CN112745933B - Method and device for separating and desulfurizing catalytic cracking light products - Google Patents
Method and device for separating and desulfurizing catalytic cracking light products Download PDFInfo
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- CN112745933B CN112745933B CN201911049459.XA CN201911049459A CN112745933B CN 112745933 B CN112745933 B CN 112745933B CN 201911049459 A CN201911049459 A CN 201911049459A CN 112745933 B CN112745933 B CN 112745933B
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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
- C10G67/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only
- C10G67/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only
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- 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
- C10G69/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process
- C10G69/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process plural serial stages only
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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
- C10G70/00—Working-up undefined normally gaseous mixtures obtained by processes covered by groups C10G9/00, C10G11/00, C10G15/00, C10G47/00, C10G51/00
- C10G70/04—Working-up undefined normally gaseous mixtures obtained by processes covered by groups C10G9/00, C10G11/00, C10G15/00, C10G47/00, C10G51/00 by physical processes
- C10G70/046—Working-up undefined normally gaseous mixtures obtained by processes covered by groups C10G9/00, C10G11/00, C10G15/00, C10G47/00, C10G51/00 by physical processes by adsorption, i.e. with the use of solids
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- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/10—Feedstock materials
- C10G2300/1037—Hydrocarbon fractions
- C10G2300/104—Light gasoline having a boiling range of about 20 - 100 °C
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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
- C10G2300/1037—Hydrocarbon fractions
- C10G2300/1044—Heavy gasoline or naphtha having a boiling range of about 100 - 180 °C
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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
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
- C10G2400/02—Gasoline
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
- C10G2400/26—Fuel gas
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Abstract
A method and apparatus for desulfurizing and separating light products of catalytic cracking, introduce the crude gasoline from catalytic cracking unit fractionating tower into the first desulfurization reactor, the rich gas enters the second desulfurization reactor, the rich gas after desulfurization enters the absorber from the bottom, contact with crude gasoline after desulfurization that the absorbing tower introduces on the top of the tower and absorb, the material flow enters the reabsorption tower from the bottom, contact and absorb with the light diesel oil countercurrent flow from catalytic cracking fractionating tower, get the dry gas after desulfurization on the top of the reabsorption tower, the rich light diesel oil that the reabsorption tower gets on the bottom of the tower returns to the catalytic cracking fractionating tower; and (3) conveying the tower bottom product of the absorption tower to a stabilizing tower after passing through a desorption tower, fractionating in the stabilizing tower to obtain desulfurized liquefied gas and stabilized gasoline, and returning the tower top gas of the desorption tower to the absorption tower. The method provided by the invention is suitable for treating rich gas and crude gasoline obtained by a catalytic cracking fractionating tower, and the obtained refined gasoline has high yield and less octane value loss.
Description
Technical Field
The invention belongs to the field of petrochemical industry, relates to a hydrocarbon oil desulfurization method and a device, and more particularly relates to a catalytic cracking rich gas and crude gasoline desulfurization and separation method and a device.
Background
The catalytic cracking unit of an oil refinery is a main source of low-carbon olefin, liquefied gas and gasoline, and in the existing catalytic cracking process flow, components such as rich gas, crude gasoline, light diesel oil, heavy diesel oil, oil slurry and the like can be obtained after the reaction product of the catalytic cracking unit is fractionated. The rich gas passes through the absorption desorption tower and the reabsorption tower to obtain a dry gas product, and the dry gas can be used as refinery fuel gas after being desulfurized. The crude gasoline can be separated by an absorption stabilizer to obtain liquefied gas and catalytic cracking stable gasoline, the catalytic cracking gasoline is desulfurized and then leaves a factory as a product, the liquefied gas can be desulfurized and then leaves a factory as a product, and meanwhile, the liquefied gas can be used as a raw material to provide high-value components such as propylene, butylene and the like for other devices.
Both dry gas, liquefied gas and catalytically cracked gasoline must be desulfurized under increasingly stringent environmental regulations and downstream process requirements. At present, the desulfurization processes of dry gas, liquefied gas and catalytic gasoline are respectively carried out under the limitation of a desulfurization process, and a large amount of waste liquid, waste residues and the like are generated again in the process of alkali washing desulfurization and the like commonly used for the dry gas and the liquefied gas. In addition, the prior liquefied gas desulfurization process has the problems of over-high sulfur content caused by insufficient desulfurization depth, and further limitation on further application.
The hydrocarbon oil adsorbing and desulfurizing process is one technological process of adsorbing and desulfurizing light hydrocarbon oil in the presence of hydrogen, and includes capturing sulfur in oil onto adsorbent and continuous regeneration of sulfur-containing adsorbent for reuse. The method has the characteristics of high desulfurization depth, low hydrogen consumption and the like, and can produce the fuel oil with the sulfur content of less than 30 micrograms/gram. The process for treating the catalytic cracked stable gasoline has the problems of low liquid yield of catalytic cracked products and large loss of gasoline octane number.
Disclosure of Invention
The invention aims to solve the technical problems of low yield and high octane value loss of stable gasoline produced by a catalytic cracking device, and provides a method for adsorbing, desulfurizing and separating catalytic cracking light products to obtain desulfurized dry gas, desulfurized liquefied gas and catalytic cracking stable gasoline.
The invention also provides a device for desulfurizing and separating the catalytic cracking light product.
The invention provides a method for desulfurizing and separating catalytic cracking light products, which is characterized in that crude gasoline and a hydrogen donor from a fractionating tower of a catalytic cracking unit are introduced into the bottom of a first desulfurization reactor, contact with a desulfurization adsorbent for desulfurization and flow upwards; the desulfurization adsorbent carrying partial sulfur obtained by gas-solid separation at the top of the reactor enters a second desulfurization reactor; introducing rich gas and hydrogen donor from the catalytic cracking fractionating tower into the bottom of the second desulfurization reactor, contacting with a desulfurization adsorbent for desulfurization, and returning reaction oil gas separated from the desulfurization adsorbent after reaction to the first desulfurization reactor;
reaction oil gas obtained by gas-solid separation of the first desulfurization reactor is separated into desulfurized rich gas and crude gasoline, the desulfurized rich gas enters the absorption tower from the bottom and is absorbed by contacting with the desulfurized crude gasoline introduced from the top of the absorption tower, material flow at the top of the absorption tower enters the reabsorption tower from the bottom and is absorbed by countercurrent contact with light diesel oil from the catalytic cracking fractionating tower, desulfurized dry gas is obtained at the top of the reabsorption tower, and the light diesel oil obtained at the bottom of the reabsorption tower returns to the catalytic cracking fractionating tower; the bottom product of the absorption tower passes through a desorption tower and is sent to a stabilization tower, the product is fractionated in the stabilization tower to obtain desulfurized liquefied gas and stabilized gasoline, and the gas at the top of the desorption tower returns to the absorption tower.
