CN111088062A - System and method for viscosity reduction - Google Patents
System and method for viscosity reduction Download PDFInfo
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- CN111088062A CN111088062A CN201811243872.5A CN201811243872A CN111088062A CN 111088062 A CN111088062 A CN 111088062A CN 201811243872 A CN201811243872 A CN 201811243872A CN 111088062 A CN111088062 A CN 111088062A
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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
- C10G21/00—Refining of hydrocarbon oils, in the absence of hydrogen, by extraction with selective solvents
- C10G21/28—Recovery of used solvent
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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
- C10G21/00—Refining of hydrocarbon oils, in the absence of hydrogen, by extraction with selective solvents
- C10G21/003—Solvent de-asphalting
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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
- C10G31/00—Refining of hydrocarbon oils, in the absence of hydrogen, by methods not otherwise provided for
- C10G31/06—Refining of hydrocarbon oils, in the absence of hydrogen, by methods not otherwise provided for by heating, cooling, or pressure treatment
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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
- C10G2300/30—Physical properties of feedstocks or products
- C10G2300/302—Viscosity
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- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The invention relates to the field of ethylene production, and discloses a viscosity reduction system and a method, wherein the viscosity reduction system comprises an extraction tower, a solvent recovery tower, a solvent tank, a pumped phase vacuum vessel, a light oil stripping tower, a pumped phase vacuum vessel, a raffinate phase solvent separation tower, a heavy oil stripping tower and a pressure pump; the extraction tower is provided with a high-viscosity oil feeding port and a solvent feeding port; the top of the extraction tower is sequentially connected with a pumping-out phase decompressor and a solvent recovery tower, the bottom of the solvent recovery tower is connected with a light oil stripping tower, and the bottom of the light oil stripping tower is provided with a light oil discharge hole; the bottom of the extraction tower is sequentially connected with a raffinate phase pressure reducer and a raffinate phase solvent separation tower, the bottom of the raffinate phase solvent separation tower is connected with a heavy oil stripping tower, and the bottom of the heavy oil stripping tower is provided with a heavy oil discharge hole; the tops of the solvent recovery tower, the light oil stripping tower, the raffinate phase solvent separation tower and the heavy oil stripping tower are respectively and sequentially connected with a pressure pump and a solvent tank; the solvent tank is connected with a solvent feed inlet of the extraction tower. The viscosity reducing system of the invention can reduce the viscosity of oil products and the solvent loss rate.
Description
Technical Field
The invention relates to the field of ethylene production in petrochemical industry, in particular to a viscosity reduction system and a viscosity reduction method.
Background
Viscosity affects the mass transfer capacity and heat transfer capacity of oil products, and high-viscosity oil consumes more energy during pipeline transportation due to higher viscosity, low diffusion coefficient and large mass transfer and heat transfer resistance, needs more heat exchange area during heat exchange and needs longer residence time in reaction. In summary, high viscosity oils cause more energy waste and material loss in petroleum and chemical operations.
Taking the quenching oil as an example, the viscosity range of the quenching oil at 50 ℃ is 10mm2/s～10000mm2The viscosity rise of the oil, which is a typical high-viscosity oil and is an important heat transfer medium of an ethylene unit, can directly influence the normal operation of a cracking furnace, an oil washing tower and a dilution steam generation system, and even cause the blockage accident of a pipeline and equipment of a quenching oil circulation system. At present, many domestic quenching oil viscosity reduction systems are not reasonable in design, only play a role in reducing the viscosity of quenching oil, but do not fundamentally and thoroughly solve the problems of high viscosity of quenching oil, particularly large loss amount of solvent, low recovery rate and the like.
For example, CN103305259A discloses a method for reducing the viscosity of quenching oil in an ethylene unit, wherein the quenching oil from the bottom of an oil scrubber is extracted and recovered by a supercritical solvent to obtain viscosity-reduced quenching oil, and the solvent is recovered. The invention obtains viscosity reduction quenching from the separation of the tower kettle of the solvent recovery towerThe oil viscosity can only be reduced to 21mm2The solvent recovery rate is improved by a multistage recovery method for the extracted phase (approximately 20 to 23mPa · s), but the solvent is still partially lost, and the heavy oil and the light oil contain the solvent, and for example, the treatment load of a downstream apparatus is increased for the subsequent treatment of the solvent contained in the light oil, and the environment is affected, and the cost is high for the supercritical extraction equipment. Therefore, there is a need to find a system and method for viscosity reduction that is more effective in reducing the viscosity of the quench oil and reducing the rate of solvent loss.
Disclosure of Invention
The invention aims to solve the problems of high viscosity of quenching oil, large loss amount of solvent, low recovery rate and the like in the prior art, and provides a viscosity reduction system and a viscosity reduction method.
In order to achieve the above object, the present invention provides, in one aspect, a viscosity reducing system comprising an extraction column, a solvent recovery column, and a solvent tank, the system further comprising a suction phase decompressor, a light oil stripper, a raffinate phase decompressor, a raffinate phase solvent separation column, a heavy oil stripper, and a pressure pump; wherein, a high-viscosity oil feeding hole and a solvent feeding hole are arranged on the extraction tower; the top of the extraction tower is sequentially connected with a pumping-out phase decompression device and a solvent recovery tower, the bottom of the solvent recovery tower is connected with a light oil stripping tower, and the bottom of the light oil stripping tower is provided with a light oil discharge hole; the bottom of the extraction tower is sequentially connected with a raffinate phase pressure reducer and a raffinate phase solvent separation tower, the bottom of the raffinate phase solvent separation tower is connected with a heavy oil stripping tower, and the bottom of the heavy oil stripping tower is provided with a heavy oil discharge hole; the tops of the solvent recovery tower, the light oil stripping tower, the raffinate phase solvent separation tower and the heavy oil stripping tower are respectively connected with a pressure pump and a solvent tank in sequence; and a supplementary solvent feeding hole and a solvent discharging hole are formed in the solvent tank and are connected with the solvent feeding hole of the extraction tower through the solvent discharging hole.
