residual oil while continuously preparing the asphaltene in large quantity; moreover, a large amount of volatile solvents in the processes of elution, filtration and evaporation can be fully recycled, the solvent consumption is reduced, the safety of the device is improved, and the pollution is reduced.
(3) According to the separation system for petroleum family components, the first elution device and the second elution device are provided with the evaporation units, so that the extracting solution and the toluene solvent containing the asphaltene can be concentrated, the concentrated extracting solution is beneficial to improving the adsorption effect of the extracting solution in the first adsorption tower and improving the desorption effect of the first solvent (n-heptane) by back flushing.
(4) The separation method of the petroleum group components adopts a plurality of solvents to repeatedly elute aiming at the solubility difference of the asphaltene, the saturated component and the aromatic component in the solvent, and respectively utilizes the evaporation and the adsorption tower to separate the four group components in the petroleum, and also utilizes the rectification tower to circularly recover the first solvent and the second solvent, the deviation of the content of the prepared four group components and the actual value is smaller, and the prepared product can be used for further precise characterization and aims to solve the problems of small preparation amount and large solvent consumption of the four group components in the petroleum.
Drawings
FIG. 1 is a flow chart of a prior art method for determining the asphaltene component of a residuum;
FIG. 2 is a schematic view of a separation system for petroleum family components of example 1 of the present invention;
reference numerals: 1-a first elutriator; 2-a second eluter; 3-a first adsorption column; 4-a second adsorption column; 5-a first evaporator; 6-a second evaporator; 7-a third evaporator; 8-an extractor; 9-a rectifying tower; a-a petroleum feedstock; b-a first solvent; c-a second solvent; d-a fourth solvent; e-asphaltenes; f-saturated component; g-aromatic component; h-colloid; i-spent solvent; j-impurity; k-third solvent.
Detailed Description
The separation system of petroleum family components of the present invention is further illustrated by the accompanying drawings, but the present invention should not be construed as being limited to the following embodiments.
As shown in fig. 2, the separation system for petroleum group components of the present invention comprises a first adsorption tower 3, a second adsorption tower 4, a first evaporator 5, a second evaporator 6, a third evaporator 7, an extractor 8, a rectification tower 9; the first adsorption tower 3 is an adsorption tower for adsorbing and desorbing aromatic components and colloid, a first unadsorbed substance outlet at the top of the first adsorption tower 3 is connected with an inlet of the first evaporator 5, and a first desorbed substance outlet at the bottom of the first adsorption tower 3 is connected with a material inlet at the lower part of the second adsorption tower 4; a first evaporation solvent outlet at the top of the first evaporator 5 is connected with the rectifying tower 9; the second adsorption tower 4 is used for adsorbing and desorbing colloid, a second unadsorbed substance outlet at the top of the second adsorption tower 4 is connected with an inlet of the second evaporator 6, and a second desorbed substance outlet at the bottom of the second adsorption tower 4 is connected with an inlet of the third evaporator 7; a second evaporation solvent outlet of the second evaporator 6 is connected with the rectifying tower 9; the third evaporator 7 is provided with a third solvent inlet, and a third evaporation outlet of the third evaporator 7 is connected with an extractor 8 inlet; the extractor 8 is provided with an inlet of a fourth solvent, and a top solution outlet of the extractor 8 is connected with the rectifying tower 9; the top outlet of the rectifying tower 9 is connected with the first solvent inlet at the upper part of the first adsorption tower 3; the bottom outlet of the rectifying tower 9 is connected with the second material inlet at the lower part of the second adsorption tower 4 and the second solvent inlet at the upper part.
In one embodiment of the invention, the separation system further comprises a first eluter 1 and a second eluter 2; the first elution device 1 is used for dissolving and extracting soluble substances of the petroleum raw material A and separating insoluble substances through a first solvent B, a first elution solution outlet of the first elution device 1 is connected with a material inlet of the first adsorption tower 3, and an insoluble substance outlet of the first elution device 1 is connected with an inlet of the second elution device 2; preferably, the inlet of the first elution device 1 is connected to the petroleum feedstock a supply line; and the second elution device 2 is used for dissolving the asphaltene in the insoluble substances through the second solvent C and separating the solution dissolved with the asphaltene to obtain the asphaltene E. Preferably, the asphaltene outlet of the second elutriator 2 is connected to an asphaltene collection means.