A method for producing low-sulfur light oil products by catalytic cracking comprises introducing catalytic cracking raw materials into a riser reactor, contacting with a catalytic cracking catalyst, reacting under the catalytic cracking reaction condition, carrying out gas-solid separation on the top of the riser reactor, introducing the obtained reaction oil gas into a catalytic cracking fractionating tower, and fractionating to obtain rich gas, crude gasoline, light diesel oil, diesel oil and oil slurry; the separated catalytic cracking catalyst is regenerated and then returned to the riser reactor for recycling; and respectively introducing the rich gas and the crude gasoline into a first desulfurization reactor and a second desulfurization reactor of an adsorption desulfurization reaction unit, and performing adsorption desulfurization and absorption stabilization separation by adopting the method to obtain desulfurized dry gas, desulfurized liquefied gas and stabilized gasoline.
A catalytic cracking light product separation and desulfurization device comprises an adsorption desulfurization unit and an absorption stabilization unit which are communicated in sequence; the adsorption desulfurization unit comprises a first desulfurization reactor, a second desulfurization reactor, a reactor receiver, a lock hopper, a regenerator feeding tank, an adsorbent regenerator and a regenerator receiver which are sequentially communicated, wherein the regenerator receiver is sequentially communicated with the lock hopper and the adsorbent reducer, and the adsorption reducer is communicated with the bottom of the first desulfurization reactor; the absorption stabilizing unit consists of an absorption tower, a desorption tower, a reabsorption tower and a stabilizing tower which are sequentially communicated; the top of the first desulfurization reactor is provided with a settling separation section, the bottom of the settling separation section is communicated with the lower part of the second desulfurization reactor, and the top of the second desulfurization reactor is communicated with the settling separation section; the outlet at the top of the first desulfurization reactor is communicated with the gas-liquid separation tank, the gas outlet of the gas-liquid separation tank is communicated with the bottom of the absorption tower, and the liquid phase of the gas-liquid separation tank is communicated with the upper part of the absorption tower.
Compared with the prior art, the method for desulfurizing and separating the catalytic cracking light product has the beneficial effects that:
the catalytic cracking rich gas and the crude gasoline are firstly subjected to adsorption desulfurization and then are subjected to absorption stabilization, so that the loss of the gasoline yield caused by the traditional method can be reduced to the maximum extent. In the adsorption desulfurization reactor, hydrogen in the rich gas is used as reaction hydrogen to participate in the reaction, so that the hydrogen consumption is saved. The sulfur content of the desulfurized dry gas, liquefied gas and stable gasoline obtained by adsorbing and desulfurizing the rich gas and the crude gasoline and passing through a fractionation-absorption-stabilization system can reach below 10ppm, even below 1 ppm. The rich gas and the crude gasoline are subjected to adsorption desulfurization, so that the loss of low-carbon olefins in the rich gas is less. The method for desulfurizing and separating the catalytic cracking light product saves devices such as dry gas, liquefied gas desulfurization and the like required by the traditional refinery, and does not have the problems of waste liquid, waste residue and the like possibly generated by the traditional desulfurization method.
Drawings
FIG. 1 is a schematic flow diagram of an adsorption desulfurization unit.
FIG. 2 is a schematic flow diagram of an absorption stabilization unit.
Wherein:
2-a first desulfurization reactor, 6-a second desulfurization reactor, 9-an adsorbent receiver, 11-a lock hopper,
14-regenerator feed tank, 17-sorbent regenerator, 20-sorbent receiver, 23-sorbent reducer, 1, 3, 4, 5, 7, 8, 10, 12, 13, 15, 16, 18, 19, 21, 22-lines;
24-absorption tower, 25-desorption tower, 26-reabsorption tower, 27-stabilization tower, 28-gas-liquid separation tank and 29, 30, 31, 32, 33, 34, 35 and 36-pipelines.
Detailed Description
The following detailed description of the embodiments of the invention:
the invention provides a method for desulfurizing and separating catalytic cracking light products, which is characterized in that crude gasoline and a hydrogen donor from a fractionating tower of a catalytic cracking unit are introduced into the bottom of a first desulfurization reactor, contact with a desulfurization adsorbent for desulfurization and flow upwards; the desulfurization adsorbent carrying partial sulfur obtained by gas-solid separation at the top of the reactor enters a second desulfurization reactor; introducing rich gas and hydrogen donor from the catalytic cracking fractionating tower into the bottom of the second desulfurization reactor, contacting with a desulfurization adsorbent for desulfurization, and returning reaction oil gas separated from the desulfurization adsorbent after reaction to the first desulfurization reactor;
reaction oil gas obtained by gas-solid separation of the first desulfurization reactor is separated into desulfurized rich gas and crude gasoline, the desulfurized rich gas enters the absorption tower from the bottom and is absorbed by contacting with the desulfurized crude gasoline introduced from the top of the absorption tower, material flow at the top of the absorption tower enters the reabsorption tower from the bottom and is absorbed by countercurrent contact with light diesel oil from the catalytic cracking fractionating tower, desulfurized dry gas is obtained at the top of the reabsorption tower, and the light diesel oil obtained at the bottom of the reabsorption tower returns to the catalytic cracking fractionating tower; and (3) conveying the tower bottom product of the absorption tower to a stabilizing tower after passing through a desorption tower, fractionating in the stabilizing tower to obtain desulfurized liquefied gas and stabilized gasoline, and returning the tower top gas of the desorption tower to the absorption tower.
