CN102220161B - Separating method of mixture containing gasoline - Google Patents
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- CN102220161B CN102220161B CN201010150739.2A CN201010150739A CN102220161B CN 102220161 B CN102220161 B CN 102220161B CN 201010150739 A CN201010150739 A CN 201010150739A CN 102220161 B CN102220161 B CN 102220161B
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Abstract
The invention provides a separating method of a mixture containing gasoline, which comprises the following steps of: (1) desorbing the mixture containing gasoline after being heated to obtain a liquid heavy component; (2) after heating the liquid heavy component A, mixing with the mixture containing gasoline and carrying out the desorption as the step (1), and separating the balance into a mixture and heavy gasoline, wherein the mixture contains light gasoline and liquefied gas; (3) after heating the mixture containing the light gasoline and the liquefied gas, separating the mixture containing the light gasoline and the liquefied gas into liquefied gas and stable light gasoline; (4) after heating the stable light gasoline A, mixing the stable light gasoline A and the mixture containing the light gasoline and the liquefied gas, and carrying out the operation of the step (3), wherein the heat source of the step (3) comes from the stable light gasoline of the balance, and the heat sources of the step (1) and the step (2) come from the heavy gasoline. According to the method provided by the invention, the energy consumption of the whole process is greatly reduced under the condition that the quality of products is ensured.
Description
Technical field
The present invention relates to a kind of separation method of hydrocarbon mixture, more precisely relate to the separation method containing gasoline mixture.
Background technology
International oil price continues to rise in recent years, and China's Economic development constantly increases the petroleum products demand of high value, and existing market is to the continuous lighting of petroleum products, high quality and the requirement cleaning and the oil supply aggravation of contradictions of heaviness, in poor quality day by day.Therefore, the technology of exploitation heavy oil Efficient Conversion, increase yield of light oil will be the significant development strategy of China's 21 century oil refining industry.At present, oil refining enterprise of China yield of light oil average out to 74%, and Foreign Advanced Lerel is more than 80%, space still improves a lot.
Catalytic cracking technology is that inferior heavy oil is converted into lightweight oil one of the most effective technology.In the exploitation direction of conventional catalytic cracking process and catalyzer, still continuing along increasing heavy oil single-pass conversion ability is development goal.But for processing inferior raw material, only increase heavy oil conversion performance and tend to be accompanied by the obvious increase of dry gas and coke yield by adjusting catalyzer composition and processing parameter, will reduce so undoubtedly the yield of light oil of raw material.
CN1425055A discloses a kind of fluidized catalytic cracking method, and the method comprises: (A) under catalytic cracking condition, FCC charging is contacted in the first catalytic cracking section with catalytic cracking catalyst, generate crackate; (B) separating out at least one cycle oil fraction from crackate, described cycle oil fraction comprises aromatic hydrocarbons; (C) under hydroconversion condition, aromatic fraction described at least one in cycle oil fraction described at least a portion under existing, hydrogenation catalyst is carried out to hydrogen treatment, generate hydrogenation cycles oil; (D) in second fluidized catalytic cracking section, described hydrogenation cycles oil is contacted under catalytic cracking condition with catalytic cracking catalyst, generate the second crackate, described second fluidized catalytic cracking section is separated with described first class catalytic cracking section, and the catalyzer of second fluidized catalytic cracking section comprises that a kind of surface-area is approximately from 5 to 400m
2the amorphous metal oxide catalyst of/g.
CN101531924A discloses a kind of method of producing light-weight fuel oil and propylene from inferior feedstock oil, first and second reaction zone that inferior feedstock oil is entered successively catalytic conversion reactor by the method contacts with catalytic converting catalyst primary first-order equation, secondary reaction occurs respectively, reaction product and reclaimable catalyst after gas solid separation, reclaimable catalyst successively through stripping, burn again after Returning reactor recycle; Reaction product is isolated to propylene, gasoline, heavy oil and other products, wherein said heavy oil and hydrogen, hydrotreating catalyst contact reacts, gained hydrogenation heavy oil is circulated to the first reaction zone of catalytic conversion reactor or/and the further reaction of other catalytic convention design obtains object product propylene and gasoline.In the method, inferior feedstock oil is after relaxing catalyzed conversion, and gained heavy oil character after hydrogenation is obviously improved, thereby lightweight oil obviously increases, and dry gas obviously reduces, and slurry oil productive rate obviously reduces, and has realized petroleum resources and has efficiently utilized.
But mitigation catalytic cracking and conventional catalytic cracking all exist the problem that gasoline products olefin(e) centent is high, the in poor quality day by day of raw material also makes content of sulfur in gasoline higher simultaneously, can not meet the vehicle fuel standard of continuous renewal.Because main ingredient in China's motor spirit is catalytically cracked gasoline, the olefin(e) centent and the sulphur content that therefore reduce catalytically cracked gasoline become key.From a series of reduction olefins in FCC gasoline and the sulphur content technology of exploitation, by catalytic gasoline be divided into gently, heavy petrol, the mixture that contains petroleum naphtha and liquefied gas goes etherificate or removes catalytic cracking unit freshening, heavy petrol goes desulfurization.Heavy petrol after desulfurization is concocted out qualified gasoline products with mixture containing petroleum naphtha and liquefied gas or stop bracket gasoline again becomes a technical scheme of producing clean gasoline of being approved by majority.For this reason, full gasoline cut need to be cut into weight gasoline component be to supply raw materials in follow-up unit to conventional catalytic cracking fractionation absorbing-stabilizing system.