The first elution device is provided with a first mixed dissolving unit, a first solid-liquid separation unit and a first heating unit, an outlet of the first mixed dissolving unit is connected with an inlet of the first solid-liquid separation unit, a liquid outlet of the first solid-liquid separation unit is connected with an inlet of the first adsorption tower 3, and a solid phase outlet is connected with an inlet of the second elution device 2; the first heating unit is used for heating the first dissolving kettle and the first rotary drum filter; preferably, the first mixed dissolving unit comprises a first dissolving tank, and the first solid-liquid separation unit comprises a first rotary drum filter; the second elution apparatus 2 is provided with a second mixed dissolution unit, an outlet of which is connected to an inlet of the second solid-liquid separation unit, a second solid-liquid separation unit, which preferably includes a second dissolution tank, and a second heating unit, which preferably includes a second drum filter, for heating the second dissolution tank and the second drum filter.
A circulating pipeline is connected between the inlet of the first solid-liquid separation unit and the liquid outlet of the first solid-liquid separation unit, and a valve body is arranged on the circulating pipeline.
The top outlet of the rectifying tower 9 is also connected with the inlet of the first elution device 1; the outlet at the bottom of the rectifying tower 9 is also connected with the inlet of the second elution device 2.
The first elution device 1 is provided with a first evaporation unit, the inlet of the first evaporation unit is connected with the liquid outlet of the first solid-liquid separation unit, and the vapor phase outlet of the first evaporation unit is connected with the inlet of the rectifying tower 9; the second elution device 2 is provided with a second evaporation unit, the inlet of the second evaporation unit is connected with the liquid outlet of the second solid-liquid separation unit, and the vapor gas phase outlet of the second evaporation unit is connected with the inlet of the rectifying tower 9.
In another embodiment of the present invention, the first evaporator 5 is an evaporator for evaporating the first solvent, the second evaporator 6 is an evaporator for evaporating the first solvent and the second solvent, and the third evaporator 7 is an evaporator for evaporating the second solvent and the third solvent; preferably, the evaporation residue outlet at the bottom of the first evaporator 5 is connected with the saturation fraction collecting device, the evaporation residue outlet at the bottom of the second evaporator 6 is connected with the aroma fraction collecting device, and the evaporation residue outlet at the bottom of the third evaporator 7 is connected with the colloid substance collecting device. Further preferably, the first evaporator 5, the second evaporator 6 and the third evaporator 7 adopt a single-effect or multi-effect falling film evaporator.
The extractor 8 is used for separating the second solvent and the third solvent by extraction, preferably, a bottom solution outlet of the extractor 8 discharges the waste solvent I, and a bottom solution outlet of the extractor 8 is connected with a waste solvent collecting device, and then the third solvent and the third solvent are separated. Further preferably, the extractor 8 is a packed extractor, a rotating disc extractor or a centrifugal extractor
The first solvent B comprises one of n-heptane, n-hexane and petroleum ether; the second solvent C comprises one of toluene and benzene; the third solvent comprises one of ethanol, methanol and propanol; the fourth solvent is water.
The first adsorption tower 3 and the second adsorption tower 4 are filler adsorption towers, wherein one or more of alumina, 5A molecular sieve, silica gel, macroporous adsorption resin and ion exchange resin are filled in the towers, preferably, the first adsorption tower 3 is filled with macroporous adsorption resin, 5A molecular sieve and alumina filler, and the second adsorption tower 4 is filled with macroporous adsorption resin, 5A molecular sieve and silica gel filler.
The rectifying tower 9 is a rectifying tower for continuous rectification of two components of the first solvent and the second solvent, preferably, the rectifying tower 9 is a multi-section rectifying tower, an outlet at the top of the rectifying tower 9 is a discharge port for the first solvent with a low boiling point, an outlet at the bottom of the rectifying tower 9 is a discharge port for the second solvent with a high boiling point, and further preferably, a discharge port for the impurity solvent is arranged at a side line of the rectifying tower 9, and the impurity J in the rectifying tower can be discharged through the discharge port.