Specifically, after the mixture of the crude gasoline and the hydrogen donor from the fractionating tower of the catalytic cracking unit is preheated to a required temperature, the mixture enters the first desulfurization reactor from the bottom of the reactor, flows from bottom to top, and contacts with the desulfurization adsorbent in the first desulfurization reactor for desulfurization. The reaction mixture at the top of the first desulfurization reactor is subjected to gas-solid separation, the desulfurization adsorbent carrying partial sulfur enters the second desulfurization reactor, and is contacted with rich gas and/or a mixture of hydrogen donor which enters from the bottom of the reactor and is preheated to a required temperature to perform desulfurization reaction, the desulfurized rich gas returns to the upper part of the first desulfurization reactor from the second desulfurization reactor, the to-be-generated adsorbent after the reaction of the second desulfurization reactor is separated from the reaction oil gas, the high-pressure hydrogen atmosphere is replaced by low-pressure oxygen atmosphere through a locking hopper, and then the to-be-generated adsorbent enters an adsorbent regenerator to be contacted with the oxygen-containing gas to perform coke burning regeneration, and the regenerated desulfurization adsorbent is reduced and then returns to the bottom of the first desulfurization reactor to be recycled.
The reaction oil gas obtained by separating the top of the first desulfurization reactor enters a gas-liquid separation tank, and is condensed, cooled and separated to obtain desulfurized rich gas and crude gasoline, the desulfurized rich gas is introduced into an absorption tower from the bottom and is in countercurrent contact with the crude gasoline and/or part of stable gasoline entering the absorption tower from the top, a gas product at the top of the absorption tower enters a reabsorption tower to be absorbed and separated with light diesel oil from a catalytic cracking fractionating tower, desulfurized dry gas is obtained at the top of the reabsorption tower, the light diesel oil is obtained at the bottom of the reabsorption tower, and the light diesel oil is returned to the fractionating tower of the catalytic cracking device. The bottom product of the absorption tower passes through a desorption tower and then is sent to a stabilization tower, the product is fractionated in the stabilization tower to obtain desulfurized liquefied gas and desulfurized stable gasoline, and the top gas of the desorption tower and the desulfurized rich gas are mixed and then enter the absorption tower.
In the method provided by the invention, rich gas and crude gasoline are obtained by oil-gas separation at the top of a fractionating tower of a catalytic cracking unit, and the sulfur content is 30 to 50000 micrograms/g, preferably more than 50 micrograms/g. The rich gas may contain nitrogen, carbon dioxide, hydrogen sulfide, and other components.
Heating the crude gasoline obtained from the catalytic cracking fractionating tower to 100-500 ℃. The heated crude gasoline is used as a raw material of a first desulfurization reactor, the crude gasoline, preferably a mixture of the crude gasoline and a hydrogen donor is conveyed into the first desulfurization reactor from the bottom, and the mixture of the crude gasoline and the hydrogen donor is uniformly distributed in the reactor through a feeding distribution disc and is in good contact with a desulfurization adsorbent in the reactor.
The hydrogen donor is selected from one or a mixture of more than two of hydrogen, hydrogen-containing gas and hydrogen donor. The hydrogen gas is hydrogen gas with various purities, the hydrogen-containing gas is preferably one or a mixture of two or more of dry gas produced by the method, catalytic cracking (FCC) dry gas, coking dry gas and thermal cracking dry gas, the hydrogen volume content is preferably more than 30%, and the hydrogen donor is one or a mixture of more than one selected from tetrahydronaphthalene, decahydronaphthalene and indane.
The desulfurization sorbent is transferred from the bottom to the first desulfurization reactor. The first desulfurization reactor is a fluidized bed reactor, preferably a dense-phase bed reactor.
Under the hydrogen condition, the weight hourly space velocity of the oil gas raw material is 0.1 to 100 h at the temperature of 200 to 550 ℃, preferably 300 to 500 ℃, the absolute pressure of 0.5 to 5MPa, preferably 1.0 to 3.5 MPa -1 Preferably 1 to 10 hours -1 Under the reaction condition that the molar ratio of hydrogen to oil is 0.01-1000, preferably 0.05-500, the sulfur-containing crude gasoline is contacted with a desulfurization adsorbent to carry out adsorption desulfurization reaction.
In the first desulfurization reactor, after the desulfurization adsorbent is separated from the reaction hydrocarbon oil, the sulfur-loaded spent adsorbent is transferred to a second desulfurization regenerator.
Heating the rich gas and/or the hydrogen donor to 100-500 ℃.
The sulfur content of the rich gas is above 30 micrograms/gram, preferably above 50 micrograms/gram.
Conveying the heated mixture of the rich gas and/or the hydrogen donor into a second reactor from the bottom of the second fluidized bed reactor, wherein the weight hourly space velocity of the oil gas raw material is 1 to 100 h at the temperature of 300 to 550, preferably 350 to 500 ℃, the absolute pressure of 0.5 to 5MPa, preferably 1.0 to 3.5 MPa and the weight hourly space velocity of the oil gas raw material -1 Preferably 2 to 20 hours -1 And (3) under the reaction condition that the molar ratio of hydrogen to oil is 0.01-500, preferably 0.05-300, enabling the sulfur-containing rich gas to be in contact with a part of sulfur-loaded adsorbent coming from the first reactor to carry out adsorption desulfurization reaction.
The mixture of the rich gas and/or the hydrogen donor is uniformly distributed in the second desulfurization reactor through the feeding distribution plate and is in good contact with the desulfurization adsorbent in the second desulfurization reactor.
After the sulfur-loaded desulfurization adsorbent in the second desulfurization reactor is separated from the reaction oil gas, the hydrocarbon adsorbed by the adsorbent to be generated is removed by steam stripping, and then the adsorbent to be generated is lifted and conveyed to an adsorbent regenerator. Under the reaction conditions that the regeneration temperature is 300-800 ℃, preferably 350-600 ℃, and the regeneration pressure is 0.1-3.0 MPa, preferably 0.1-1.0 MPa, the regeneration gas is contacted with the regeneration gas input from the lower end of the regenerator to realize regeneration. The regeneration gas comprises oxygen, which may be air or a mixture of air or oxygen and an inert gas, such as nitrogen.