In a second aspect, the present invention provides a method of reducing tackiness comprising the steps of:
(1) the high-viscosity oil and the solvent enter an extraction tower for extraction, an extraction phase is obtained at the top of the extraction tower, and a raffinate phase is obtained at the bottom of the extraction tower;
(2) the extracted phase enters a solvent recovery tower for separation after being decompressed by an extraction phase decompressor, the solvent and light oil are separated in the solvent recovery tower, the top of the solvent recovery tower obtains a first recovered solvent, and the bottom of the solvent recovery tower obtains light oil containing the solvent;
(3) the light oil containing the solvent enters a light oil stripping tower to be subjected to steam stripping, steam and the solvent are obtained at the top of the light oil stripping tower, a gas phase and a water phase are obtained through separation after cooling, the gas phase is a recovered solvent II, and light oil is obtained at the bottom of the tower;
(4) reducing the pressure of the raffinate phase by a raffinate phase pressure reducer, and then separating the raffinate phase in a raffinate phase solvent separation tower to obtain a third recovered solvent at the top of the raffinate phase solvent separation tower and heavy oil at the bottom of the raffinate phase solvent separation tower;
(5) heavy oil enters a heavy oil stripping tower and is subjected to steam stripping, steam and a solvent are obtained at the top of the heavy oil stripping tower, a gas phase and a water phase are obtained after cooling and separation, the gas phase is a recovered solvent IV, and asphalt is obtained at the bottom of the tower;
(6) and (3) boosting the pressure of the recovered solvent I, the recovered solvent II, the recovered solvent III and the recovered solvent IV, and collecting the mixture in a solvent tank for recycling.
By adopting the technical scheme, viscosity of oil products can be remarkably reduced by using the viscosity reducing system for viscosity reduction, solvent loss rate can be remarkably reduced, and the problems of solvent residue in the products and environmental pollution are thoroughly solved.
Drawings
Fig. 1 is a schematic diagram of a viscosity reducing system according to an embodiment of the present invention.
Description of the reference numerals
1-extraction tower, 2-extraction phase pressure reducer, 3-raffinate phase pressure reducer, 4-solvent recovery tower, 5-light oil stripping tower, 6-raffinate phase solvent separation tower, 7-heavy oil stripping tower, 8-solvent tank, 9-pressure pump, 10-heat exchanger, 11-heat exchanger, 12-heavy oil heater
Detailed Description
The endpoints of the ranges and any values disclosed herein are not limited to the precise range or value, and such ranges or values should be understood to encompass values close to those ranges or values. For ranges of values, between the endpoints of each of the ranges and the individual points, and between the individual points may be combined with each other to give one or more new ranges of values, and these ranges of values should be considered as specifically disclosed herein.
As shown in fig. 1, the present invention provides a viscosity reduction system, which comprises an extraction tower 1, a solvent recovery tower 4 and a solvent tank 8, and further comprises an extraction phase pressure reducer 2, a light oil stripping tower 5, a raffinate phase pressure reducer 3, a raffinate phase solvent separation tower 6, a heavy oil stripping tower 7 and a pressure pump 9; wherein, a high-viscosity oil feeding port and a solvent feeding port are arranged on the extraction tower 1; the top of the extraction tower 1 is sequentially connected with an extraction phase decompression device 2 and a solvent recovery tower 4, the bottom of the solvent recovery tower 4 is connected with a light oil stripping tower 5, and the bottom of the light oil stripping tower 5 is provided with a light oil discharge hole; the bottom of the extraction tower 1 is sequentially connected with a raffinate phase pressure reducer 3 and a raffinate phase solvent separation tower 6, the bottom of the raffinate phase solvent separation tower 6 is connected with a heavy oil stripping tower 7, and the bottom of the heavy oil stripping tower 7 is provided with a heavy oil discharge hole; the tops of the solvent recovery tower 4, the light oil stripping tower 5, the raffinate phase solvent separation tower 6 and the heavy oil stripping tower 7 are respectively connected with a pressure pump 9 and a solvent tank 8 in sequence; and a supplementary solvent feeding hole and a solvent discharging hole are formed in the solvent tank 8 and are connected with the solvent feeding hole of the extraction tower 1 through the solvent discharging hole.
The invention realizes the complete recovery of the solvent in the light oil through the pumping phase pressure reducer, the solvent recovery tower and the light oil stripping tower, reduces the processing load of downstream devices of residual solvent in the light oil, realizes the complete recovery of the solvent in the heavy oil through the raffinate phase pressure reducer, the raffinate phase solvent separation tower and the heavy oil stripping tower, ensures the product quality and also reduces the influence of the solvent on the environment. Therefore, the invention thoroughly recovers the solvent and greatly reduces the solvent loss rate.