The invention also provides a separation method of the separation system based on the petroleum family components, which comprises the steps of extracting saturated components, aromatic components and colloid in the petroleum raw material A by using the first solvent B to obtain an extracting solution; the extracting solution enters the first adsorption tower 3 from a material inlet at the lower part of the tower and is adsorbed, the first solvent B and the saturated component which are not adsorbed enter a first evaporator 5, then a first evaporant containing the first solvent B is evaporated, the first evaporant enters a rectifying tower 9 for rectification, and meanwhile, the saturated component F is obtained at the bottom of the first evaporator 5; a first solvent B discharged from an outlet at the top of the rectifying tower 9 enters the first adsorption tower 3 from a first solvent inlet, the first adsorbate in the first adsorption tower 3 is subjected to back flushing and desorption to obtain a first desorbed solution, and then the first desorbed solution is mixed with a second solvent and enters the second adsorption tower 4 from a material inlet at the lower part of the second adsorption tower 4 to be adsorbed; the first solvent B, the second solvent C and the aromatic component which are not adsorbed enter a second evaporator 6, a second evaporant containing the first solvent B and the second solvent C is evaporated, and then the second evaporant enters a rectifying tower 9 for rectification, and simultaneously the aromatic component G is obtained at the bottom of the second evaporator 6; a second solvent C discharged from an outlet at the bottom of the rectifying tower 9 enters the second adsorption tower 4 from a second solvent inlet, a second adsorbate in the second adsorption tower 4 is subjected to back flushing and desorption to obtain a solution containing a second adsorbate, the solution enters the third evaporator 7 from an inlet of the third evaporator 7, a third evaporant containing the second solvent and the third solvent is evaporated, the solution enters the extractor 8 for extraction, and colloid H is obtained at the bottom of the third evaporator 7; during or after the second desorbed solution enters the third evaporator 7, a third solvent is also introduced into the inlet of the third evaporator 7; before, during or after the third evaporant enters the extraction process, a fourth solvent D is also introduced into the inlet of the extractor 8, and the fourth solvent D is used for extracting the third solvent; after the extractor 8 is finished, the extract liquid containing the second solvent at the upper part of the extractor 8 enters a rectifying tower 9 for rectification.
The method comprises the following steps of extracting saturated components, aromatic components and colloid in the petroleum raw material A by using a first solvent B: adding the petroleum raw material A and a fresh first solvent B and/or a first solvent B obtained by rectifying in a rectifying tower 9 into a first elution device 1, and then carrying out first mixed dissolution and first solid-liquid separation to obtain insoluble substances and an extracting solution; preferably, the temperature of the first mixing and dissolving is 25-90 ℃ for 5-30 min, and the temperature of the first solid-liquid separation is 25-90 ℃ for 1-10 min; then, discharging the insoluble substances into a second elution device 2, simultaneously introducing a second solvent C into the second elution device 2, and then carrying out second mixed dissolution and second solid-liquid separation to obtain a second solvent solution dissolved with the asphaltene; preferably, the temperature of the second mixing and dissolving is 25-110 ℃ for 5-30 min, and the temperature of the second solid-liquid separation is 25-110 ℃ for 1-10 min.
When the first elution device 1 is provided with a first evaporation unit, after first solid-liquid separation, the extracting solution is firstly discharged to the first evaporation unit, the first evaporation unit carries out evaporation concentration on the extracting solution, then the concentrated extracting solution is discharged to the first adsorption tower 3, and the evaporated gas phase of the first evaporation unit is discharged to the rectifying tower 9 for rectification; when the second elution device 2 is provided with a second evaporation unit, after second solid-liquid separation is carried out, the second solvent solution with the dissolved asphaltene is firstly discharged to the second evaporation unit, the second solvent solution of the first evaporation unit is evaporated and concentrated, and the evaporated gas phase of the second evaporation unit is discharged to the rectifying tower 9 for rectification;
when the first solvent and the second solvent are circulated sufficiently for the first elution and the second elution, the first solvent and the second solvent which can be rectified by the rectifying tower are added to the first elution device and the second elution device, respectively. When the circulation amount is insufficient, the weight ratio of the petroleum raw material and the fresh first solvent added into the first elution device 1 is 1: (0-5), the weight ratio of the petroleum raw material and the fresh second solvent added into the second elution device 2 is 1: (0-3).