The regenerated desulfurizing adsorbent drawn from the regenerator is stripped to remove its adsorbed impurities (such as adsorbed oxygen), and then lifted and conveyed to the adsorbent reducer.
The regenerated desulfurization adsorbent conveyed to the adsorbent reducer is contacted with a reducing gas, and the reduction is carried out under the reducing conditions that the reducing temperature is 250 to 550 ℃, preferably 300 to 450 ℃, and the reducing pressure is 0.2 to 5.0 MPa, preferably 0.5 to 3.5 MPa, wherein the reducing gas is hydrogen or a gas rich in hydrogen.
The reduced desulfurization adsorbent is conveyed into the first desulfurization reactor from the bottom for recycling, so that continuous cycle of adsorption desulfurization reaction, adsorbent regeneration, adsorbent reduction and adsorption desulfurization reaction is realized.
And (3) the hydrocarbon oil product after reaction in the first desulfurization reactor is subjected to heat exchange and then sent to a gas-liquid separation tank to obtain desulfurized rich gas and crude gasoline.
The operating pressure of the gas-liquid separation tank is 0.2-4.0 MPa, preferably 0.5-3.0 MPa, and the operating temperature is 20-300 ℃, preferably 50-200 ℃.
And the desulfurized rich gas and the crude gasoline and/or part of the stable gasoline are respectively sent to an absorption tower after heat exchange to obtain the desulfurized rich gas with the components of more than 2 and the desulfurized crude gasoline with the components of 2 and below.
The operating pressure of the absorption tower is 0.2 to 3.0MPa, preferably 0.5 to 1.6MPa, and the operating temperature is 20 to 100 ℃, preferably 30 to 70 ℃.
The stable gasoline is preferably desulfurized stable gasoline produced by the device.
And (3) sending the desulfurized rich gas with the components above C2 reduced into a reabsorber to contact with diesel oil fraction from a catalytic cracking fractionating tower to obtain a desulfurized dry gas product with the components above C2 further reduced. The diesel fraction absorbing the components above C2 is returned to the fractionating tower of the catalytic cracking unit.
The operating pressure of the reabsorption tower is 0.1 to 3.0MPa, preferably 0.5 to 2.5MPa, and the operating temperature is 20 to 100 ℃, preferably 30 to 70 ℃.
The diesel oil fraction from the catalytic cracking fractionating tower is preferably light diesel oil.
And (3) sending the desulfurized crude gasoline with the reduced components of C2 and below to a desorption tower to obtain the desulfurized crude gasoline with the further reduced components of C2 and below, and returning the gas product at the top of the desorption tower and the desulfurized rich gas to the absorption tower after mixing.
The operating pressure of the desorption tower is 0.1 to 3.0MPa, preferably 0.5 to 2.5MPa, and the operating temperature is 20 to 250 ℃, preferably 50 to 200 ℃.
And sending the desulfurized crude gasoline with the further reduced components of C2 and the following components to a stabilizer to obtain desulfurized liquefied gas and catalytic cracking stable gasoline products.
The operating pressure of the stabilizing tower is 0.1 to 3.0MPa, preferably 0.5 to 2.5MPa, and the operating temperature is 20 to 250 ℃, preferably 50 to 200 ℃.
The desulfurization adsorbent comprises one or a mixture of more than two of various supported metal oxide adsorbents, supported metal oxides loaded with metal promoters and various sulfur conversion agents and sulfur adsorbents. Preferably, the desulfurization adsorbent comprises an adsorbent carrier and a metal component loaded on the adsorbent carrier, wherein the content of the desulfurization adsorbent carrier is 70-95 wt% and the content of the metal component is 5-30 wt% based on the total weight of the desulfurization adsorbent. Preferably, the adsorbent carrier is a mixture of zinc oxide, silica and/or alumina, and the metal component is one or more selected from cobalt, nickel, copper, iron, manganese, molybdenum, tungsten, silver, tin and vanadium. The desulfurization adsorbent is preferably microspherical in shape for facilitating fluidization, and the average particle size of the desulfurization adsorbent is 20 to 200 μm, preferably 40 to 100 μm.
The invention provides a catalytic cracking light product separation and desulfurization device, which comprises an adsorption desulfurization unit and an absorption stabilization unit which are sequentially communicated; the adsorption desulfurization unit comprises a first desulfurization reactor, a second desulfurization reactor, a reactor receiver, a lock hopper, a regenerator feeding tank, an adsorbent regenerator and a regenerator receiver which are sequentially communicated, wherein the regenerator receiver is sequentially communicated with the lock hopper and the adsorbent reducer, and the adsorption reducer is communicated with the bottom of the first desulfurization reactor; the absorption stabilizing unit consists of an absorption tower, a desorption tower, a reabsorption tower and a stabilizing tower which are sequentially communicated; the top of the first desulfurization reactor is provided with a settling separation section, the bottom of the settling separation section is communicated with the lower part of the second desulfurization reactor, and the top of the second desulfurization reactor is communicated with the settling separation section; the outlet at the top of the first desulfurization reactor is communicated with the gas-liquid separation tank, the gas outlet of the gas-liquid separation tank is communicated with the bottom of the absorption tower, and the liquid phase of the gas-liquid separation tank is communicated with the upper part of the absorption tower.
The method provided by the present invention is further described below with reference to the accompanying drawings, but the present invention is not limited thereby.
FIG. 1 is a schematic flow diagram of an adsorptive desulfurization unit. As shown in fig. 1, the adsorption desulfurization unit includes a first desulfurization reactor 2, a second desulfurization reactor 6, a reactor receiver 9, a lock hopper 11 for isolating the reaction-regeneration system, a regenerator feed tank 14, an adsorbent regenerator 17 and a regenerator receiver 20, which are connected in sequence, wherein the regenerator receiver 20 is connected to an adsorbent reducer 23 through the lock hopper 11, and the adsorbent reducer 23 is connected to the bottom of the first desulfurization reactor 2 to provide a desulfurization adsorbent to the first desulfurization reactor 2.