Preferably, the solvent recovery rate is further increased by providing a heavy oil heater 12 between the raffinate phase solvent separation column 6 and the heavy oil stripper 7 to heat the heavy oil drawn from the bottom of the raffinate phase solvent separation column 6 before the heavy oil enters the heavy oil stripper 7.
The heavy oil heater 12 may be any conventional heater, and may be a heat exchanger or a heating furnace, for example.
In the present invention, the extraction phase pressure reducer 2 and/or the raffinate phase pressure reducer 3 may be a pressure reducing valve.
In the present invention, the top of the light oil stripping tower 5, the raffinate phase solvent separation tower 6, and the heavy oil stripping tower 7 are sequentially connected to a heat exchanger 10 (to reduce the temperature of the recovered solvent), a pressure pump 9, and a solvent tank 8, thereby effectively ensuring the recovery of the solvent.
In the invention, the solvent discharge port of the solvent tank 8 is connected with the solvent feed port of the extraction tower 1 through the heat exchanger 11, so that the temperature of the solvent entering the extraction tower is effectively ensured.
In the invention, the steam in the light oil stripping tower 5 and the steam in the heavy oil stripping tower 7 can be recycled.
The invention provides a viscosity breaking method, which comprises the following steps:
(1) the high-viscosity oil and the solvent enter an extraction tower for extraction, an extraction phase is obtained at the top of the extraction tower, and a raffinate phase is obtained at the bottom of the extraction tower;
(2) the extracted phase enters a solvent recovery tower for separation after being decompressed by an extraction phase decompressor, the solvent and light oil are separated in the solvent recovery tower, the top of the solvent recovery tower obtains a first recovered solvent, and the bottom of the solvent recovery tower obtains light oil containing the solvent;
(3) the light oil containing the solvent enters a light oil stripping tower to be subjected to steam stripping, steam and the solvent are obtained at the top of the light oil stripping tower, a gas phase and a water phase are obtained through separation after cooling, the gas phase is a recovered solvent II, and light oil is obtained at the bottom of the tower;
(4) reducing the pressure of the raffinate phase by a raffinate phase pressure reducer, and then separating the raffinate phase in a raffinate phase solvent separation tower to obtain a third recovered solvent at the top of the raffinate phase solvent separation tower and heavy oil at the bottom of the raffinate phase solvent separation tower;
(5) heavy oil enters a heavy oil stripping tower and is subjected to steam stripping, steam and a solvent are obtained at the top of the heavy oil stripping tower, a gas phase and a water phase are obtained after cooling and separation, the gas phase is a recovered solvent IV, and asphalt is obtained at the bottom of the tower;
(6) and (3) boosting the pressure of the recovered solvent I, the recovered solvent II, the recovered solvent III and the recovered solvent IV, and collecting the mixture in a solvent tank for recycling.
In the invention, high viscosity oil (pressurized by a pressure pump) and a solvent enter an extraction tower, the solvent extracts light oil in the high viscosity oil, the light oil is taken out from the top of the tower as an extraction phase, and a raffinate phase is taken out from the bottom of the tower. The extracted phase is decompressed by an extraction phase decompressor (such as a pressure reducing valve) and enters a solvent recovery tower, most of the solvent is gasified in the tower and separated from light oil, and a recovered solvent I is obtained at the top of the solvent recovery tower. And (3) introducing the solvent-containing light oil led out from the bottom of the solvent recovery tower into a light oil stripping tower, utilizing steam to strip out the residual solvent, obtaining steam and the solvent at the top of the light oil stripping tower, cooling and separating to obtain a recovered solvent II, and obtaining light oil at the bottom of the light oil stripping tower. The raffinate phase is decompressed by a raffinate phase decompressor (such as a pressure reducing valve) and then enters a raffinate phase solvent separation tower, most of the solvent is gasified in the tower and separated from heavy oil, a recovered solvent III is obtained at the tower top, heavy oil obtained at the tower bottom is heated preferably by a heavy oil heater and then enters a heavy oil stripping tower, residual solvent is extracted by steam, a recovered solvent IV is obtained after cooling and separation, and asphalt is obtained at the bottom of the heavy oil stripping tower. The recovered solvent I, the recovered solvents II, III and IV can be recycled after the pressure is increased.
In the present invention, the viscosity of the high viscosity oil is in various conventional viscosity ranges in the art. For example, in step (1), the high viscosity oil may have a viscosity in the range of 20mPa · s to 50000mPa · s at 50 ℃.
In the present invention, the high viscosity oil is fed at a temperature of 30 to 250 ℃ for better extraction separation of heavy oil and light oil.
In the present invention, the high viscosity oil may be any of various conventional high viscosity oils in the art. For example, the high viscosity oil may be at least one of crude oil, coal tar, quench oil, residual oil, and slurry oil.
In the invention, the solvent-oil ratio is too low, the mass transfer of the solvent and the high-viscosity oil is insufficient, and the extraction effect is reduced; and the energy consumption caused by the circulation of the solvent is too high due to the fact that the ratio of the solvent to the oil is too high. In order to comprehensively consider the extraction effect and the energy consumption, in step (1), the solvent may be fed in an amount of 0.5 to 10 times, for example, 0.5 times, 0.6 times, 0.7 times, 0.8 times, 1 time, 1.5 times, 2 times, 2.5 times, 3 times, 3.5 times, 4 times, 4.5 times, 5 times, 5.5 times, 6 times, 6.5 times, 7 times, 7.5 times, 8 times, 8.5 times, 9 times, 9.5 times, 10 times, and any value in the range of any two of these point values, preferably 2 to 5 times, by weight, based on the high viscosity oil.