CN1542085A discloses a kind of separation method of catalytically cracked gasoline, the reaction oil gas that wherein catalytic cracking obtains is through main fractionation, absorb, desorption, steady component obtains stable gasoline, in catalytic cracking system device, set up again gasoline separate part, the stable gasoline obtaining is isolated mixture and the heavy petrol product containing petroleum naphtha and liquefied gas through gasoline separate part, wherein reflux as providing thermal source at the bottom of the tower in gasoline separate part in the stage casing of the main fractionation part of catalytic cracking, the absorption portion of catalytic cracking simultaneously adopts the heavy petrol absorption agent as a supplement after stable gasoline fractionation.But there is the higher problem of energy consumption in the method.
Summary of the invention
The object of this invention is to provide a kind of new separation method containing gasoline mixture.
Separation method containing gasoline mixture provided by the invention, the method comprises the following steps:
(1) should, containing carrying out desorb after gasoline mixture heating, contain the light constituent dry gas of gasoline mixture mid-boiling point lower than liquefied gas to isolate this, obtain liquid heavy constituent;
(2) liquid heavy constituent A heating is mixed and carries out the desorb of above-mentioned steps (1) afterwards with containing gasoline mixture, liquid heavy constituent B is separated into mixture and the heavy petrol containing petroleum naphtha and liquefied gas, wherein, the heavy constituent A of described liquid state is a part for the heavy constituent of step (1) gained liquid state, and the heavy constituent B of described liquid state is the remainder of the heavy constituent of step (1) gained liquid state;
(3) gained is separated into liquefied gas and stable petroleum naphtha after the mixture heating containing petroleum naphtha and liquefied gas;
(4) after stablizing petroleum naphtha A heating, mix and carry out the operation of above-mentioned steps (3) with the mixture that contains petroleum naphtha and liquefied gas, described stable petroleum naphtha A is the part that step (3) gained is stablized petroleum naphtha;
Wherein, to the heating of the described mixture containing petroleum naphtha and liquefied gas, by described mixture and stable petroleum naphtha B heat exchange containing petroleum naphtha and liquefied gas realized, described stable petroleum naphtha B is the remainder that step (3) gained is stablized petroleum naphtha; The heating of heavy constituent A to described liquid state and to containing the heating of gasoline mixture by by described heavy petrol successively with the heavy constituent A of described liquid state and describedly realize containing gasoline mixture heat exchange.
Separation method containing gasoline mixture provided by the invention is by making the liquid heavy constituent that desorb obtains first be separated into mixture and the heavy petrol containing petroleum naphtha and liquefied gas, carry out again gasoline stable operation, make only to need the component of mixture to containing petroleum naphtha and liquefied gas to stablize, thereby greatly reduce the load of stabilizer tower.In addition, by rational flow setting, the heating of the described mixture containing petroleum naphtha and liquefied gas is realized by described mixture and described stable petroleum naphtha B heat exchange containing petroleum naphtha and liquefied gas, the heating of heavy constituent A to described liquid state and to containing the heating of gasoline mixture by by described heavy petrol successively with heavy constituent A liquid described in this with describedly realize containing gasoline mixture heat exchange, thereby under the prerequisite that ensures quality product, greatly reduce the energy consumption of whole technique.
Brief description of the drawings
Fig. 1 is the process flow sheet of the separation method containing gasoline mixture of the present invention;
Fig. 2 is the process flow sheet of the existing separation method containing gasoline mixture.
Embodiment
In the present invention, described cut point light, heavy petrol is 60-150 DEG C, is preferably 70-130 DEG C, and the content of corresponding heavy petrol in whole gasoline boiling range is 20-90 % by weight, is preferably 30-80 % by weight.
In the present invention, the object of only describing for convenience, introduce liquid heavy constituent A, liquid heavy constituent B, stablize the concept of petroleum naphtha A and stable petroleum naphtha B, and do not represent between liquid heavy constituent A and liquid heavy constituent B and have any different between stable petroleum naphtha A and stable petroleum naphtha B, more do not represent that the liquid heavy constituent that need in advance step (1) be obtained is separated into liquid heavy constituent A and liquid heavy constituent B or the stable petroleum naphtha that need in advance step (3) be obtained is separated into and stablizes petroleum naphtha A and stable petroleum naphtha B.