The preheated catalytic cracking fractionating tower crude gasoline and hydrogen enter from the bottom of the first desulfurization reactor 2 through a pipeline 1, contact with a desulfurization adsorbent in the first desulfurization reactor 2 to carry out desulfurization reaction, and the adsorbent loaded with partial sulfur moves upwards along with reaction materials. The reacted reaction oil gas and the adsorbent enter a settling separation section at the top of the first desulfurization reactor 2 for oil agent separation, and the mixture of the desulfurized rich gas, the crude gasoline and the hydrogen is sent to a subsequent product separation and stabilization system through a pipeline 3 for treatment. The desulfurization adsorbent carrying partial sulfur is transferred from the first desulfurization reactor to the bottom of a second desulfurization reactor 6 through a pipeline 4, a mixture of rich gas and hydrogen from a catalytic cracking fractionating tower is introduced into the second desulfurization reactor 9 from the bottom of the second desulfurization reactor to be contacted with the desulfurization adsorbent for adsorption desulfurization reaction, the reaction mixture is subjected to gas-solid separation in a settling zone at the upper part of the second desulfurization reactor, the separated sulfur-carrying adsorbent is conveyed to a reactor receiver 9 through a transfer agent transverse pipe 8 at the upper part of the second desulfurization reactor, is subjected to steam stripping in the reactor receiver 9 and then conveyed to a locking hopper 11 through a pipeline 10, is converted into low-pressure inactive atmosphere from a high-pressure hydrogen environment after nitrogen displacement, and replacement gas is conveyed to a combustion furnace through a pipeline 12 to be burnt. The sulfur-laden sorbent is transported via line 13 to a regenerator feed tank 14, lifted by a lift gas, and passed via line 15 to a sorbent regenerator 17. The method comprises the steps that oxygen-containing gas enters an adsorbent regenerator from the bottom through a pipeline 16, an adsorbent to be regenerated is contacted with the oxygen-containing gas in an adsorbent regenerator 17 to be subjected to sulfur burning and carbon burning to obtain a regenerated adsorbent, sulfur-containing flue gas is separated from the regenerated adsorbent at the top of the adsorbent regenerator and then is conveyed to a sulfur production system or is subjected to alkali washing to remove SOx through a pipeline 18, the regenerated adsorbent is conveyed from the adsorbent regenerator to a regenerator receiver 20 through a pipeline 19, is lifted by nitrogen and conveyed to a lock hopper 11 through a pipeline 21, is subjected to stripping replacement by hydrogen in the lock hopper 11, is boosted and then converted into a high-pressure hydrogen environment, is conveyed to an adsorbent reducer 23 through a pipeline 22 to be reduced, and the reduced regenerated adsorbent is conveyed to a first desulfurization reactor 2 through a pipeline 24 to realize continuous adsorption desulfurization reaction.
FIG. 2 is a schematic flow diagram of an absorption stabilization unit. As shown in fig. 2, the desulfurized reaction oil gas is sent to a gas-liquid separation tank 28, and is subjected to gas-liquid separation by condensation to obtain desulfurized rich gas and crude gasoline, the desulfurized rich gas passes through a pipeline 22, the crude gasoline and/or a part of the stabilized gasoline enters an absorption tower 24 through a pipeline 23, the desulfurized rich gas with the components of more than C2 reduced and the desulfurized crude gasoline with the components of more than C2 increased are obtained, the desulfurized rich gas with the components of more than C2 reduced enters a reabsorber 26 through a pipeline 35, and is contacted with light diesel oil produced by a catalytic device introduced through a pipeline 38, the desulfurized dry gas components with the components of more than C2 reduced are obtained and are discharged from the reabsorber through a pipeline 31, and the light diesel oil with the components of more than C2 absorbed is returned to a fractionating tower of the catalytic device through a pipeline 39 from the bottom of the reabsorber. The desulfurized raw gasoline containing the components of C2 and above is fed into the desorption tower 25 through the pipeline 36 to remove the redundant components (containing C2) below C2, and then fed into the stabilization tower 27 through the pipeline 37, and is fractionated in the stabilization tower 27 to obtain the desulfurized liquefied gas 32 and the desulfurized catalytic cracking stabilized gasoline 34. The gas at the top of the desorption tower is led out through a pipeline 30 and enters the absorption tower together with the desulfurized rich gas.
The following examples further illustrate the invention but are not intended to limit it accordingly. The rich gas and naphtha feedstock used in the examples was obtained from a catalytic cracking unit of Yanshan division, a petrochemical Co., ltd, china, under the trade designation FCAS, and was produced by Nanjing catalyst division, a petrochemical Co., ltd, china, using zinc oxide, silica and alumina as carriers, and Ni as a promoter, and the properties of the catalyst are shown in Table 1.
In the examples and comparative examples: the sulfur content in dry gas and liquefied gas is analyzed by a GC-SCD method on an Agilent GC-7890A gas chromatography, and the sulfur content in gasoline is analyzed by a ZSX 100X-ray fluorescence spectrometer produced by Japan pharmacology. The hydrocarbon composition of the dry gas, the liquefied gas and the gasoline is analyzed and determined by adopting a gas chromatography.
The calculation method of the ethylene saturation rate, the propylene saturation rate and the olefin saturation rate in the gasoline comprises the following steps: the mass fractions of the ethylene, the propylene in the liquefied gas and the olefin in the gasoline in the dry gas which is not subjected to desulfurization treatment in the comparative example 2 and is subjected to adsorption desulfurization and absorption stabilization separation in the corresponding examples are measured by taking the mass contents of the ethylene, the propylene in the liquefied gas and the olefin in the gasoline in the dry gas which is not subjected to desulfurization treatment in the comparative example 1 as references, and the mass percentage of the difference value between the reference value and the value after desulfurization in the reference value is taken as the olefin saturation ratio of each.