In the present invention, the solvent is fed at a temperature of 30 to 250 ℃ for better extraction separation of heavy oil and light oil.
In the present invention, the solvent may be any of those conventionally used in the art. For example, the solvent is a hydrocarbon having a carbon number of 2 to 6 and/or carbon dioxide.
In the invention, when the hydrocarbon with higher carbon number is selected as the solvent, the temperature of the top of the extraction tower is higher. If hydrocarbon with carbon number of 2-6 is selected as solvent, the pressure range of the extraction tower is generally controlled at 3-6 MPa; if carbon dioxide is selected as the solvent, the pressure range of the extraction tower is generally controlled to be 7-20 MPa. Therefore, in step (1), the pressure of the extraction column may be in the range of 3 to 20MPa (for example, any of 3MPa, 4MPa, 5MPa, 6MPa, 7MPa, 8MPa, 9MPa, 10MPa, 11MPa, 12MPa, 13MPa, 14MPa, 15MPa, 16MPa, 17MPa, 18MPa, 19MPa, 20MPa, and any two of these points) and the column top temperature may be in the range of 30 to 250 ℃ (for example, any of 30 ℃, 50 ℃, 80 ℃, 100 ℃, 130 ℃, 150 ℃, 180 ℃, 200 ℃, 220 ℃, 250 ℃, and any two of these points).
In the invention, part of the solvent can be mixed with the high-viscosity oil from the high-viscosity oil feed port and enter the upper part of the extraction tower, the part of the solvent can account for 0 to 90 percent of the total solvent feed amount, and preferably accounts for 0.1 to 15 percent of the total solvent feed amount, so that the addition method can reduce the viscosity of the high-viscosity oil entering the extraction tower, the high-viscosity oil can be dispersed more uniformly in the extraction tower, the mass transfer efficiency between the solvent and the high-viscosity oil is higher, and the rest of the solvent enters the lower part of the extraction tower from the solvent feed port.
In the present invention, in order to separate the most solvent from the light oil in the extract phase, it is preferable that in the step (2), the pressure of the extract phase after the pressure reduction by the extract phase vacuum apparatus is 0.1 to 3MPa, and then the extract phase is introduced into the solvent recovery column, the pressure of the solvent recovery column is preferably in the range of 0.1 to 3MPa (for example, any one of the ranges of 0.1MPa, 0.3MPa, 0.5MPa, 0.7MPa, 1.0MPa, 1.2MPa, 1.4MPa, 1.6MPa, 1.8MPa, 2.0MPa, 2.2MPa, 2.4MPa, 2.6MPa, 2.8MPa, 3.0MPa and any two of these points may be used), the temperature range is 30 to 250 ℃ (30 ℃, 50 ℃, 80 ℃, 100 ℃, 130 ℃, 150 ℃, 180 ℃, 200 ℃, 220 ℃, 250 ℃ and any two of these points are used), the most solvent is vaporized in the solvent recovery column is separated from the light oil, and the solvent recovery column is recovered at the top, the solvent-containing light oil obtained at the bottom of the solvent recovery column.
In the present invention, in order to make the steam more favorably strip out the remaining solvent, it is preferable that, in the step (3), the pressure of the light oil stripper is in the range of 0.1 to 3MPa (for example, may be any value in the range of 0.1MPa, 0.5MPa, 0.8MPa, 1MPa, 1.5MPa, 2MPa, 2.5MPa, 3MPa and any two of these values), the temperature is in the range of 100-, and obtaining a recovered solvent II.
In the present invention, in order to allow steam to be more effectively stripped of the solvent remaining in the light oil so that the viscosity of the light oil is greatly reduced from that of the original high-viscosity oil, the steam stripping is carried out with a steam feed amount of 0.1 to 5 times, by weight, the solvent-containing light oil feed amount. For example, the amount may be any value in a range of 0.1 times, 0.2 times, 0.3 times, 0.4 times, 0.5 times, 0.6 times, 0.7 times, 0.8 times, 0.9 times, 1 times, 2 times, 3 times, 4 times, 5 times, and any two of these values.
Preferably, the steam used for the steam stripping is steam generated by the water phase circulation.
In the present invention, in order to separate the majority of the solvent in the raffinate phase from the heavy oil, in the step (4), it is preferable that the pressure of the raffinate phase after being depressurized by the raffinate phase depressurizer is 0.1 to 3MPa, the depressurized raffinate phase is introduced into a raffinate phase solvent separation column for separation, the pressure of the raffinate phase solvent separation column is preferably in the range of 0.1 to 3MPa (for example, any one of the ranges of 0.1MPa, 0.3MPa, 0.5MPa, 0.7MPa, 1.0MPa, 1.2MPa, 1.4MPa, 1.6MPa, 1.8MPa, 2.0MPa, 2.2MPa, 2.4MPa, 2.6MPa, 2.8MPa, 3.0MPa and any two of these values) and the temperature range is 100 ℃ to 300 ℃ (for example, any one of the ranges of 100 ℃, 130 ℃, 150 ℃, 180 ℃, 200 ℃, 220 ℃, 250 ℃, 280 ℃, 300 ℃ and any two of these values) is included in the raffinate phase solvent separation column, most of the solvent in the raffinate phase is gasified and separated from the heavy oil, a third recovered solvent is obtained at the top of the raffinate phase solvent separation tower, and the heavy oil is led out from the bottom of the raffinate phase solvent separation tower.
