CN114106874A - Method and device for pyrolysis deacidification of high-acid crude oil or high-acid residual oil - Google Patents
Method and device for pyrolysis deacidification of high-acid crude oil or high-acid residual oil Download PDFInfo
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- CN114106874A CN114106874A CN202010881202.7A CN202010881202A CN114106874A CN 114106874 A CN114106874 A CN 114106874A CN 202010881202 A CN202010881202 A CN 202010881202A CN 114106874 A CN114106874 A CN 114106874A
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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
- C10G55/00—Treatment of hydrocarbon oils, in the absence of hydrogen, by at least one refining process and at least one cracking process
- C10G55/02—Treatment of hydrocarbon oils, in the absence of hydrogen, by at least one refining process and at least one cracking process plural serial stages only
- C10G55/04—Treatment of hydrocarbon oils, in the absence of hydrogen, by at least one refining process and at least one cracking process plural serial stages only including at least one thermal cracking 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
- C10G2300/20—Characteristics of the feedstock or the products
- C10G2300/201—Impurities
- C10G2300/202—Heteroatoms content, i.e. S, N, O, P
Abstract
The invention discloses a method and a device for pyrolysis deacidification of high-acid crude oil or high-acid residual oil. The method comprises the following steps: inputting the heated raw materials into a gas-liquid separation tank, and separating water and light gas oil; the raw materials of separated water and light gas oil flow out from the bottom of the gas-liquid separation tank and flow out from the bottom of the shallow thermal cracking reaction tower and enter the top of the shallow thermal cracking reaction tower, and the shallow thermal cracking product oil, namely the deacidification product, is obtained after quenching. By applying the technical scheme of the invention, a shallow thermal cracking process is adopted, high-acid crude oil or high-acid residual oil is taken as a raw material, the viscosity of oil generated by shallow thermal cracking is reduced, the acid value is greatly reduced, the reduction amplitude can reach more than 90 percent, and deacidified products meet the acid value requirement of fuel oil products, preferably, the naphthenic acid corrosion of equipment can be reduced by using the high-acid crude oil or the high-acid residual oil as the raw material and preferably, the reaction temperature is 370-450 ℃, the retention time is 20-200 minutes, and the reaction pressure is normal pressure to 1.0 MPa.
Description
Technical Field
The invention relates to the technical field of petroleum processing, in particular to a method and a device for pyrolysis deacidification of high-acid crude oil or high-acid residual oil.
Background
With the rapid increase in global high acid crude oil production, the proportion of high acid crude oil in the total crude oil production increases year by year. Because the price of the high-acid crude oil is low, the refining enterprises can obtain higher profits for processing the high-acid crude oil, and therefore, the processing technology of the high-acid crude oil is widely concerned. The crude oil or residual oil with the acid value higher than 1.0mgkOH/g is generally called high-acid crude oil or high-acid residual oil, the high-acid crude oil is generally thick oil and is also called high-acid thick oil or thick oil, the domestic high-acid thick oil has low sulfur content which is generally lower than 0.5 percent compared with that of foreign countries, for example, the sulfur content of Liaohe super thick oil, Liaohe low-condensation thick oil, Liaohe mixed thick oil, Craya super thick oil, Zhonghai 36-1 thick oil and the like is 0.15 to 0.25 percent, the sulfur content of the residual oil is also low, and the method is suitable for producing residual fuel oil such as low-sulfur bunker fuel oil by a viscosity-reducing cracking method, but the acid value of the high-acid crude oil or high-acid residual oil is limited by the acid value index of the bunker fuel oil for ships, and the acid value of the high-acid residual oil must be reduced to the index requirement. In addition, when the conventional process is adopted to process the high-acid crude oil, the high-acid crude oil has the characteristics of high acid value, high density, high viscosity, high carbon residue, high metal content and the like, so that the yield of the light oil fraction is low, the quality is poor, the light oil fraction can not be directly used as a product or a blending component of the product without refining, and meanwhile, the serious corrosion problem of equipment and pipelines also causes great risk to the safe and stable operation of the device.
In view of the strong corrosion of petroleum acid during the processing, in order to reduce and avoid the corrosion of equipment during the processing of petroleum acid and to meet the quality requirements of some petroleum products, methods such as blending crude oil with low acid value and high acid value, adding chemical agents for neutralization, esterification deacidification, extraction separation deacidification by chemical reaction solvents and the like are generally adopted in the prior art to reduce the acid value of the crude oil, and the equipment is made of acid-resistant materials during the processing.