Ethylene saturation = ((mass fraction of ethylene in comparative example-mass fraction of ethylene after desulfurization)/mass fraction of ethylene in comparative example) × 100%;
propylene saturation = ((mass fraction of propylene in comparative example-mass fraction of propylene after desulfurization)/mass fraction of propylene in comparative example) × 100%;
gasoline olefin saturation = (mass fraction of gasoline olefins-mass fraction of gasoline olefins after desulfurization in comparative example)/mass fraction of gasoline olefins in comparative example) × 100%.
Comparative example 1
Taking a catalytic cracking device of Yanshan division as an example, rich gas and crude gasoline produced by a catalytic cracking fractionating tower respectively enter an absorption stabilizing unit of the catalytic cracking device, the rich gas enters an absorption tower from the bottom and is absorbed by contacting with the crude gasoline introduced from the top of the absorption tower, material flow at the top of the absorption tower enters a reabsorber from the bottom and is absorbed by countercurrent contacting with light diesel oil from the catalytic cracking fractionating tower, dry gas is obtained at the top of the reabsorber, and the rich light diesel oil obtained at the bottom of the reabsorber returns to the catalytic cracking fractionating tower; and (3) conveying the tower bottom product of the absorption tower to a stabilizing tower after passing through a desorption tower, fractionating in the stabilizing tower to obtain liquefied gas and stable gasoline, and returning the tower top gas of the desorption tower to the absorption tower. The properties of the non-desulfurized dry gas, liquefied gas and stabilized gasoline obtained are shown in Table 2.
Comparative example 2
And (2) taking the stable gasoline obtained in the comparative example 1 as a raw material, feeding the stable gasoline into a gasoline adsorption desulfurization reactor to contact with a desulfurization adsorbent to perform adsorption desulfurization reaction, performing gas-solid separation on reaction oil gas and the sulfur-carrying adsorbent at the top of the adsorption desulfurization reactor, and cooling the separated reaction oil gas to obtain the desulfurized stable gasoline. The sulfur-carrying adsorbent obtained by separation enters an adsorbent regenerator, reacts with oxygen-containing gas under the regeneration condition to be burnt and regenerated, and the regenerated desulfurization adsorbent enters an adsorbent reducer to react with reducing gas under the reduction reaction condition to obtain a reduced desulfurization adsorbent which is returned to the adsorption desulfurization reactor for recycling. The adopted adsorbent is FCAS, the properties are shown in table 1, the reaction temperature is 400 ℃, the reaction pressure is 2.0MPa, and the weight hourly space velocity is 5 h -1 The reaction was carried out under the reaction conditions of a hydrogen-oil volume ratio of 45, and the reaction results are shown in Table 2.
Examples 1 and 2 illustrate the effectiveness of the catalytic cracking light product separation and desulfurization process provided by the present invention.
Example 1
The sulfur-containing rich gas and the crude gasoline are treated by adopting the flow of an adsorption desulfurization unit shown in the attached figure 1, a desulfurization adsorbent from an adsorbent reducer enters a first desulfurization reactor from the bottom, and the crude gasoline is taken as a raw material and is introduced into a first desulfurization reactor from the bottomIn a desulfurization reactor, the reaction temperature is 380 ℃, the reaction pressure is 2.0MPa, and the weight hourly space velocity is 5 h -1 And the volume ratio of hydrogen to oil is 60. Rich gas enters a second desulfurization reactor from the bottom, contacts with a desulfurization adsorbent which is conveyed from a first desulfurization reactor and reacts with the crude gasoline to carry out desulfurization reaction, the reaction temperature is 420 ℃, the reaction pressure is 2.0MPa, and the weight hourly space velocity is 5 h -1 And the desulfurized rich gas obtained by separation from the desulfurization adsorbent is returned to the first desulfurization reactor, and the mixed crude gasoline and the rich gas desulfurization product are further separated from the adsorbent in the first desulfurization reactor and then sent to an absorption stabilizing unit. The flow of the absorption stabilization unit is shown in figure 2, the desulfurized rich gas enters an absorption tower from the bottom, the pressure of the top of the absorption tower is 1.447MPa, the temperature of the top of the absorption tower is 38.5 ℃, and the temperature of the bottom of the absorption tower is 44.6 ℃; the desulfurized crude gasoline enters an absorption tower from the upper part and is in countercurrent contact absorption with rich gas, the material flow on the top of the absorption tower enters a reabsorber from the bottom and is in countercurrent contact absorption with light diesel oil from a catalytic cracking fractionating tower, the pressure on the top of the reabsorber is 1.394MPa, the temperature on the top of the tower is 36.8 ℃, the temperature on the bottom of the tower is 45.4 ℃, desulfurized dry gas is obtained on the top of the reabsorber, and the rich light diesel oil obtained on the bottom of the reabsorber returns to the catalytic cracking fractionating tower; and (3) subjecting the bottom product of the absorption tower to desorption treatment by a desorption tower, wherein the top pressure of the desorption tower is 1.536MPa, the temperature of the top of the tower is 78.9 ℃, the temperature of the bottom of the tower is 137.5 ℃, the bottom product of the tower is sent to a stabilization tower, the top pressure of the stabilization tower is 0.872MPa, the temperature of the top of the tower is 55.3 ℃, the temperature of the bottom of the tower is 160.7 ℃, fractionating in the stabilization tower to obtain desulfurized liquefied gas and stabilized gasoline, and returning the top gas of the desorption tower to the absorption tower. The properties of the resulting desulfurized dry gas, liquefied gas and stabilized gasoline are shown in Table 2.