The temperature of the first evaporator 5 for evaporation is 100-105 ℃; the temperature of the second evaporator 6 for evaporation is 105.0-110.6 ℃, and the temperature of the third evaporator 7 for evaporation is 105.0-110.6 ℃. When the first evaporator, the second evaporator and the third evaporator are used for evaporation, the solvent can be evaporated according to the requirements of experiments on saturation components, aroma components and colloid, and the evaporation is stopped when the solvent amount in the evaporation residue is less than 1%.
When the third solvent is not required to be added in the third evaporator, the amount of the third solvent to be added may be 0. The weight ratio of the petroleum raw material to the third solvent and the fourth solvent is 1: (0-2): (10-100).
The method further comprises the following steps: the saturated component at the bottom of the first evaporator 5 is discharged to the saturated component collecting device, the aromatic component at the bottom of the second evaporator 6 is discharged to the aromatic component collecting device, and the gum at the bottom of the third evaporator 7 is discharged to the gum collecting device.
The method further comprises the following steps: the solution containing impurities is drawn off at the side of the rectification column 9.
Example 1
(1) Firstly, all the devices of the invention are normally started and operated, 200-500 kg of normal heptane solvent obtained by a rectifying tower is added into a first elution device 1, and 50-100 kg of toluene obtained by a rectifying tower is added into a second elution device 2. Adding a mixture of 0.5kg of petroleum raw material A1 and 0.1kg of fresh n-heptane into a first elution device 1, and then carrying out first mixed dissolution and first solid-liquid separation to obtain an extracting solution and insoluble substances; the temperature of the first mixing and dissolving is 85 ℃ and the time is 5min, and the temperature of the first solid-liquid separation is 85 ℃ and the time is 10 min.
The extracting solution is firstly discharged to a first evaporation unit, the first evaporation unit carries out evaporation concentration on the extracting solution, then the concentrated extracting solution is discharged to a first adsorption tower 3, and the evaporation gas phase (normal heptane) of the first evaporation unit is discharged to a rectifying tower 9 for rectification.
Discharging the insoluble substances into a second elution device 2, simultaneously introducing 0.1kg of toluene into the second elution device 2, and then performing second mixed dissolution and second solid-liquid separation to obtain a second solvent solution in which the asphaltenes are dissolved; the temperature of the second mixing and dissolving is 95 ℃ and the time is 5min, and the temperature of the second solid-liquid separation is 95 ℃ and the time is 10 min. After the second solid-liquid separation, the second solvent solution with the dissolved asphaltenes is discharged to the second evaporation unit, the second evaporation unit evaporates and concentrates the second solvent solution, and the evaporated gas phase (toluene) of the second evaporation unit is discharged to the rectifying tower 9 for rectification.
(2) The first extraction solution enters a first adsorption tower 3 (filled with macroporous adsorption resin, 5A molecular sieve and alumina filler) from a material inlet at the lower part of the tower and is adsorbed, the adsorption temperature is 25 ℃, unadsorbed n-heptane and saturated components enter a first evaporator 5, then n-heptane is evaporated and enters a rectifying tower 9 for rectification, and meanwhile, the saturated components are obtained at the bottom of the first evaporator 5 or further discharged to a saturated component collecting device; the temperature of the first evaporator 5 for evaporation is 100 to 105 ℃.
After the first adsorption tower 3 finishes adsorption, n-heptane discharged from an outlet at the top of the rectifying tower 9 enters the first adsorption tower 3 from a first solvent inlet, the first adsorbate in the first adsorption tower 3 is subjected to back flushing and desorption at the desorption temperature of 25 ℃ to obtain a first desorbed solution, and then the first desorbed solution is mixed with toluene and discharged to the second adsorption tower 4 from a material inlet at the lower part of the second adsorption tower 4.