In the present invention, in order to further improve the recovery rate of the solvent, before introducing the heavy oil into the heavy oil stripper, a heavy oil heater is further used to heat the heavy oil. Preferably, the heavy oil is heated to 100-.
In the present invention, in order to steam-strip the solvent remaining in the heavy oil more preferably, in step (5), the heavy oil stripper has a pressure in the range of 0.1 to 3MPa (for example, any value in the range of 0.1MPa, 0.5MPa, 0.8MPa, 1MPa, 1.5MPa, 2MPa, 2.5MPa, 3MPa, and any two of these values), a temperature in the range of 100 ° and 300 ℃ (for example, any value in the range of 100 ℃, 130 ℃, 150 ℃, 180 ℃, 200 ℃, 220 ℃, 250 ℃, 280 ℃, 300 ℃, and any two of these values), the materials (steam and solvent) obtained at the top of the heavy oil stripper reach a temperature in the range of 0 to 100 ℃ after cooling, so that the steam is condensed into water to be separated from the solvent (for example, the temperature after cooling may be any value in the range of 0 ℃, 20 ℃, 50 ℃, 80 ℃, 100 ℃, and any two of these values), thereby obtaining a recovered solvent IV.
In the present invention, the steam stripping is performed with a steam feed amount of 0.1 to 5 times the heavy oil feed amount by weight in order to better strip the solvent remaining in the heavy oil with steam. For example, the amount may be any value in a range of 0.1 times, 0.2 times, 0.3 times, 0.4 times, 0.5 times, 0.6 times, 0.7 times, 0.8 times, 0.9 times, 1 times, 2 times, 3 times, 4 times, 5 times, and any two of these values.
Preferably, the steam used for the steam stripping is steam generated by the water phase circulation.
In the invention, in order to make the heavy oil disperse more uniformly in the heavy oil stripping tower, avoid adhering to the inner wall, and improve the mass transfer efficiency, so that the stripping is easier to carry out, in step (5), the heavy oil enters the heavy oil stripping tower in the form of the mixed oil of the heavy oil obtained in step (4) and the light oil, and is subjected to steam stripping, and the feeding amount of the light oil is 0.05-0.1 time of the feeding amount of the heavy oil by weight. For example, it may be any value in the range of 0.05 times, 0.06 times, 0.07 times, 0.08 times, 0.09 times, 0.1 times, and any two of these point values. Preferably, the light oil is the light oil obtained in the step (3).
In the present invention, the heat source of the heavy oil heater is preferably the heat released from the recovered solvent during the cooling process (e.g., the cooling process of step (3) and step (5)) for better energy utilization.
In the present invention, in order to ensure the amount of solvent required for viscosity reduction, in step (6), the solvent in the solvent tank further comprises a fresh solvent for replenishment.
In the present invention, the recovered solvent one, the recovered solvent two, the recovered solvent three and the recovered solvent four may be recycled to the extraction column after being pressurized, and the specific pressure is not particularly limited. Before boosting, the recovered solvent I, the recovered solvent II, the recovered solvent III and the recovered solvent IV can be cooled by a heat exchanger until the pressurizing pump is easy to suck, and the degree of cooling can be that the first solvent, the second solvent, the third solvent and the fourth solvent are cooled to be liquid firstly.
In the invention, the raffinate phase, the heavy oil and the asphalt are conveyed by a screw pump, so that the raffinate phase, the heavy oil and the asphalt are easy to convey.
In the invention, in order to ensure good fluidity of the raffinate phase, the heavy oil and the asphalt, the temperature of a pipeline connecting the screw pump with the raffinate phase, the heavy oil and the asphalt is kept at 100-300 ℃. For example, the temperature may be, for example, 100 ℃, 130 ℃, 150 ℃, 180 ℃, 200 ℃, 220 ℃, 250 ℃, 280 ℃, 300 ℃ or any value in the range of any two of these values.
In the present invention, in order to reduce the viscosity and prevent the clogging, it is further comprised that a step light oil, for example, the light oil obtained in the step (3), is fed to the bottoms of the extraction column, the raffinate phase solvent separation column, the heavy oil heater and the heavy oil stripper and the connecting line therebetween, and the feeding amount of the light oil is 0.01 to 0.05 times the feeding amount of the high viscosity oil by weight. For example, it may be any value in the range of 0.01 times, 0.02 times, 0.03 times, 0.04 times, 0.05 times, and any two of these point values.
In conclusion, the viscosity of the high-viscosity oil product can be obviously reduced by using the viscosity reducing system for viscosity reduction, the solvent loss rate can be obviously reduced, and the problems of solvent residue in the product and environmental pollution are thoroughly solved. In addition, the energy consumption in the viscosity reducing system is comprehensively utilized, and the viscosity reducing cost is reduced.
The present invention will be described in detail below by way of examples. In the following examples:
the viscosity of the quenching oil is measured by a rotational viscosity method, and the quenching oil is used from an ethylene industrial unit;
the solvent loss rate parameter is the total amount of solvent recovered/total amount of solvent × 100%.