For example, patent CN106701153A provides a deacidification process for high acid crude oil, in which high acid crude oil and deacidification agent are added into a supergravity machine according to a preset volume ratio to continuously react to obtain an intermediate product; and (4) carrying out oil-water separation on the intermediate product to obtain the deacidified crude oil. The method can reduce the acid value of crude oil to below 0.5mgKOH/g, and reach the standard of low-acid crude oil, but is difficult to realize industrially.
The patent CN 103788999B provides a pretreatment method of high-acid crude oil, which utilizes the characteristic that the high-acid crude oil is easy to emulsify, mixes water and the high-acid crude oil, enters a water thermal cracking reactor for treatment, and the high-acid crude oil is deacidified and cracked at a higher temperature, and is accompanied with demulsification, so that dehydration and desalination are realized, and the corrosion problem in the treatment process can be effectively solved. The method needs to be carried out at the temperature of 260-340 ℃, the reaction pressure of 5.0-20.0 MPa and the volume space velocity of 1.0h-1～8.0h-1The process is carried out under harsh conditions, and industrial devices are difficult to realize.
The patent CN101785992B is a catalyst for reducing the acid value of crude oil, the decomposition deacidification catalyst is obtained by uniformly mixing three components of magnesium aluminum hydrotalcite, gamma-alumina and pseudo-boehmite according to a certain proportion, adding a proper amount of water, then forming, and roasting the formed catalyst for 3-8 hours at 500-600 ℃. At one endLoading the above catalyst into a fixed bed reactor in laboratory, feeding with metering pump, and using vacuum second-line distillate oil with acid value of 3.6mgKOH/g, reaction pressure is normal pressure, reaction temperature is 300 deg.C, and space velocity is 1hr-1Then, after stable operation for 4hr, the acid value of the crude oil was measured to be 0.16mgKOH/g, and the deacidification rate was measured to be 95.6%. The method is a laboratory result, the industrial cost is high, and the adaptability of the catalyst to thickened oil with high acid value is yet to be verified.
The method only aims at the method for reducing the acid value of the high-acid crude oil or the high-acid distillate oil, no effective method for reducing the acid value of the high-acid residual oil serving as the raw material exists at present, industrial production shows that the viscosity and the acid value of the raw material can be reduced by a viscosity breaking method, but the reduction of the acid value of a viscosity reducing product is limited, the existing technology for reducing the acid value of the high-acid crude oil cannot be effectively applied to an industrial production device, the problem of corrosion to equipment during processing the high-acid crude oil is still solved, for the high-acid heavy oil or the residual oil with the acid value of 4 mgKOH/g-13 mgKOH/g, the prior art cannot reduce the acid value of the raw material to be less than 0.5mgKOH/g in the industrial device, even the index of meeting the requirement of the acid value of a low-sulfur ship fuel product to be less than 2.5mgKOH/g is difficult, and a practical method for reducing the acid value of the high-acid crude oil or the high-acid residual oil is urgently needed.
Disclosure of Invention
The invention aims to provide a method and a device for pyrolysis deacidification of high-acid crude oil or high-acid residual oil, which aim to solve the technical problems that the acid value of the high-acid crude oil or the high-acid residual oil in the prior art is reduced to a small extent, the acid value requirement of a product is not met or equipment corrosion is caused by subsequent processing.
In order to achieve the above object, the present invention provides a method for the thermal decomposition deacidification of high acid crude oil or high acid residual oil. The method comprises the following steps: inputting the heated raw materials into a gas-liquid separation tank, and separating water and light gas oil; the raw materials of separated water and light gas oil flow out from the bottom of the gas-liquid separation tank and enter the shallow thermal cracking reaction tower, flow out from the bottom of the shallow thermal cracking reaction tower and enter the top of the shallow thermal cracking reaction tower, and the raw materials are quenched to obtain the shallow thermal cracking product oil, namely the deacidification product.
Further, the raw material is heated in a heating furnace before being input into the gas-liquid separation tank, and water with the mass fraction of 0.5-0.7% of the raw material is injected into the heating furnace.
Furthermore, the inlet material temperature of the shallow thermal cracking reaction tower is 370-450 ℃.