(3) The first desorbed substances enter a second adsorption tower 4 (filled with macroporous adsorption resin, a 5A molecular sieve and silica gel filler) and are adsorbed, the adsorption temperature is 25 ℃, unadsorbed n-heptane, toluene and aromatic components enter a second evaporator 6, then a second evaporated substance containing n-heptane and toluene is evaporated, and then the second evaporated substance enters a rectifying tower 9 for rectification, and simultaneously aromatic components are obtained at the bottom of the second evaporator 6; the temperature of the second evaporator 6 is 105.0-110.6 ℃.
After the second adsorption tower 4 finishes the adsorption, the toluene discharged from the outlet at the bottom of the rectifying tower 9 enters the second adsorption tower 4 from the second solvent inlet, the second adsorbate in the second adsorption tower 4 is subjected to back flushing and desorption at the desorption temperature of 60 ℃ to obtain a second desorbent solution, and then the second desorbent solution enters the third evaporator 7 from the inlet of the third evaporator 7.
(4) After entering a third evaporator 7, evaporating a third evaporant containing toluene and ethanol, then entering an extractor 8 for extraction, and simultaneously obtaining colloid at the bottom of the third evaporator 7, or further discharging the colloid to a colloid collecting device; wherein, in the process that the second desorbed solution enters the third evaporator 7, ethanol is introduced into an inlet of the third evaporator 7, and the temperature of the third evaporator 7 for evaporation is 105.0-110.6 ℃; in the process that the third evaporant enters the extraction, water is introduced into the inlet of the extractor 8 and is used for extracting ethanol; after the extractor 8 is finished, the extract liquid containing toluene at the upper part of the extractor 8 enters a rectifying tower 9 for rectification.
(5) And when all the raw materials enter the system and are fully separated, the product outlet is not separated any more to obtain a new product, the n-heptane outlet and the toluene outlet of the rectifying tower are switched to a solvent storage device, and the system is kept running until all the solvents are fully recovered. The recovered solvent can be used for the next separation process.
Example 2
(2) The method of this example is basically the same as example 1, except that: after the four-component separation of petroleum was completed in example 1, the four-component separation was continued by changing to another petroleum feedstock a 2. And when all the raw materials enter the system and are fully separated, the product outlet is not separated any more to obtain a new product, the n-heptane outlet and the toluene outlet of the rectifying tower are switched to a solvent storage device, and the system is kept running until all the solvents are fully recovered. The recovered solvent can be used for the next separation process.
TABLE 1 Properties of Petroleum feedstocks
| Petroleum feedstock | A1 | A2 |
| Elemental analysis | ||
| C,% | 82.2 | 86.46 |
| H,% | 10.16 | 11.14 |
| S,% | 5.11 | 1.51 |
| N,ppm | 4193 | 3890 |
| Residual carbon content% | 23.91 | 12.71 |
| Molecular weight | 618 | 586 |
| Liquid high temperature simulated distillation% | ||
| IBP | 389.4 | 160.8 |
| 10% | 520.4 | 329 |
| 30% | 586.4 | 473 |
| 50% | 643.4 | 555.6 |
| 70% | 711.2 | 632.2 |
TABLE 2 separation of petroleum family Components
| Standard methods | Example 1 | Standard methods | Example 2 | |
| Petroleum feedstock | A1 | A1 | A2 | A2 |
| Raw material mass, g | 1 | 500 | 1 | 500 |
| Consumption of n-heptane, g | 150 | 2000 | 200 | 2500 |
| Amount of toluene consumed, g | 200 | 2000 | 200 | 2500 |
| Solvent consumption per unit raw material, g/g | 350 | 11 | 400 | 8 |
| Determining the saturation fraction% | 19.31 | 18.90 | 30.21 | 29.89 |
| Measuring the aroma fraction% | 47.23 | 47.15 | 55.49 | 53.55 |
| Determination of the degree of gelatinization | 27.91 | 28.34 | 12.87 | 15.08 |
| Determination of asphaltene% | 5.55 | 5.61 | 1.44 | 1.48 |
Note: standard methods test according to NB SH/T0509-.