Example 1
1. A viscosity reducing system, as shown in fig. 1, including an extraction column 1, a solvent recovery column 4, a solvent tank 8, a suction phase pressure reducer 2 (pressure reducing valve), a light oil stripping column 5, a raffinate phase pressure reducer 3 (pressure reducing valve), a raffinate phase solvent separation column 6, a heavy oil heater 12, a heavy oil stripping column 7, and a pressure pump 9; wherein, a high-viscosity oil feeding hole and a solvent feeding hole from a solvent tank 8 are arranged on the extraction tower 1; the top of the extraction tower 1 is sequentially connected with an extraction phase decompression device 2 and a solvent recovery tower 4, the bottom of the solvent recovery tower 4 is connected with a light oil stripping tower 5, and the bottom of the light oil stripping tower 5 is provided with a light oil discharge hole; the bottom of the extraction tower 1 is sequentially connected with a raffinate phase pressure reducer 3 and a raffinate phase solvent separation tower 6, a heavy oil heater 12 is arranged at the bottom of the raffinate phase solvent separation tower 6, the heavy oil heater 12 is connected with a heavy oil stripping tower 7, and a heavy oil discharge hole is formed in the bottom of the heavy oil stripping tower 7; the tops of the solvent recovery tower 4, the light oil stripping tower 5, the raffinate phase solvent separation tower 6 and the heavy oil stripping tower 7 are respectively and sequentially connected with a heat exchanger 10, a booster pump 9 and a solvent tank 8; and a supplementary solvent feeding hole and a solvent discharging hole are formed in the solvent tank 8 and are connected with the solvent feeding hole of the extraction tower 1 through the solvent discharging hole and the heat exchanger 11.
2. The viscosity reducing method for reducing the viscosity of quenching oil with the viscosity of 1030mPa & s (measured at 50 ℃) by taking n-butane as a solvent specifically comprises the following steps:
(1) feeding quenching oil at the temperature of 150 ℃ and the flow rate of 8000kg/h into an extraction tower from a high-viscosity oil feeding hole, feeding a solvent from a solvent tank at the temperature of 150 ℃ and the flow rate of 24000kg/h into the extraction tower from the solvent feeding hole, wherein the pressure of the extraction tower is 4.5MPa, the temperature of the top of the extraction tower is 140 ℃, extracting by the extraction tower to obtain an extraction phase at the top of the extraction tower, and obtaining a raffinate phase at the bottom of the extraction tower;
(2) reducing the pressure of the extracted phase to 0.5MPa through a pressure reducing valve, then entering a solvent recovery tower (the temperature is 140 ℃ and the pressure is 0.5MPa), separating most of the solvent from light oil, obtaining a recovered solvent I at the top of the solvent recovery tower, and obtaining light oil containing the solvent at the bottom of the solvent recovery tower;
(3) the light oil containing the solvent enters the upper part of a light oil stripping tower, and is subjected to 0.5 MPa-level saturated steam stripping (by weight, the steam consumption is 0.06 times that of the light oil containing the solvent), the steam feeding amount is 300kg/h, the temperature is 150 ℃, the pressure is 0.5MPa, the light oil is obtained at the bottom of the light oil stripping tower, the viscosity is 9mPa & s, the steam and the solvent are obtained at the top, the light oil is cooled and separated into a gas-water two phase through a condenser (cooled to 40 ℃), the gas phase is the recovered solvent II, and the water phase is circulated to generate steam;
(4) reducing the pressure of the raffinate phase to 0.5MPa through a pressure reducing valve, then entering a raffinate phase solvent separation tower for raffinate phase separation (the temperature is 250 ℃ and the pressure is 0.5MPa), separating most of the solvent in the raffinate phase from the asphalt, obtaining a recovered solvent III at the top of the raffinate phase solvent separation tower, and obtaining heavy oil at the bottom of the tower;
(5) heating heavy oil to 200 ℃ by a heavy oil heater, feeding the heated heavy oil into a heavy oil stripping tower, carrying out 1MPa saturated steam stripping (the steam consumption is 0.1 time of the heavy oil by weight), wherein the steam feeding amount is 300kg/h, the temperature is 200 ℃, the pressure is 1MPa, obtaining asphalt at the bottom of the heavy oil stripping tower, obtaining steam and a solvent at the top, cooling and separating the asphalt and the solvent into a gas-water two phase by a tower top condenser (cooling to 40 ℃), wherein the gas phase is a recovered solvent IV, and the water phase generates steam in a circulating manner;
(6) and (3) converging the recovered solvent I, the recovered solvent II, the recovered solvent III and the recovered solvent IV, cooling to 20 ℃, then raising the pressure to 4.5MPa by using a pressure pump, entering a solvent tank, adjusting the temperature of the solvent led out from the solvent tank to 150 ℃ by using a heat exchanger, and recycling the solvent as the solvent of the extraction tower.
The viscosity of the quenching oil is reduced from 1030 mPas to 9 mPas by viscosity reduction, 4256kg/h of light oil is obtained, the loss of the solvent is 6kg/h, and the loss rate is 0.025 percent.