Furthermore, the retention time of the raw materials in the shallow thermal cracking reaction tower is 20-200 minutes.
Furthermore, the pressure of the top of the shallow thermal cracking reaction tower is between normal pressure and 1.0 MPa.
Further, the acid value of the high acid crude oil or the high acid residual oil is more than 1.0mgkOH/g, and preferably 4mgKOH/g to 13 mgKOH/g.
Further, injecting gas into the lower part of a feed inlet of the gas-liquid separation tank for stripping; preferably, the gas is refinery dry gas; the injection amount of the gas is 0-1.0% of the mass fraction of the raw material, and preferably, the injection amount of the gas is 0.1-0.5% of the mass fraction of the raw material; preferably, the temperature of the gas is 380 ℃ to 500 ℃.
According to another aspect of the invention, a device for the pyrolysis deacidification of high-acid crude oil or high-acid residual oil is provided. The device includes: the heating furnace is provided with a heating furnace raw material inlet and a heating furnace raw material outlet; the gas-liquid separation tank is provided with a gas-liquid separation tank raw material inlet and a gas-liquid separation tank raw material outlet, the gas-liquid separation tank raw material inlet is arranged at the middle upper part of the gas-liquid separation tank, the outlet is arranged at the bottom of the gas-liquid separation tank, and the heating furnace raw material outlet is communicated with the gas-liquid separation tank raw material inlet; and the shallow thermal cracking reaction tower is provided with a shallow thermal cracking reaction tower inlet and a shallow thermal cracking reaction tower outlet, the shallow thermal cracking reaction tower inlet is arranged at the bottom of the shallow thermal cracking reaction tower, and the gas-liquid separation tank raw material outlet is communicated with the shallow thermal cracking reaction tower inlet.
Further, a stripping gas inlet is arranged at the lower part of the raw material inlet of the gas-liquid separation tank.
Further, the top of the gas-liquid separation tank is provided with a water vapor and light gas oil outlet; preferably, the top effluent line of the shallow thermal cracking reactor is provided with a quench oil injection port and a deacidified product stream outlet.
By applying the technical scheme of the invention, a shallow thermal cracking process is adopted, high-acid crude oil or high-acid residual oil is taken as a raw material, the viscosity of oil generated by shallow thermal cracking is reduced while the acid value of the oil is reduced from 4 mgKOH/g-13 mgKOH/g of the raw material to below 0.4 mgKOH/g-1.3 mgKOH/g under the conditions that the reaction temperature is 370-450 ℃, the retention time is 20-200 minutes and the overhead pressure of a shallow thermal cracking reaction tower is normal pressure-1.0 MPa, so that the acid value reduction rate is more than 90 percent, the acid value requirement of a fuel oil product is met, or the naphthenic acid corrosion of equipment can be reduced by performing subsequent processing as the raw material.
Drawings
The accompanying drawings, which are incorporated in and constitute a part of this application, illustrate embodiments of the invention and, together with the description, serve to explain the invention and not to limit the invention. In the drawings:
fig. 1 shows a schematic flow diagram of a process for the thermal pyrolysis deacidification of high acid crude oil or high acid residue according to an embodiment of the present invention, wherein 1. high acid crude oil or high acid residue; 2. heating furnace; 3. a gas-liquid separation tank; 4. a shallow thermal cracking reaction tower; 5. deacidifying the product; 6. stripping gas; 7. water and light gas oil; 8. quenching oil.
Detailed Description
It should be noted that the embodiments and features of the embodiments in the present application may be combined with each other without conflict. The present invention will be described in detail below with reference to the embodiments with reference to the attached drawings.
According to an exemplary embodiment of the present invention, a method for thermal de-acidification of a high acid crude oil or a high acid residual oil is provided. The method comprises the following steps: inputting the heated raw materials into a gas-liquid separation tank, and separating water and light gas oil; the raw materials of separated water and light gas oil flow out from the bottom of the gas-liquid separation tank and flow out from the bottom of the shallow thermal cracking reaction tower and enter the top of the shallow thermal cracking reaction tower, and the deacidification product is obtained after quenching.