According to the separation method containing gasoline mixture of the present invention, as long as the described needs that meet stable operation containing gasoline and the mixture of liquefied gas and the heat exchange of described stable petroleum naphtha B, preferable case, described containing gasoline and the mixture of liquefied gas and the heat exchange of described stable petroleum naphtha B make with described stable petroleum naphtha B heat exchange after the temperature of the described mixture that contains petroleum naphtha and liquefied gas be 60-150 DEG C, more preferably 90-140 DEG C.Under preferable case, can be 0.1-0.9 by the weight ratio of controlling described stable petroleum naphtha B and the described mixture containing petroleum naphtha and liquefied gas: 1, the difference between the temperature of described stable petroleum naphtha B and the temperature of the described mixture containing petroleum naphtha and liquefied gas is 10-100 DEG C of temperature that realizes the described mixture containing petroleum naphtha and liquefied gas after above-mentioned heat exchange.Further, under preferable case, the weight ratio of controlling described stable petroleum naphtha B and the described mixture containing petroleum naphtha and liquefied gas is 0.2-0.8: 1, and the temperature head of described stable petroleum naphtha B and the described mixture containing petroleum naphtha and liquefied gas is 10-80 DEG C.In the present invention, when carrying out containing being separated in gasoline separation tower between the mixture of petroleum naphtha and liquefied gas and heavy petrol in step (2), when step (3) is carried out in stabilizer tower, unless stated otherwise, the column bottom temperature that the temperature head of the temperature of described stable petroleum naphtha B and the described mixture containing petroleum naphtha and liquefied gas is stabilizer tower and the feeding temperature of gasoline separation tower poor.
According to the present invention, the degree of described heavy petrol and the heavy constituent A heat exchange of described liquid state is returned with described and is mixed and carry out separating of step (1) and be as the criterion containing gasoline mixture to meet this liquid heavy constituent A.Under preferable case, with the temperature of the heavy constituent A of the described liquid state after described heavy petrol heat exchange be 30-150 DEG C, more preferably 50-120 DEG C.Further under preferable case, the weight ratio of the heavy constituent A by controlling described heavy petrol and described liquid state is 0.1-1: 1, and the temperature head of the heavy constituent A of described heavy petrol and described liquid state is 20-200 DEG C and realizes above-mentioned heat exchange degree.Further under preferable case, the weight ratio of the heavy constituent A by controlling described heavy petrol and described liquid state is 0.3-0.7: 1, and the temperature head of the heavy constituent A of described heavy petrol and described liquid state is 50-180 DEG C and realizes above-mentioned heat exchange degree.In the present invention, when described desorb in desorption tower, carry out and described step (2) in while carrying out in gasoline separation tower containing being separated between the mixture of petroleum naphtha and liquefied gas and heavy petrol, unless stated otherwise, the column bottom temperature that the temperature head of the heavy constituent A of described heavy petrol and described liquid state is gasoline separation tower and the column bottom temperature of desorption tower poor.
In the present invention, the weight ratio of the heavy constituent A of described liquid state and the heavy constituent B of described liquid state is 0.5-3: 1, and more preferably 0.8-2: 1.
According to the present invention, described heavy petrol and described degree containing gasoline mixture heat exchange describedly can be carried out the described desorb of step (1) containing gasoline mixture and are as the criterion to be met.Under preferable case, with the described temperature containing gasoline mixture after described heavy petrol heat exchange be 30-150 DEG C, more preferably 50-100 DEG C., under preferable case, be further 0.2-0.9 by controlling described heavy petrol with the described weight ratio containing gasoline mixture: 1, described heavy petrol and the described temperature head that contains gasoline mixture are 50-230 DEG C and realize above-mentioned heat exchange degree.Further under preferable case, the weight ratio of the heavy constituent A by controlling described heavy petrol and described liquid state is 0.3-0.8: 1, and the temperature head of the heavy constituent A of described heavy petrol and described liquid state is 80-200 DEG C and realizes above-mentioned heat exchange degree.In the present invention, unless stated otherwise, described heavy petrol and described temperature head containing gasoline mixture are enter temperature that heat exchanger carries out described heavy petrol before heat exchange and the described temperature that contains gasoline mixture poor.
Method provided by the invention is passed through using the heavy petrol from the bottom of gasoline separation tower tower first as desorption tower tower bottom reboiler thermal source, then goes the charging of preheating desorption tower, cools afterwards as being down to 40 DEG C of left and right again.The stabilizer tower tower base stream that separates liquefied gas and petroleum naphtha stablizes first preheating stabilizer tower charging of petroleum naphtha B, cools afterwards as being down to 40 DEG C of left and right again.Thereby under the prerequisite that ensures quality product, greatly reduce the energy consumption of whole technique.
Under normal circumstances, the product that hydrocarbon oil catalytic cracking obtains is admitted in catalytic cracking main fractionating tower, carries out cutting and separating according to boiling point height, obtains rich gas, naphtha fraction, solar oil cut, heavy gas oil cut, recycle stock cut and slurry oil.Wherein, described rich gas refers to the gaseous matter that is gaseous state under normal temperature and pressure, mainly comprises dry gas (H
2, N2, CO, CO
2, H
2s, C1 and C2 hydro carbons etc.), liquefied gas (C3-C4 hydro carbons).Described naphtha fraction refers to that boiling range under normal pressure is the distillate of 25-205 DEG C.Described solar oil cut refers to that boiling range under normal pressure is the distillate of 180-360 DEG C.Described heavy gas oil cut refers to that boiling range under normal pressure is the distillate of 250-420 DEG C.Described recycle stock cut refers to that boiling range under normal pressure is the distillate of 260-500 DEG C.Described slurry oil refers to that boiling range under normal pressure is the distillate of 260-600 DEG C.Described rich gas mainly comprises dry gas, liquefied gas and gasoline component, therefore needs further separation, the liquefied gas that just can obtain conforming to quality requirements, and can also separate being wherein worth higher gasoline component by separating.