Comparative example 1
The viscosity reducing method for reducing the viscosity of quenching oil with the viscosity of 1030mPa & s (measured at 50 ℃) by taking n-butane as a solvent specifically comprises the following steps:
(1) feeding quenching oil at the temperature of 150 ℃ and the flow rate of 8000kg/h into an extraction tower from a high-viscosity oil feeding hole, feeding a solvent from a solvent tank at the temperature of 150 ℃ and the flow rate of 24000kg/h into the extraction tower from the solvent feeding hole, wherein the pressure of the extraction tower is 4.5MPa, the temperature of the top of the extraction tower is 140 ℃, extracting by the extraction tower to obtain an extraction phase at the top of the extraction tower, and obtaining a raffinate phase at the bottom of the extraction tower;
(2) reducing the pressure of the extracted phase to 0.5MPa through a pressure reducing valve, then entering a solvent recovery tower (the temperature is 140 ℃ and the pressure is 0.5MPa), separating the extracted phase into a solvent and light oil in the solvent recovery tower, obtaining a recovered solvent I at the top of the solvent recovery tower, and obtaining low-viscosity light oil at the bottom of the solvent recovery tower, wherein the viscosity of the light oil is 9 mPas;
(3) reducing the pressure of the raffinate phase to 0.5MPa through a pressure reducing valve, then feeding the raffinate phase into a raffinate phase solvent separation tower, carrying out raffinate phase temperature rise separation (the pressure is 0.5MPa), separating most of the solvent in the raffinate phase from the asphalt, obtaining a recovered solvent II at the top of the raffinate phase solvent separation tower, and obtaining the asphalt at the bottom of the tower.
The viscosity of the quenching oil is reduced from 1030 mPas to 9 mPas by viscosity reduction to obtain 4256kg/h of light oil, the loss of the solvent is 120kg/h, and the loss rate is 0.5%.
In conclusion, the viscosity reduction system of the invention is used for viscosity reduction, so that the loss rate of the solvent is greatly reduced, and the viscosity of the high-viscosity oil product is also greatly reduced.
The preferred embodiments of the present invention have been described above in detail, but the present invention is not limited thereto. Within the scope of the technical idea of the invention, many simple modifications can be made to the technical solution of the invention, including combinations of various technical features in any other suitable way, and these simple modifications and combinations should also be regarded as the disclosure of the invention, and all fall within the scope of the invention.
Claims (19)
1. A viscosity reduction system comprises an extraction tower (1), a solvent recovery tower (4) and a solvent tank (8), and is characterized by further comprising an extraction phase pressure reducer (2), a light oil stripping tower (5), a raffinate phase pressure reducer (3), a raffinate phase solvent separation tower (6), a heavy oil stripping tower (7) and a pressure pump (9); wherein, a high-viscosity oil feeding port and a solvent feeding port are arranged on the extraction tower (1); the top of the extraction tower (1) is sequentially connected with an extraction phase decompression device (2) and a solvent recovery tower (4), the bottom of the solvent recovery tower (4) is connected with a light oil stripping tower (5), and the bottom of the light oil stripping tower (5) is provided with a light oil discharge hole; the bottom of the extraction tower (1) is sequentially connected with a raffinate phase pressure reducer (3) and a raffinate phase solvent separation tower (6), the bottom of the raffinate phase solvent separation tower (6) is connected with a heavy oil stripping tower (7), and the bottom of the heavy oil stripping tower (7) is provided with a heavy oil discharge hole; the tops of the solvent recovery tower (4), the light oil stripping tower (5), the raffinate phase solvent separation tower (6) and the heavy oil stripping tower (7) are respectively connected with a pressure pump (9) and a solvent tank (8) in sequence; and a supplementary solvent feeding hole and a solvent discharging hole are formed in the solvent tank (8) and are connected with the solvent feeding hole of the extraction tower (1) through the solvent discharging hole.
2. A visbreaking system according to claim 1, wherein the tops of the solvent recovery column (4), the light oil stripper column (5), the raffinate phase solvent separation column (6) and the heavy oil stripper column (7) are connected in sequence to a heat exchanger (10), a booster pump (9) and a solvent tank (8).
3. A visbreaking system according to claim 1, wherein the solvent outlet of the solvent tank (8) is connected to the solvent inlet of the extraction column (1) via a heat exchanger (11).
4. A visbreaking system according to any one of claims 1-3, wherein a heavy oil heater (12) is further provided between the raffinate solvent separation column (6) and the heavy oil stripper column (7) to heat the heavy oil exiting the bottom of the raffinate solvent separation column (6) before it enters the heavy oil stripper column (7).
5. A method of reducing viscosity comprising the steps of:
(1) the high-viscosity oil and the solvent enter an extraction tower for extraction, an extraction phase is obtained at the top of the extraction tower, and a raffinate phase is obtained at the bottom of the extraction tower;
(2) the extracted phase enters a solvent recovery tower for separation after being decompressed by an extraction phase decompressor, the solvent and light oil are separated in the solvent recovery tower, the top of the solvent recovery tower obtains a first recovered solvent, and the bottom of the solvent recovery tower obtains light oil containing the solvent;
(3) the light oil containing the solvent enters a light oil stripping tower to be subjected to steam stripping, steam and the solvent are obtained at the top of the light oil stripping tower, a gas phase and a water phase are obtained through separation after cooling, the gas phase is a recovered solvent II, and light oil is obtained at the bottom of the tower;
(4) reducing the pressure of the raffinate phase by a raffinate phase pressure reducer, and then separating the raffinate phase in a raffinate phase solvent separation tower to obtain a third recovered solvent at the top of the raffinate phase solvent separation tower and heavy oil at the bottom of the raffinate phase solvent separation tower;
(5) heavy oil enters a heavy oil stripping tower and is subjected to steam stripping, steam and a solvent are obtained at the top of the heavy oil stripping tower, a gas phase and a water phase are obtained after cooling and separation, the gas phase is a recovered solvent IV, and asphalt is obtained at the bottom of the tower;
(6) and (3) boosting the pressure of the recovered solvent I, the recovered solvent II, the recovered solvent III and the recovered solvent IV, and collecting the mixture in a solvent tank for recycling.