By applying the technical scheme of the invention, a shallow thermal cracking process is adopted, high-acid crude oil or high-acid residual oil is taken as a raw material, preferably, the viscosity of the oil generated by shallow thermal cracking is reduced under the conditions of reaction temperature of 370-450 ℃, residence time of 20-200 minutes and pressure of normal pressure of 1.0MPa, the acid value can be reduced to below 0.4-1.3 mgKOH/g from 4-13 mgKOH/g of the raw material, and the reduction of the acid value can reach more than 90 percent, so that the acid value requirement of a fuel oil product is met, or the naphthenic acid corrosion of equipment can be reduced by performing subsequent processing as the raw material.
Preferably, the raw material is heated in a heating furnace before being input into the gas-liquid separation tank, and water with the mass fraction of 0.5-0.7% of the raw material is injected into the heating furnace, so that the furnace tube of the heating furnace is prevented from coking. The gas-liquid separation tank removes water and light gas oil components.
Preferably, the temperature of the raw material at the inlet of the shallow thermal cracking reaction tower is 370-450 ℃, and the retention time of the raw material in the shallow thermal cracking reaction tower is 20-200 minutes, so that the reaction is fully carried out.
In one embodiment of the present invention, the acid value of the highly acidic crude oil or the highly acidic residual oil is more than 1.0mgkOH/g, preferably 4mgKOH/g to 13 mgKOH/g. Preferably, gas is injected into the lower part of the feed inlet of the gas-liquid separation tank for stripping; more preferably, the gas is refinery dry gas; the injection amount of the gas is 0-1.0% of the mass fraction of the raw material; the temperature of the gas is 380-500 ℃, so that the water and the light gas oil in the gas-liquid separation tank can be removed more thoroughly.
According to an exemplary embodiment of the present invention, an apparatus for thermal de-acidification of high acid crude oil or high acid residual oil is provided. The device comprises a heating furnace, a gas-liquid separation tank and a shallow thermal cracking reaction tower, wherein the heating furnace is provided with a heating furnace raw material inlet and a heating furnace raw material outlet; the gas-liquid separation tank is provided with a gas-liquid separation tank raw material inlet and a gas-liquid separation tank raw material outlet, the gas-liquid separation tank raw material outlet is arranged at the bottom of the gas-liquid separation tank, and the heating furnace raw material outlet is communicated with the gas-liquid separation tank raw material inlet; the shallow thermal cracking reaction tower is provided with a shallow thermal cracking reaction tower inlet and a shallow thermal cracking reaction tower outlet, the shallow thermal cracking reaction tower inlet is arranged at the bottom of the shallow thermal cracking reaction tower, and the gas-liquid separation tank raw material outlet is communicated with the shallow thermal cracking reaction tower inlet.
Preferably, the lower part of the raw material inlet of the gas-liquid separation tank is provided with a stripping gas inlet; the top of the gas-liquid separation tank is provided with a water and light gas oil outlet; the top outflow pipeline of the shallow thermal cracking reaction tower is provided with a quenching oil filling opening and a deacidification product outflow opening.
In a typical embodiment of the present invention, as shown in fig. 1, a highly acidic crude oil or residue 1 is heated in a heating furnace 2 and then introduced into a gas-liquid separation tank 3 to separate water and light gas oil 7; the lower part of the feed inlet of the gas-liquid separation tank 3 is injected with stripping gas 6 for stripping, so that the separation is more thorough, the raw materials of separated water and light gas oil flow out from the bottom of the gas-liquid separation tank 3 and flow out from the bottom of the shallow thermal cracking reaction tower 4 to the top, and the deacidification product 5 is obtained after quenching (quenching by the quenching oil 8).
The following examples are provided to further illustrate the advantageous effects of the present invention.
Example 1
The acid value of Liaohe super-thick oil is 10.5mgKOH/g, the invention injects water 0.5 m% into a heating furnace, the retention time of the raw material in a shallow thermal cracking reaction tower is 180 minutes, the pressure of the tower top is 0.7MPa, the heated raw material enters a gas-liquid separation tank, the temperature of the raw material after removing water and light gas oil is 370 ℃, the raw material enters from the bottom of the shallow thermal cracking reaction tower, flows out from the top of the shallow thermal cracking reaction tower, and is quenched to obtain an oil product generated by the shallow thermal cracking reaction, the quenching oil is the oil generated by the shallow thermal cracking reaction after heat exchange and water cooling, the acid value of the oil product generated by the shallow thermal cracking reaction is 1.0mgKOH/g, and the acid value reduction rate is 90.48%.