In the present invention, described can be the various mixtures that contain gasoline and dry gas and/or liquefied gas containing gasoline mixture, the tower top oil gas that for example can obtain for catalytic cracking is the condensed oil that above-mentioned rich gas compression the laggard row gas-liquid separation of condensation obtain, and can be also the various containing gasoline mixture of other sources.Preferably described is the condensed oil that above-mentioned rich gas compression the laggard row gas-liquid separation of condensation obtain containing gasoline mixture, described in, contain mixture and heavy petrol that gasoline mixture contains liquefied gas, contains petroleum naphtha and liquefied gas, taking the described total amount containing gasoline mixture as benchmark, the content of described liquefied gas is 10-60 % by weight, the content of the described mixture containing petroleum naphtha and liquefied gas is 10-70 % by weight, and the content of described heavy petrol is 20-80 % by weight.
As shown in Figure 1, the overhead oil air pressure that catalytic cracking the is obtained laggard row gas-liquid separation of condensation of contracing, generally obtains water, condensed oil and top gas, and the temperature of described condensation can be 20-50 DEG C.Described top gas is the dry gas in catalytic cracking process.The boiling range of described condensed oil is generally 20-210 DEG C.Owing to still may containing a small amount of component such as liquefied gas or gasoline in above-mentioned top gas, therefore, under normal circumstances, also utilize above-mentioned naphtha fraction to carry out one or many counter current contact as absorption agent and above-mentioned top gas, to absorb liquefied gas and light gasoline fraction wherein.Now, under preferable case, method provided by the invention also comprise by successively with the heavy constituent A of described liquid state and described containing the cooling heavy petrol after gasoline mixture heat exchange and/or at least a portion in cooled stable petroleum naphtha B as a supplement absorption agent and described top gas carry out counter current contact, to absorb the liquefied gas component in top gas.By use heavy petrol as a supplement absorption agent contact with above-mentioned top gas together with naphtha fraction, to absorb the hydrocarbon ils in top gas, the consumption that supplements absorption agent can be greatly reduced, thereby the energy consumption of whole catalytic cracking production separating technology route can be reduced.But with stable petroleum naphtha absorption agent as a supplement, can further reduce the energy consumption of whole catalytic cracking production separating technology route.The cooling heavy petrol of remainder and/or stable petroleum naphtha B send separation system.The temperature of described cooled heavy petrol and stable petroleum naphtha is preferably 20-50 DEG C separately.
Can realize separating of dry gas in catalytically cracked gasoline, water and liquid heavy constituent by above-mentioned compression and condensation.Described compression can be carried out in compressor, and described condensation can be carried out in condenser, and described gas-liquid separation can be carried out in the conventional knockout drum using in this area, and their concrete operations have been technology well-known to those skilled in the art.The water that gas-liquid separation obtains is outer row conventionally.The tower top pressure on described absorption tower can be 1-2MPa, and tower top temperature can be 35-60 DEG C, and column bottom temperature can be 40-70 DEG C.The weight ratio of supplementing absorption agent consumption and absorption agent naphtha fraction is 0.2-1.3.Under preferable case, the tower top pressure on described absorption tower can be 1-2MPa, and tower top temperature can be 35-50 DEG C, and column bottom temperature can be 40-55 DEG C.The stage number on described absorption tower can be 30-50, is preferably 30-40 piece.Described absorption tower can be the conventional various absorption towers that use, this area, for example, can be sieve-tray tower or bubble-plate column and packing tower.In described absorption tower, the weight ratio of the raw gasline that described top gas and catalytic cracking obtain can be 0.01-0.5: 1, and the tower top pressure on described absorption tower can be 1-2MPa, and tower top temperature can be 35-45 DEG C, and column bottom temperature can be 40-55 DEG C.Under preferable case, the weight ratio of the raw gasline that described top gas and catalytic cracking obtain can be 0.02-0.4: 1, and the tower top pressure on described absorption tower can be 1-2MPa, and tower top temperature can be 35-45 DEG C, and column bottom temperature can be 40-55 DEG C.The theoretical plate number on described absorption tower can be 10-30, is preferably 15-28 piece.Described absorption tower can be the conventional various absorption towers that use, this area, for example, can be sieve-tray tower or bubble-plate column.In order as far as possible the gasoline component being mingled with in dry gas to be absorbed cleanly, under preferable case, described absorption can be carried out in the absorption tower of multiple series connection.Also be that described absorption can comprise that one-level absorbs and secondary absorbs even more multistage absorption.After absorbing, obtain dry gas as H
2, N
2, CO, CO
2, H
2s, C1 and C2 hydro carbons etc.The main component of described top gas is dry gas and liquefied gas component.
Tower top oil gas after the first tower base stream obtaining at the bottom of absorption tower and compression merges, and carries out above-mentioned gas-liquid separation after condensation.
Condensed oil separates by separation method of the present invention, obtains liquefied gas, petroleum naphtha and heavy petrol.In this case, method provided by the invention preferably also comprises described top gas and absorption agent counter current contact, to absorb the liquefied gas component in top gas.