It should be noted that the various features described in the foregoing detailed description may be combined in any suitable manner and still fall within the scope of the invention disclosed. In addition, any combination of the various embodiments of the present invention is also possible, and the same should be considered as the disclosure of the present invention as long as it does not depart from the spirit of the present invention.
The preferred embodiments of the present invention have been described in detail with reference to the accompanying drawings, however, the present invention is not limited to the specific details of the above embodiments, and various simple modifications can be made to the technical solution of the present invention within the technical idea of the present invention, and these simple modifications are within the protective scope of the present invention.
Claims (30)
1. A separation system for continuously separating petroleum group components is characterized by comprising a first adsorption tower, a second adsorption tower, a first evaporator, a second evaporator, a third evaporator, an extractor and a rectifying tower;
the first adsorption tower is used for adsorbing and desorbing aromatic components and colloid, a first unadsorbed substance outlet at the top of the first adsorption tower is sequentially connected with the first evaporator and the rectifying tower, and a first desorbed substance outlet at the bottom of the first adsorption tower is connected with a material inlet at the lower part of the second adsorption tower;
the second adsorption tower is used for adsorbing and desorbing the colloid, and a second unadsorbed substance outlet at the top of the second adsorption tower is sequentially connected with the second evaporator and the rectifying tower; a second desorbed substance outlet at the bottom of the second adsorption tower is sequentially connected with the third evaporator, the extractor and the rectifying tower; the third evaporator is provided with an inlet of a third solvent, and the extractor is provided with an inlet of a fourth solvent;
the top outlet of the rectifying tower is connected with the first solvent inlet at the upper part of the first adsorption tower; and the bottom outlet of the rectifying tower is connected with a material inlet at the lower part of the second adsorption tower and a second solvent inlet at the upper part of the second adsorption tower.
2. The separation system of claim 1, wherein: the separation system further comprises a first elutriator and a second elutriator;
the first elution device is used for dissolving and extracting soluble substances of the petroleum raw materials and separating insoluble substances through a first solvent, a first elution solution outlet of the first elution device is connected with a material inlet of the first adsorption tower, and an insoluble substance outlet of the first elution device is connected with an inlet of the second elution device;
and the second elution device is used for dissolving the asphaltene in the insoluble substances through a second solvent and separating the solution dissolved with the asphaltene.
3. The separation system of claim 2, wherein: the inlet of the first elution device is connected with a petroleum raw material supply pipeline; the asphaltene outlet of the second elution device is connected with an asphaltene collection device.
4. The separation system of claim 2, wherein: the first elution device is provided with a first mixed dissolving unit, a first solid-liquid separation unit and a first heating unit, an outlet of the first mixed dissolving unit is connected with an inlet of the first solid-liquid separation unit, a liquid outlet of the first solid-liquid separation unit is connected with an inlet of the first adsorption tower, and a solid phase outlet is connected with an inlet of the second elution device; the first heating unit is used for heating the first dissolving kettle and the first rotary drum filter; the first mixing and dissolving unit comprises a first dissolving kettle, and the first solid-liquid separation unit comprises a first rotary drum filter;
the second elution device is provided with a second mixing and dissolving unit, a second solid-liquid separation unit and a second heating unit, an outlet of the second mixing and dissolving unit is connected with an inlet of the second solid-liquid separation unit, the second mixing and dissolving unit comprises a second dissolving kettle, the second solid-liquid separation unit comprises a second rotary drum filter, and the second heating unit is used for heating the second dissolving kettle and the second rotary drum filter.
5. The separation system of claim 4, wherein: a circulating pipeline is connected between the inlet of the first solid-liquid separation unit and the liquid outlet of the first solid-liquid separation unit, and a valve body is arranged on the circulating pipeline.
6. The separation system of claim 2, wherein: the top outlet of the rectifying tower is also connected with the inlet of the first elution device; the outlet at the bottom of the rectifying tower is also connected with the inlet of the second elution device.