Comparative example 1
The acid value of the Liaohe super-thick oil is 10.5mgKOH/g, the existing visbreaking technology is adopted, 0.5 m% of water is injected into a heating furnace, the residence time of a visbreaking tower is 180 minutes, the pressure of the top of the visbreaking tower is 0.7MPa, the heated raw material enters from the bottom of the visbreaking tower, the temperature is 370 ℃, the raw material flows out from the top of the visbreaking tower, the raw material is quenched to obtain a visbreaking product oil, the quenching oil is the oil which is obtained by carrying out heat exchange and water cooling on the shallow thermal cracking reaction product oil, the acid value of the shallow thermal cracking product oil is 5.3mgKOH/g, and the reduction rate of the acid value is 49.5%.
Example 2
The acid value of Liaohe super-thick oil is 10.5mgKOH/g, the invention injects water 0.5 m% into a heating furnace, the raw material stays in a visbreaking tower for 20 minutes, the pressure of the visbreaking tower top is 0.7MPa, the heated raw material enters a gas-liquid separating tank, the lower part of the gas-liquid separating tank is injected with stripping gas, the stripping gas is refinery dry gas, the injection amount is 0.5 m% of the raw material, the temperature of the raw material after water and light gas oil are removed is 450 ℃, the stripping gas enters from the bottom of a shallow thermal cracking reaction tower, flows out from the top of the shallow thermal cracking reaction tower, and is quenched to obtain an oil product after the shallow thermal cracking reaction is cooled by heat exchange water, the acid value of the oil product generated by the shallow thermal cracking reaction is 0.3mgKOH/g, and the reduction rate of the acid value is 97.1%.
Comparative example 2
The acid value of the Liaohe super-thick oil is 10.5mgKOH/g, the existing visbreaking technology is adopted, 0.5 m% of water is injected into a heating furnace, the water stays for 20 minutes, the pressure of the top of the visbreaking tower is 0.7MPa, the heated raw material enters from the bottom of the visbreaking tower, the temperature is 450 ℃, the raw material flows out from the top of the visbreaking tower, the visbreaking oil product is obtained after quenching, the quenching oil is the oil which is generated by the shallow thermal cracking reaction and is subjected to heat exchange and water cooling, the acid value of the oil product generated by the shallow thermal cracking reaction is 3.2mgKOH/g, and the reduction rate of the acid value is 69.5%.
Example 3
The acid value of certain vacuum residue is 6.2mgKOH/g, the invention is adopted to inject water into a heating furnace by 0.6m percent, the raw material stays in a shallow thermal cracking reaction tower for 30 minutes, the pressure of the top of the shallow thermal cracking reaction tower is 0.8MPa, the heated raw material enters a gas-liquid separation tank, the lower part of the gas-liquid separation tank is injected with stripping gas, the stripping gas is refinery dry gas, the injection amount is 1.0m percent of the raw material, the temperature of the raw material after water and light gas oil are removed is 440 ℃, the stripping gas enters from the bottom of the shallow thermal cracking reaction tower and flows out from the top of the shallow thermal cracking reaction tower, the oil product is obtained after the shallow thermal cracking reaction after quenching, the quenching oil is the oil which is the oil generated after the water cooling and heat exchange, the acid value is 0.2mgKOH/g, and the reduction rate of the acid value is 96.7 percent.
Comparative example 3
The acid value of certain vacuum residue is 6.2mgKOH/g, the existing visbreaking technology is adopted, water is injected into a heating furnace for 0.6m percent, the residence time is 30 minutes, the pressure at the top of the visbreaking tower is 0.7MPa, the heated raw material enters from the bottom of the visbreaking tower, the temperature is 440 ℃, the raw material flows out from the top of the visbreaking tower, the visbreaking generated oil product is obtained after quenching, the quenching oil is the oil generated by the shallow thermal cracking reaction and subjected to heat exchange and water cooling, the acid value of the oil generated by the shallow thermal cracking reaction is 2.9mgKOH/g, and the reduction rate of the acid value is 53.2 percent.