Method of the present invention can be used petroleum naphtha absorption agent as a supplement, also can be used as heavy petrol absorption agent as a supplement.A preferred embodiment of the invention, use heavy petrol absorption agent as a supplement, be the described absorption agent of part be successively with the heavy constituent A of described liquid state and described containing the part in the heavy petrol after gasoline mixture heat exchange, and be the 20-90 % by weight of the total consumption of absorption agent as the amount of the heavy petrol of described absorption agent.
According to another embodiment of the invention, use stable petroleum naphtha absorption agent as a supplement, be that the described absorption agent of part is a part of described stable petroleum naphtha B, and be the 10-60 % by weight of the total consumption of absorption agent as the amount of the stable petroleum naphtha B of described absorption agent.
According to the present invention, described desorb is carried out conventionally in desorption tower, the tower top pressure of desorption tower can be 1-2MPa, tower top temperature can be 50-90 DEG C, be preferably 60-85 DEG C, column bottom temperature can be 100-160 DEG C, is preferably 100-155 DEG C, at the bottom of tower, the weight ratio of the inlet amount of load and tower is 0.1-0.99: 1, and stage number can be 30-50 piece.The concrete operations of described desorb have been conventionally known to one of skill in the art.The present inventor finds, by control desorption tower condition as above, and described is that overhead oil air pressure by catalytic cracking is obtained is while contracing the condensed oil that the laggard row gas-liquid separation of condensation obtains containing gasoline mixture, the weight ratio that can realize the heavy constituent A of described heavy petrol and described liquid state is 0.1-1: 1, thus reach object of the present invention.Therefore, in following examples, the weight ratio of the heavy constituent A to described heavy petrol and described liquid state is not measured especially and is illustrated.
In the separation of step (2) preferably, carry out in gasoline separation tower containing separating preferably between the mixture of petroleum naphtha and liquefied gas and heavy petrol, the tower top pressure of described gasoline separation tower can be 1-2MPa, tower top temperature can be 100-150 DEG C, be preferably 100-140 DEG C, column bottom temperature can be 200-265 DEG C, trim the top of column ratio can be 0.2-3: 1, and stage number can be 25-50 piece.
Step (3) is generally carried out in stabilizer tower, the tower top pressure of described stabilizer tower can be 1-2MPa, tower top temperature can be 40-80 DEG C, be preferably 40-60 DEG C, column bottom temperature can be 100-200 DEG C, trim the top of column ratio can be 0.5-3: 1, and stage number or theoretical pedal number can be 30-50 piece.
Below in conjunction with accompanying drawing, the present invention is described in detail.
A preferred embodiment of the invention, as shown in Figure 1, the rich gas that carrys out catalytic cracking main fractionating tower enters rich gas compressor 1 through pipeline 101, is compressed to after 1.2-1.8MPa to enter water cooler 2 through pipeline 102 and be chilled to 20-50 DEG C and preferably enter knockout drum 3 after 40 DEG C.At the bottom of knockout drum, water is discharged through pipeline 105, and condensed oil enters desorption tower 5 tops or top through pipeline 104, desorption tower feed preheater 4.Knockout drum 3 top gas are sent into absorption tower 7 through pipeline 103 and are contacted with the absorption agent raw gasline from pipeline 110, absorb the liquefied gas component in gas.Eject the gas coming can enter absorbing-stabilizing system reabsorber through pipeline 109 from absorption tower 7.The liquid at 7 ends of absorption tower is through pipeline 108, the laggard knockout drum 3 of water cooler 2.Desorption tower 5 tower top materials enter knockout drum 3 after pipeline 106, water cooler 2.A part for the material at 5 ends of desorption tower is that at the bottom of the heavy constituent A of described liquid state enters and returns to tower after reboiler 6 heating, another part is that the heavy constituent B of described liquid state enters gasoline separation tower 8 through pipeline 107.Gasoline separation tower 8 tower tops go out the mixture containing liquefied gas and petroleum naphtha, after interchanger 15 preheatings, enter stabilizer tower 11 through pipeline 111.At the bottom of gasoline tower 8 towers, go out heavy petrol, at the bottom of a part is returned to tower after reboiler 9 heating, another part first goes desorb tower bottom reboiler 6 to do to go interchanger 4 preheating desorption tower chargings after thermal source again, be cooled to 40 DEG C finally by interchanger 16 and all go out device or a part and go absorption tower 7 tower tops to do to supplement absorption agent, another part goes out device.Stabilizer tower 11 tower top oil gas go condensate cooler 12 to be cooled to 40 DEG C of left and right through pipeline 115, enter knockout drum 13, and non-condensable gas is discharged through pipeline 116, and liquefied gas product is through pipeline 117 carrying devices.At the bottom of stablize petroleum naphtha A returning to tower after reboiler 10 heat containing a mixture part for petroleum naphtha and liquefied gas at the bottom of tower, another part stablizes petroleum naphtha B after interchanger 15 preheating stabilizer tower chargings, be cooled to 40 DEG C through interchanger 14 and all go out device or a part and go absorption tower 7 tower tops to do to supplement absorption agent, a part goes out device.Selecting which kind of in stable petroleum naphtha or heavy petrol to make to supplement absorption agent can select flexibly, takes temperature from supplementing the use of absorption agent, selects heavy petrol more favourable, but slave unit investment and work angle particularly energy consumption angle see that to select stable petroleum naphtha more suitable.