7. The separation system of claim 2, wherein: the first elution device is provided with a first evaporation unit, an inlet of the first evaporation unit is connected with a liquid outlet of the first solid-liquid separation unit, and a vapor phase outlet of the first evaporation unit is connected with an inlet of the rectifying tower;
the second elution device is provided with a second evaporation unit, an inlet of the second evaporation unit is connected with a liquid outlet of the second solid-liquid separation unit, and a vapor gas phase outlet of the second evaporation unit is connected with an inlet of the rectifying tower.
8. The separation system of claim 1, wherein: the first evaporator is an evaporator for evaporating the first solvent, the second evaporator is an evaporator for evaporating the first solvent and the second solvent, and the third evaporator is an evaporator for evaporating the second solvent and the third solvent.
9. The separation system of claim 8, wherein: the evaporation residue outlet at the bottom of the first evaporator is connected with the saturation fraction collecting device, the evaporation residue outlet at the bottom of the second evaporator is connected with the fragrance fraction collecting device, and the evaporation residue outlet at the bottom of the third evaporator is connected with the colloid collecting device.
10. The separation system of claim 8, wherein: the first evaporator, the second evaporator and the third evaporator adopt a single-effect or multi-effect falling-film evaporator.
11. The separation system of claim 1, wherein: the extractor is used to separate the second solvent and the third solvent by extraction.
12. The separation system of claim 11, wherein: the bottom solution outlet of the extractor is connected with a waste solvent collecting device.
13. The separation system of claim 11, wherein: the extractor adopts a filler type extractor, a rotating disc type extractor or a centrifugal extractor.
14. The separation system of claim 1, wherein: the first solvent comprises one of n-heptane, n-hexane and petroleum ether; the second solvent comprises one of toluene and benzene; the third solvent comprises one of ethanol, methanol and propanol; the fourth solvent is water.
15. The separation system of claim 1, wherein: the first adsorption tower and the second adsorption tower are filler adsorption towers, wherein one or more of alumina, a 5A molecular sieve, silica gel, macroporous adsorption resin and ion exchange resin are filled in the towers.
16. The separation system of claim 15, wherein: the first adsorption tower is filled with macroporous adsorption resin, a 5A molecular sieve and alumina filler, and the second adsorption tower is filled with macroporous adsorption resin, a 5A molecular sieve and silica gel filler.
17. The separation system of claim 1, wherein: the rectifying tower is used for continuously rectifying the first solvent and the second solvent.
18. The separation system of claim 17, wherein: the rectifying tower adopts a multi-section rectifying tower, the outlet at the top of the rectifying tower is a discharge port of a first solvent with a low boiling point, and the outlet at the bottom of the rectifying tower is a discharge port of a second solvent with a high boiling point.
19. The separation system of claim 18, wherein: the side line of the rectifying tower is provided with an outlet of the impurity solvent.
20. A separation method for continuously separating petroleum group components is characterized in that: separation of petroleum family components is carried out on a petroleum feedstock using the separation system of any one of claims 1 to 19.
21. The separation method of claim 20, wherein: the separation method comprises the following steps:
extracting saturated components, aromatic components and colloid in the petroleum raw material by using a first solvent to obtain an extracting solution;
the extracting solution enters the first adsorption tower from a material inlet at the lower part of the first adsorption tower and is adsorbed, the first solvent and the saturated component which are not adsorbed enter a first evaporator, then a first evaporant containing the first solvent is evaporated, the first evaporant enters a rectifying tower for rectification, and the saturated component is obtained at the bottom of the first evaporator;
a first solvent discharged from an outlet at the top of the rectifying tower enters a first adsorption tower from a first solvent inlet, a first adsorbate in the first adsorption tower is subjected to back flushing and desorption to obtain a first desorbed solution, and then the first desorbed solution is mixed with a second solvent and enters a second adsorption tower from a material inlet at the lower part of the second adsorption tower for adsorption; the first solvent, the second solvent and the aromatic component which are not adsorbed enter a second evaporator, a second evaporant containing the first solvent and the second solvent is evaporated, and then the second evaporant enters a rectifying tower for rectification, and the aromatic component is obtained at the bottom of the second evaporator;
a second solvent discharged from an outlet at the bottom of the rectifying tower enters a second adsorption tower from a second solvent inlet, a second adsorbate in the second adsorption tower is subjected to back flushing and desorption to obtain a second desorbed solution, then the second desorbed solution enters a third evaporator from an inlet of the third evaporator, then a third evaporant containing the second solvent and the third solvent is evaporated, then the third evaporant enters an extractor for extraction, and meanwhile, a colloid is obtained at the bottom of the third evaporator; during or after the second desorbed solution enters the third evaporator, introducing a third solvent into the inlet of the third evaporator;
before, during or after the third evaporant enters the extraction process, introducing a fourth solvent into the inlet of the extractor, and extracting the third solvent by using the fourth solvent; and after the extractor is finished, the extract containing the second solvent at the upper part of the extractor enters a rectifying tower for rectification.