Example 4
The acid value of certain residual oil is 4.7mgKOH/g, the invention is adopted to inject water into a heating furnace by 0.7m percent, the raw material stays in a shallow thermal cracking reaction tower for 40 minutes, the pressure of the top of the shallow thermal cracking reaction tower is 0.7MPa, the heated raw material enters a gas-liquid separation tank, stripping gas is injected into the lower part of the gas-liquid separation tank and is refinery dry gas, the injection amount is 0.1m percent of the raw material, the temperature of the raw material after water and light gas oil are removed is 430 ℃, the stripping gas enters from the bottom of the shallow thermal cracking reaction tower and flows out from the top of the shallow thermal cracking reaction tower, the shallow thermal cracking reaction product is obtained after quenching, the quenching oil is the oil which is generated after the oil is subjected to heat exchange and water cooling, the acid value of the oil product generated by the shallow thermal cracking reaction is 0.3mgKOH/g, and the reduction rate of the acid value is 93.6%.
From the above description, it can be seen that the above-described embodiments of the present invention achieve the following technical effects: the method and the equipment of the invention can produce the fuel oil product with low acid value or the blending component thereof by taking high-acid heavy oil or high-acid residual oil as raw materials.
The above description is only a preferred embodiment of the present invention and is not intended to limit the present invention, and various modifications and changes may be made by those skilled in the art. Any modification, equivalent replacement, or improvement made within the spirit and principle of the present invention should be included in the protection scope of the present invention.
Claims (10)
1. A method for pyrolysis deacidification of high-acid crude oil or high-acid residual oil is characterized by comprising the following steps:
inputting the heated raw materials into a gas-liquid separation tank, and separating water and light gas oil;
and the raw materials of separated water and light gas oil flow out of the bottom of the gas-liquid separation tank and enter a shallow thermal cracking reaction tower, flow out of the bottom of the shallow thermal cracking reaction tower and enter the top of the shallow thermal cracking reaction tower, and are quenched to obtain shallow thermal cracking oil, namely a deacidification product.
2. The method according to claim 1, wherein the raw material is heated in a heating furnace before being introduced into the gas-liquid separation tank, and water is injected into the heating furnace in a mass fraction of 0.5 to 0.7% of the raw material.
3. The method as claimed in claim 1, wherein the inlet feed temperature of the shallow thermal cracking reaction tower is 370 ℃ to 450 ℃.
4. The method of claim 1, wherein the residence time of the feedstock in the shallow thermal cracking reactor is between 20 minutes and 200 minutes.
5. The method as claimed in claim 1, wherein the overhead pressure of the shallow thermal cracking reactor is from atmospheric pressure to 1.0 MPa.
6. The process according to claim 1, wherein the acid value of the high acid crude oil or high acid residue is more than 1.0mgkOH/g, preferably 4mgkOH/g to 13 mgkOH/g.
7. The method according to claim 1, wherein stripping is performed by injecting gas into the lower part of the feed inlet of the gas-liquid separation tank;
preferably, the gas is refinery dry gas;
the injection amount of the gas is 0-1.0% of the mass fraction of the raw material;
preferably, the injection amount of the gas is 0.1 to 0.5% of the mass fraction of the raw material;
preferably, the temperature of the gas is 380 ℃ to 500 ℃.
8. A device for pyrolysis deacidification of high acid crude oil or high acid residual oil is characterized by comprising:
the heating furnace is provided with a heating furnace raw material inlet and a heating furnace raw material outlet;
the gas-liquid separation tank is provided with a gas-liquid separation tank raw material inlet and a gas-liquid separation tank raw material outlet, the gas-liquid separation tank raw material inlet is arranged at the middle upper part of the gas-liquid separation tank, the outlet is arranged at the bottom of the gas-liquid separation tank, and the heating furnace raw material outlet is communicated with the gas-liquid separation tank raw material inlet; and
the shallow thermal cracking reaction tower is provided with a shallow thermal cracking reaction tower inlet and a shallow thermal cracking reaction tower outlet, the shallow thermal cracking reaction tower inlet is arranged at the bottom of the shallow thermal cracking reaction tower, and the gas-liquid separation tank raw material outlet is communicated with the shallow thermal cracking reaction tower inlet.
9. The apparatus according to claim 8, wherein a stripping gas inlet is provided at a lower portion of the raw material inlet of the gas-liquid separation tank.
10. The apparatus of claim 8, wherein a top of the gas-liquid separation tank is provided with a water vapor and light gas oil outflow port;
preferably, the top effluent line of the shallow thermal cracking reaction column is provided with a quench oil injection port and a deacidified product effluent port.
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