Example 2
Adopting the desulfurization and separation method flow shown in the adsorption desulfurization unit and the absorption stabilization unit shown in the attached figures 1 and 2, the desulfurization adsorbent from the adsorbent reducer enters a first desulfurization reactor from the bottom, the raw gasoline raw material is introduced into the first desulfurization reactor from the bottom, and the reaction temperature is 430 ℃, the reaction pressure is 1.4MPa, and the weight hourly space velocity is 8 h -1 Hydrogen to oil volume ratio of 100Reacting under the reaction condition, allowing rich gas to enter a second desulfurization reactor from the bottom, contacting with a desulfurization adsorbent conveyed from a first desulfurization reactor and reacted with crude gasoline to perform desulfurization reaction, wherein the reaction temperature is 445 ℃, the reaction pressure is 1.4MPa, and the weight hourly space velocity is 12 h -1 And returning the desulfurized rich gas separated from the desulfurization adsorbent to the first desulfurization reactor, and further separating the mixed naphtha and the rich gas desulfurization product from the adsorbent in the first desulfurization reactor and then sending the mixture to an absorption stabilizing unit. The flow of the absorption stabilization unit is shown in figure 2, the desulfurized rich gas enters an absorption tower from the bottom, the pressure at the top of the absorption tower is 1.658MPa, the temperature at the top of the absorption tower is 45.1 ℃, and the temperature at the bottom of the absorption tower is 52.6 ℃; the crude gasoline separated by the gas-liquid separation tank 28 is led out by a pipeline 23, enters an absorption tower from the upper part, is in countercurrent contact with rich gas for absorption, the material flow at the top of the absorption tower enters a reabsorber from the bottom and is in countercurrent contact with light diesel oil from a catalytic cracking fractionating tower for absorption, the pressure at the top of the reabsorber is 1.556MPa, the temperature at the top of the tower is 38.9 ℃, the temperature at the bottom of the tower is 45.7 ℃, desulfurized dry gas is obtained at the top of the reabsorber, and the rich light diesel oil obtained at the bottom of the reabsorber returns to the catalytic cracking fractionating tower; and (3) subjecting the bottom product of the absorption tower to desorption treatment by a desorption tower, wherein the top pressure of the desorption tower is 1.728MPa, the temperature of the top of the tower is 80.9 ℃, the temperature of the bottom of the tower is 142.5 ℃, the bottom product of the tower is sent to a stabilization tower, the top pressure of the stabilization tower is 0.806MPa, the temperature of the top of the tower is 55.4 ℃, the temperature of the bottom of the tower is 159.7 ℃, fractionating in the stabilization tower to obtain desulfurized liquefied gas and stabilized gasoline, and returning the top gas of the desorption tower to the absorption tower. The properties of the resulting desulfurized dry gas, liquefied gas and stabilized gasoline are shown in Table 2.
The results in table 2 show that the method for desulfurizing and separating the catalytic cracking light product can realize the desulfurization of dry gas and liquefied gas simultaneously, the yield of the liquefied gas is respectively increased by 0.1 percent, the yield of the stable gasoline is increased by 0.4 to 0.6 percent, the sulfur content of the stable gasoline is reduced, the olefin saturation rate in the gasoline is reduced, and the octane number loss is reduced.
TABLE 1 Properties of the desulfurization sorbent
TABLE 2
Claims (10)
1. A method for desulfurizing and separating light products of catalytic cracking is characterized in that crude gasoline and hydrogen donor from a fractionating tower of a catalytic cracking unit are introduced into the bottom of a first desulfurization reactor, contact with a desulfurization adsorbent for desulfurization, and flow upwards; the desulfurization adsorbent carrying partial sulfur obtained by gas-solid separation at the top of the reactor enters a second desulfurization reactor; introducing rich gas and hydrogen donor from the catalytic cracking fractionating tower into the bottom of the second desulfurization reactor, contacting with a desulfurization adsorbent for desulfurization, and returning reaction oil gas separated from the desulfurization adsorbent after reaction to the first desulfurization reactor;
reaction oil gas obtained by gas-solid separation of the first desulfurization reactor is separated into desulfurized rich gas and crude gasoline, the desulfurized rich gas enters the absorption tower from the bottom and is absorbed by contacting with the desulfurized crude gasoline introduced from the top of the absorption tower, material flow at the top of the absorption tower enters the reabsorption tower from the bottom and is absorbed by countercurrent contact with light diesel oil from the catalytic cracking fractionating tower, desulfurized dry gas is obtained at the top of the reabsorption tower, and the light diesel oil obtained at the bottom of the reabsorption tower returns to the catalytic cracking fractionating tower; the bottom product of the absorption tower passes through a desorption tower and is sent to a stabilization tower, the product is fractionated in the stabilization tower to obtain desulfurized liquefied gas and stabilized gasoline, and the gas at the top of the desorption tower returns to the absorption tower;
the operating temperature of the first desulfurization reactor is 200-550 ℃, the absolute pressure is 0.5-5 MPa, and the weight hourly space velocity of the oil gas raw material is 0.1-100 h -1 The molar ratio of hydrogen to oil is 0.01 to 1000;
the operating temperature of the second desulfurization reactor is 300-550 ℃, the absolute pressure is 0.5-5 MPa, and the weight hourly space velocity of the oil gas raw material is 1-100 h -1 The molar ratio of hydrogen to oil is 0.01 to 500;
the hydrogen donor is selected from one or a mixture of more than two of hydrogen, hydrogen-containing gas and hydrogen donor;
the desulfurization adsorbent comprises an adsorbent carrier and a metal component loaded on the adsorbent carrier, wherein the content of the desulfurization adsorbent carrier is 70-95 wt%, the content of the metal component is 5-30 wt%, the adsorbent carrier is a mixture of zinc oxide, silica and/or alumina, and the metal component is one or more selected from cobalt, nickel, copper, iron, manganese, molybdenum, tungsten, silver, tin and vanadium.
2. The method for desulfurizing and separating a catalytically cracked light product according to claim 1, wherein the mixture of the reaction oil gas and the desulfurizing adsorbent is subjected to gas-solid separation at the top of the second desulfurizing reactor, the separated desulfurizing adsorbent carrying sulfur is subjected to calcination regeneration with an oxygen-containing gas in an adsorbent regenerator, and the regenerated desulfurizing adsorbent is reduced and returned to the first desulfurizing reactor.
3. The method for desulfurizing and separating a catalytic cracking light product according to claim 1, wherein the operating temperature of the first desulfurization reactor is 300 to 500 ℃, the absolute pressure is 1.0 to 3.5 MPa, and the weight hourly space velocity of the oil and gas raw material is 1 to 10 h -1 The molar ratio of hydrogen to oil is 0.05 to 500.