At the bottom of method of the present invention is utilized the tower that gasoline separation tower obtains cleverly, heavy petrol is as the thermal source that enters the condensed oil in desorption tower, before carrying device, first condensed oil is heated, and then the condensed oil after heating is sent in desorption tower, thereby the temperature of condensed oil can reach desorb requirement, has saved energy consumption.
In addition, sent in gasoline separation tower and separated by the tower base stream that desorb is obtained, tower top obtains the mixed oil and gas of liquefied gas and petroleum naphtha, obtains heavy petrol at the bottom of tower.Adopt this flow process can greatly reduce the load of stabilizer tower.And heavy petrol can meet product requirement without stablizing.In addition, the thermal source by heavy petrol that gasoline separation tower is obtained as desorption tower reboiler, energy efficient greatly.By the charging of stabilizer tower and discharging are carried out to heat exchange, the heat that can make full use of stabilizer tower discharging meets the heat of stabilizer tower charging.
Utilize stable petroleum naphtha that above-mentioned technique obtains owing to containing more alkene, therefore can produce low-carbon alkene or go ether-based device to produce high-octane rating blend component ether by freshening; Heavy petrol can go desulfurizer desulfurization to produce clean gasoline with high octane.In addition, as mentioned above, in the situation that raw gasline amount is inadequate, can use aforementioned stable petroleum naphtha and/or heavy petrol absorption agent as a supplement.The above-mentioned Comparison of separating methods containing gasoline mixture is flexible, can use as required aforementioned stable petroleum naphtha and/or heavy petrol absorption agent as a supplement.
The thermal source of gasoline separation tower tower bottom reboiler 9 can be provided by catalytic cracking main fractionating tower stage casing reflow heat source (preferably two in reflux), and temperature is generally 230-350 DEG C.Stablize tower bottom reboiler 10 the optional above-mentioned catalytic cracking main fractionating tower of thermal source one in or two in reflux (preferably one in reflux), temperature is generally 170-250 DEG C.
Fig. 2 is the schematic flow sheet of the disclosed separation method containing gasoline mixture of prior art CN1542085A.Stablize flow process cardinal principle identical with absorbing described in Fig. 1.Difference is after preheater 15 preheatings, to enter stabilizer tower 11 through pipeline 111 at material out at the bottom of desorption tower 5 towers, stabilizer tower 11 tower tops go out liquefied gas, at the bottom of tower, go out blend gasoline, at the bottom of wherein a part for this blend gasoline is returned to tower after reboiler 10 heating, another part goes to enter gasoline separation tower 8 through pipeline 119 after interchanger 4 preheating desorption tower chargings after interchanger 15 preheating stabilizer tower 11 chargings again.The tower top of this gasoline separation tower 8 obtains stable petroleum naphtha, obtains heavy petrol at the bottom of tower, and wherein stable petroleum naphtha is through pipeline 120 carrying devices, and at the bottom of a heavy petrol part is returned to tower after reboiler 9 heating, another part goes out device through being cooled to 40 DEG C.The tower top temperature of gasoline separation tower 8 is 40-80 DEG C, and column bottom temperature is 130-170 DEG C, and tower top pressure is 0.1-0.5MPa.
Can find out by Fig. 1 and Fig. 2 contrast, what the separation method provided by the invention shown in Fig. 1 need to extraneous provide thermal source is reboiler 9 and reboiler 10, and the separation method of the prior art shown in Fig. 2 need extraneous provide thermal source except reboiler 9 and reboiler 10, also have reboiler 6.Therefore,, compared with the method for prior art, method energy consumption provided by the invention reduces greatly.
The following examples are further described the present invention as an example of the catalytic cracking unit of 2,000,000 tons/year of a set for the treatment of capacities example.Utilize Aspen plus software to stablize flow process to catalytic cracking fractionation absorption and carry out analog calculation.The about 185t/h of rich gas amount, the about 100t/h of raw gasline amount.Gently, heavy petrol cut point be that heavy petrol 5v% distillates is a little 90 DEG C.Quality product requires: rich gas propylene specific absorption > 97%, C5 in liquefied gas product
+< 1% (volume), stable petroleum naphtha C4
-< 1% (quality).
Embodiment 1
This embodiment is for illustrating the separation method containing gasoline mixture provided by the invention.
Adopt flow process shown in Fig. 1 to separate the condensed oil that carrys out catalytic cracking main fractionating tower, gasoline separation tower 8 is after desorption tower 5, before stabilizer tower 11, using the naphtha fraction of catalytic cracking main fractionating tower as absorption agent, the stable petroleum naphtha obtaining with stabilizer tower 11 makes to supplement absorption agent.The inlet amount of condensed oil is 206t/h, and the temperature of entering before interchanger 4 is 40 DEG C, and the temperature that goes out interchanger 4 is 65 DEG C; The flow of the mixture containing gasoline and liquefied gas that discharge at gasoline separation tower 8 tops is 99.4t/h, and the temperature of entering before interchanger 15 is 114 DEG C, and the temperature that goes out interchanger 15 is 122 DEG C; The temperature that petroleum naphtha enters interchanger 15 is 140 DEG C.Operating parameters and the analog calculation of each tower the results are shown in Table 1, and the amount of stablizing petroleum naphtha in table 1 refers to the amount of outer row's petroleum naphtha, do not comprise the amount that enters interchanger 10 and return the stable petroleum naphtha of stabilizer tower 11.The amount of described heavy petrol refers to the amount of outer row's heavy petrol, does not comprise the amount that enters interchanger 9 and return the heavy petrol of gasoline separation tower 8, and following examples are identical.