6. The method according to claim 5, wherein in step (1), the high viscosity oil has a viscosity in the range of 20 mPa-s to 50000 mPa-s at 50 ℃;
preferably, the feed temperature of the high viscosity oil is 30 to 250 ℃;
preferably, the high viscosity oil is at least one of crude oil, coal tar, quench oil, residual oil, and slurry oil.
7. The process according to claim 5, wherein in step (1), the solvent is fed in an amount of 0.5 to 10 times, preferably 2 to 5 times, by weight as much as the high viscosity oil;
preferably, the high viscosity oil further comprises 0 to 90 wt% of a feed solvent;
preferably, the feed temperature of the solvent is 30-250 ℃;
preferably, the solvent is a hydrocarbon having a carbon number of 2 to 6 and/or carbon dioxide.
8. The process according to claim 5, wherein in the step (1), the pressure of the extraction column is in the range of 3 to 20MPa, and the temperature at the top of the extraction column is in the range of 30 to 250 ℃.
9. The process according to any one of claims 5 to 8, wherein in the step (2), the pressure of the extract phase after being depressurized by the extract phase depressurizer is 0.1 to 3MPa, and the pressure of the solvent recovery column is in the range of 0.1 to 3MPa and the temperature is in the range of 30 to 250 ℃.
10. The method as claimed in any one of claims 5 to 8, wherein in the step (3), the pressure of the light oil stripping tower is in the range of 0.1 to 3MPa, the temperature is in the range of 100 ℃ to 300 ℃, and the temperature of the steam and the solvent after cooling is in the range of 0 ℃ to 100 ℃;
preferably, the steam stripping is carried out with a steam feed amount of 0.1 to 5 times by weight as much as the solvent-containing light oil feed amount; preferably, the steam used for the steam stripping is steam generated by the water phase recycle.
11. The process according to any one of claims 5 to 8, wherein in the step (4), the pressure of the raffinate phase after the pressure reduction by the raffinate phase pressure reducer is 0.1 to 3MPa, the pressure of the raffinate phase solvent-separating column is in the range of 0.1 to 3MPa, and the temperature is in the range of 100 ℃ to 300 ℃.
12. The method according to any one of claims 5-8, further comprising: before introducing the heavy oil obtained in the step (4) into a heavy oil stripping tower, heating the heavy oil in a heavy oil heater;
preferably, the temperature after heating the heavy oil is 100-300 ℃.
13. The method as claimed in any one of claims 5 to 8, wherein in the step (5), the pressure of the heavy oil stripping tower is in the range of 0.1 to 3MPa, the temperature is in the range of 100 ℃ to 300 ℃, and the cooled temperature of the steam and the solvent is in the range of 0 ℃ to 100 ℃;
preferably, the steam stripping is carried out with a steam feed amount of 0.1 to 5 times the heavy oil feed amount by weight; preferably, the steam used for the steam stripping is steam generated by the water phase recycle.
14. The method as claimed in any one of claims 5 to 8, wherein in the step (5), the heavy oil is steam-stripped by feeding a mixed oil of the heavy oil obtained in the step (4) and light oil in an amount of 0.05 to 0.1 times the feeding amount of the heavy oil by weight.
15. The method of claim 12, wherein the heat source of the heavy oil heater is the heat released by the step (3) cooling process and/or the heat released by the step (5) cooling process.
16. The method of any one of claims 5 to 8, wherein in step (6), the solvent in the solvent tank further comprises make-up fresh solvent.
17. The method according to any one of claims 5 to 8, wherein the raffinate phase, heavy oil and bitumen are delivered using a progressive cavity pump.
18. The method as claimed in claim 17 wherein the tubing connecting the screw pump to the raffinate phase, heavy oil, bitumen is maintained at a temperature of 100 ℃ to 300 ℃.
19. The method as set forth in any one of claims 5 to 8, further comprising feeding a light oil to bottoms of the extraction column, the raffinate phase solvent separation column, the heavy oil heater and the heavy oil stripping column and a connection line therebetween, wherein a feeding amount of the light oil is 0.01 to 0.05 times as large as a feeding amount of the high viscosity oil by weight.
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| CN1884150A (en) * | 2006-06-23 | 2006-12-27 | 华南理工大学 | Method for treating coal gasification wastewater by single-tower pressurization stripping and device therefor |
| CN101168492A (en) * | 2006-10-27 | 2008-04-30 | 北京金伟晖工程技术有限公司 | Aromatic hydrocarbons extraction system and method thereof |
| CN103305259A (en) * | 2012-03-16 | 2013-09-18 | 中国石油化工股份有限公司 | Method for reducing viscosity of quenching oil of ethylene unit |
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| CN1884150A (en) * | 2006-06-23 | 2006-12-27 | 华南理工大学 | Method for treating coal gasification wastewater by single-tower pressurization stripping and device therefor |
| CN101168492A (en) * | 2006-10-27 | 2008-04-30 | 北京金伟晖工程技术有限公司 | Aromatic hydrocarbons extraction system and method thereof |
| CN103305259A (en) * | 2012-03-16 | 2013-09-18 | 中国石油化工股份有限公司 | Method for reducing viscosity of quenching oil of ethylene unit |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN115477958A (en) * | 2021-06-16 | 2022-12-16 | 中国石油化工股份有限公司 | Quenching oil viscosity reducing system and method |
| CN115477958B (en) * | 2021-06-16 | 2024-03-19 | 中国石油化工股份有限公司 | Quenching oil viscosity reducing system and method |
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