22. The separation method of claim 21, wherein: the method comprises the following steps of extracting saturated components, aromatic components and colloid in the petroleum raw material by using a first solvent: adding the petroleum raw material and a fresh first solvent and/or a first solvent obtained by rectifying in a rectifying tower into a first elution device, and then carrying out first mixed dissolution and first solid-liquid separation to obtain insoluble substances and an extracting solution;
and then, discharging the insoluble substances into a second elution device, introducing a second solvent into the second elution device, and then carrying out second mixing dissolution and second solid-liquid separation to obtain a second solvent solution dissolved with the asphaltene.
23. The separation method of claim 22, wherein: the temperature of the first mixing and dissolving is 25-90 ℃, the time is 5-30 min, the temperature of the first solid-liquid separation is 25-90 ℃, and the time is 1-10 min; the temperature of the second mixing and dissolving is 25-110 ℃, the time is 5-30 min, the temperature of the second solid-liquid separation is 25-110 ℃, and the time is 1-10 min.
24. The separation method of claim 22, wherein: when the first elution device is provided with a first evaporation unit, after first solid-liquid separation, the extracting solution is firstly discharged to the first evaporation unit, the first evaporation unit carries out evaporation concentration on the extracting solution, then the concentrated extracting solution is discharged to a first adsorption tower, and the evaporation gas phase of the first evaporation unit is discharged to a rectification tower for rectification;
when the second elution device is provided with a second evaporation unit, after second solid-liquid separation is carried out, the second solvent solution with the dissolved asphaltene is firstly discharged to the second evaporation unit, the second solvent solution of the first evaporation unit is evaporated and concentrated, and the evaporated gas phase of the second evaporation unit is discharged to the rectifying tower for rectification.
25. The separation method of claim 22, wherein: the weight ratio of the petroleum raw material and the fresh first solvent added into the first elution device is 1: (0-5), wherein the weight ratio of the insoluble matters from the first elution device and the fresh second solvent added into the second elution device is 1: (0-3).
26. The separation method of claim 21, wherein: the adsorption temperature of the first adsorption tower is 20-40 ℃, and the desorption temperature is 50-80 ℃; the adsorption temperature of the second adsorption tower is 20-40 ℃, and the desorption temperature is 50-80 ℃.
27. The separation method of claim 21, wherein: the temperature of the first evaporator for evaporation is 100-105 ℃; the temperature of the second evaporator for evaporation is 105.0-110.6 ℃, and the temperature of the third evaporator for evaporation is 105.0-110.6 ℃.
28. The separation method of claim 21, wherein: the weight ratio of the petroleum raw material to the third solvent and the fourth solvent is 1: (0-2): (10-100).
29. The separation method of claim 21, wherein: the separation method further comprises: the saturated components at the bottom of the first evaporator are discharged to a saturated component collecting device, the aromatic components at the bottom of the second evaporator are discharged to an aromatic component collecting device, and the colloid at the bottom of the third evaporator is discharged to a colloid collecting device.
30. The separation method of claim 21, wherein: the separation method further comprises: the solution containing impurities is led out from the side line of the rectifying tower.
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