This embodiment is for illustrating the separation method containing gasoline mixture provided by the invention.
Adopt flow process shown in Fig. 1 to separate the condensed oil that carrys out catalytic cracking main fractionating tower, gasoline separation tower 8 is after desorption tower 5, before stabilizer tower 11, using the raw gasline of catalytic cracking main fractionating tower as absorption agent, the heavy petrol obtaining with gasoline separation tower 8 makes to supplement absorption agent.The inlet amount of condensed oil is 222t/h, and the temperature of entering before interchanger 4 is 40 DEG C, and the temperature that goes out interchanger 4 is 65 DEG C; The flow of the mixture containing gasoline and liquefied gas that discharge at gasoline separation tower 8 tops is 70.9t/h, and the temperature of entering before interchanger 15 is 104 DEG C, and the temperature that goes out interchanger 15 is 114 DEG C; The temperature that the stable petroleum naphtha that stabilizer tower 11 obtains enters interchanger 15 is 138 DEG C.Operating parameters and the analog calculation of each tower the results are shown in Table 1.
Adopt flow process shown in Fig. 1 to separate the condensed oil that carrys out catalytic cracking main fractionating tower, gasoline separation tower 8 is after desorption tower 5, before stabilizer tower 11, using the raw gasline of catalytic cracking main fractionating tower as absorption agent, the stable petroleum naphtha obtaining with stabilizer tower 11 makes to supplement absorption agent.The inlet amount of condensed oil is 185t/h, and the temperature of entering before interchanger 4 is 40 DEG C, and the temperature that goes out interchanger 4 is 70 DEG C; The flow of the mixture containing gasoline and liquefied gas that discharge at gasoline separation tower 8 tops is 63.5t/h, and the temperature of entering before interchanger 15 is 119 DEG C, and the temperature that goes out interchanger 15 is 130 DEG C; The temperature that the stable petroleum naphtha that stabilizer tower 11 obtains enters interchanger 15 is 160 DEG C.Operating parameters and the analog calculation of each tower the results are shown in Table 1.
Embodiment 4
Adopt flow process shown in Fig. 1 to separate the condensed oil that carrys out catalytic cracking main fractionating tower, gasoline separation tower 8 is after desorption tower 5, before stabilizer tower 11, using the raw gasline of catalytic cracking main fractionating tower as absorption agent, the stable petroleum naphtha obtaining with stabilizer tower 11 makes to supplement absorption agent.The inlet amount of condensed oil is 235t/h, and the temperature of entering before interchanger 4 is 40 DEG C, and the temperature that goes out interchanger 4 is 60 DEG C; The flow of the mixture containing gasoline and liquefied gas that discharge at gasoline separation tower 8 tops is 90.2t/h, and the temperature of entering before interchanger 15 is 145 DEG C, and the temperature that goes out interchanger 15 is 154 DEG C; The temperature that the stable petroleum naphtha that stabilizer tower 11 obtains enters interchanger 15 is 250 DEG C.Operating parameters and the analog calculation of each tower the results are shown in Table 1.
Comparative example 1
Adopt flow process described in Fig. 2 to separate the condensed oil that carrys out catalytic cracking main fractionating tower, gasoline separation tower 8 is located at after stabilizer tower 11, and using the naphtha fraction of catalytic cracking main fractionating tower as absorption agent, the heavy petrol obtaining with gasoline separation tower makes to supplement absorption agent.Operating parameters and the analog calculation of each tower the results are shown in Table 1.