4. The method for desulfurizing and separating a catalytic cracking light product according to claim 1, wherein the operating temperature of the second desulfurization reactor is 350 to 500 ℃, the absolute pressure is 1.0 to 3.5 MPa, and the weight hourly space velocity of the oil and gas raw material is 2 to 20 h -1 The molar ratio of hydrogen to oil is 0.05 to 300.
5. The process for desulfurization and separation of catalytically cracked light products as set forth in claim 2, wherein said adsorbent regenerator is operated under the following conditions: the regeneration temperature is 300-800 ℃, and the regeneration pressure is 0.1-3.0 MPa.
6. The process for desulfurization and separation of catalytically cracked light products of claim 5, wherein the adsorbent regenerator is operated under the following conditions: the regeneration temperature is 350-600 ℃, and the regeneration pressure is 0.1-1.0 MPa.
7. The process for desulfurization and separation of a catalytically cracked light product according to claim 1 or 2, wherein the absorber is operated under the following conditions: the pressure is 0.2 to 3.0MPa, and the temperature is 20 to 100 ℃; the operating conditions of the desorption tower are as follows: the pressure is 0.1 to 3.0MPa, and the temperature is 20 to 250 ℃; the operating conditions of the reabsorption tower are as follows: the pressure is 0.1 to 3.0MPa, and the temperature is 20 to 100 ℃; the operation conditions of the stabilizing tower are as follows: the pressure is 0.1 to 3.0MPa, and the temperature is 20 to 250 ℃.
8. The process for desulfurizing and separating a catalytically cracked light product according to claim 7, wherein said absorber is operated under the following conditions: the pressure is 0.5 to 1.6MPa, and the temperature is 30 to 70 ℃; the operating conditions of the desorption tower are as follows: the pressure is 0.5 to 2.5MPa, and the temperature is 50 to 200 ℃; the operating conditions of the reabsorption tower are as follows: the pressure is 0.5 to 2.5MPa, and the temperature is 30 to 70 ℃; the operation conditions of the stabilizing tower are as follows: the pressure is 0.5 to 2.5MPa, and the temperature is 50 to 200 ℃.
9. A method for producing low-sulfur light oil products by catalytic cracking is characterized in that catalytic cracking raw materials are introduced into a riser reactor, contacted with a catalytic cracking catalyst, reacted under the catalytic cracking reaction condition, gas-solid separation is carried out on the top of the riser reactor, obtained reaction oil gas enters a catalytic cracking fractionating tower, and rich gas, crude gasoline, light diesel oil, diesel oil and oil slurry are obtained by fractionation; the separated catalytic cracking catalyst is regenerated and then returned to the riser reactor for recycling;
respectively introducing rich gas and crude gasoline from a fractionating tower of a catalytic cracking device into a first desulfurization reactor and a second desulfurization reactor of an adsorption desulfurization reaction unit, carrying out adsorption desulfurization by adopting the catalytic cracking light product desulfurization and separation method of any one of claims 1-8, and carrying out absorption stabilization separation to obtain desulfurized dry gas, desulfurized liquefied gas and stabilized gasoline.
10. A catalytic cracking light product separation and desulfurization device, which is used for the catalytic cracking light product desulfurization and separation method according to any one of claims 1 to 8, and comprises an adsorption desulfurization unit and an absorption stabilization unit which are communicated in sequence; the adsorption desulfurization unit comprises a first desulfurization reactor, a second desulfurization reactor, a reactor receiver, a lock hopper, a regenerator feed tank, an adsorbent regenerator and a regenerator receiver which are sequentially communicated, wherein the regenerator receiver is sequentially communicated with the lock hopper and the adsorbent reducer, and the adsorbent reducer is communicated with the bottom of the first desulfurization reactor; the absorption stabilizing unit consists of an absorption tower, a desorption tower, a reabsorption tower and a stabilizing tower which are sequentially communicated; the system comprises a catalytic cracking fractionating tower, a first desulfurization reactor, a second desulfurization reactor, a settling separation section, a first desulfurization reactor, a second desulfurization reactor and a gas-enriched gas inlet, wherein the crude gasoline inlet from the catalytic cracking fractionating tower is arranged at the bottom of the first desulfurization reactor, the gas-enriched inlet from the catalytic cracking fractionating tower is arranged at the bottom of the second desulfurization reactor, the top of the first desulfurization reactor is provided with the settling separation section, the bottom of the settling separation section is communicated with the lower part of the second desulfurization reactor, and the top of the second desulfurization reactor is communicated with the settling separation section; the outlet at the top of the first desulfurization reactor is communicated with the gas-liquid separation tank, the gas outlet of the gas-liquid separation tank is communicated with the bottom of the absorption tower, and the liquid phase of the gas-liquid separation tank is communicated with the upper part of the absorption tower.
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| CN201911049459.XA CN112745933B (en) | 2019-10-31 | 2019-10-31 | Method and device for separating and desulfurizing catalytic cracking light products |
| EP20882534.9A EP4053250A4 (en) | 2019-10-31 | 2020-10-30 | Method and apparatus for desulfurization and separation of catalytically cracked light product |
| KR1020227018593A KR20220093182A (en) | 2019-10-31 | 2020-10-30 | Method and apparatus for desulfurization and separation of catalytic cracking light products |
| AU2020374918A AU2020374918A1 (en) | 2019-10-31 | 2020-10-30 | Method and apparatus for desulfurization and separation of catalytically cracked light product |
| JP2022525762A JP2023500332A (en) | 2019-10-31 | 2020-10-30 | Method and apparatus for desulphurization and separation of catalytic cracking light products |
| PCT/CN2020/125166 WO2021083314A1 (en) | 2019-10-31 | 2020-10-30 | Method and apparatus for desulfurization and separation of catalytically cracked light product |
| US17/755,541 US20220380689A1 (en) | 2019-10-31 | 2020-10-30 | Method and apparatus for desulfurization and separation of catalytically cracked light product |
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| CN1763156A (en) * | 2004-10-22 | 2006-04-26 | 中国石油化工股份有限公司 | Process for reducing contents of components above C3 in dry gas |
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| CN1763156A (en) * | 2004-10-22 | 2006-04-26 | 中国石油化工股份有限公司 | Process for reducing contents of components above C3 in dry gas |
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