Table 1
| Operating parameters | Embodiment 1 | |
|
Embodiment 4 | Comparative example 1 |
| Absorption tower | |||||
| Stage number | 40 | 40 | 30 | 50 | 40 |
| Tower top pressure, MPa | 1.4 | 1.4 | 2 | 1 | 1.4 |
| Tower top temperature, DEG C | 42 | 40 | 55 | 40 | 44 |
| Column bottom temperature, DEG C | 46 | 46 | 60 | 45 | 47 |
| Desorption tower | |||||
| Stage number | 40 | 40 | 50 | 30 | 40 |
| Tower top pressure, MPa | 1.5 | 1.5 | 2 | 1 | 1.5 |
| Tower top temperature, DEG C | 68 | 68 | 60 | 52 | 68 |
| Column bottom temperature, DEG C | 120 | 115 | 150 | 110 | 119 |
| Discharging at the bottom of tower, t/h | 184.6 | 201.5 | 179.6 | 200.7 | 183.8 |
| Gasoline separation tower | |||||
| Stage number | 35 | 20 | 40 | 45 | 20 |
| Feed entrance point | 15 | 10 | 20 | 25 | 10 |
| Tower top pressure, MPa | 1.2 | 1.2 | 1 | 2 | 0.2 |
| Tower top temperature, DEG C | 104 | 115 | 120 | 145 | 50 |
| Column bottom temperature, DEG C | 233 | 232 | 210 | 250 | 140 |
| Trim the top of column ratio | 0.4 | 0.4 | 0.3 | 0.6 | 0.8 |
| Heavy petrol, t/h | 83.9 | 81.9 | 74.8 | 82.5 | 79.9 |
| Stabilizer tower | |||||
| Stage number | 40 | 40 | 50 | 80 | 40 |
| Feed entrance point | 20 | 20 | 20 | 30 | 20 |
| Tower top pressure, MPa | 1.17 | 1.18 | 1.5 | 2 | 1.18 |
| Tower top temperature, DEG C | 50 | 45 | 40 | 70 | 45 |
| Column bottom temperature, DEG C | 140 | 138 | 160 | 250 | 192 |
| Trim the top of column ratio | 1.55 | 2.3 | 2.6 | 2.9 | 1.5 |
| Liquefied gas, t/h | 42.0 | 41.6 | 35.6 | 46.8 | 38.4 |
| Stablize petroleum naphtha, t/h | 26.4 | 29.1 | 27.5 | 43.5 | 34.4 |
| Supplement absorption dose, t/h | 34.3 | 47.9 | 28.6 | 37.9 | 51.9 |
| Total heating load, MW | 27.07 | 27.82 | 25.9 | 28.7 | 31.75 |
| Total cooling load, MW | 23.50 | 24.64 | 22.1 | 23.9 | 27.85 |
Can find out from analog calculation result, require identical in the situation that in each quality product, each scheme all can meet processing requirement.Embodiment 2 supplementary absorption dose minimum used, embodiment 1 energy consumption is minimum, and the supplementary absorption agent consumption of comparative example 1 is large, energy consumption is also high, has embodied thus advantage of the present invention.
Claims (12)
1. containing a separation method for gasoline mixture, the method comprises the following steps:
(1) should, containing carrying out desorb after gasoline mixture heating, contain the light constituent dry gas of gasoline mixture mid-boiling point lower than liquefied gas to isolate this, obtain liquid heavy constituent;
(2) liquid heavy constituent A heating is mixed and carries out the desorb of above-mentioned steps (1) afterwards with containing gasoline mixture, liquid heavy constituent B is separated into mixture and the heavy petrol containing petroleum naphtha and liquefied gas, wherein, the heavy constituent A of described liquid state is a part for the heavy constituent of step (1) gained liquid state, and the heavy constituent B of described liquid state is the remainder of the heavy constituent of step (1) gained liquid state;
(3) gained is separated into liquefied gas and stable petroleum naphtha after the mixture heating containing petroleum naphtha and liquefied gas;
(4) after stablizing petroleum naphtha A heating, mix and carry out the operation of above-mentioned steps (3) with the mixture that contains petroleum naphtha and liquefied gas, described stable petroleum naphtha A is the part that step (3) gained is stablized petroleum naphtha;
Wherein, to the heating of the described mixture containing petroleum naphtha and liquefied gas by described mixture and stable petroleum naphtha B heat exchange containing petroleum naphtha and liquefied gas realized, described stable petroleum naphtha B is the remainder that step (3) gained is stablized petroleum naphtha, with the temperature of the described mixture containing petroleum naphtha and liquefied gas after described stable petroleum naphtha B heat exchange be 60-150 DEG C, the weight ratio of described stable petroleum naphtha B and the described mixture containing petroleum naphtha and liquefied gas is 0.1-0.9:1, the temperature head of described stable petroleum naphtha B and the described mixture containing petroleum naphtha and liquefied gas is 10-100 DEG C, the heating of heavy constituent A to described liquid state and to containing the heating of gasoline mixture by by described heavy petrol successively with the heavy constituent A of described liquid state and describedly realize containing gasoline mixture heat exchange, with the temperature of the heavy constituent A of the described liquid state after described heavy petrol heat exchange be 30-150 DEG C, the weight ratio of the heavy constituent A of described heavy petrol and described liquid state is 0.1-1:1, and the temperature head of the heavy constituent A of described heavy petrol and described liquid state is 20-200 DEG C.
2. separation method according to claim 1, wherein, with the described temperature containing gasoline mixture after described heavy petrol heat exchange be 50-100 DEG C.
3. separation method according to claim 2, wherein, described heavy petrol and the described weight ratio that contains gasoline mixture are 0.2-0.9:1, described heavy petrol and the described temperature head that contains gasoline mixture are 50-230 DEG C.
4. separation method according to claim 3, wherein, described heavy petrol and the described weight ratio that contains gasoline mixture are 0.3-0.8:1, described heavy petrol and the described temperature head that contains gasoline mixture are 80-200 DEG C.
5. separation method according to claim 1, wherein, the described gasoline mixture that contains contains liquefied gas, petroleum naphtha and heavy petrol, taking the described total amount containing gasoline mixture as benchmark, the content of described liquefied gas is 10-60 % by weight, the content of described petroleum naphtha is 10-70 % by weight, and the content of described heavy petrol is 20-80 % by weight.
6. separation method according to claim 5, wherein, described is overhead oil air pressure by catalytic cracking the is obtained condensed oil that the laggard row gas-liquid separation of condensation obtains that contracts containing gasoline mixture.
7. according to the separation method described in claim 1 or 6, wherein, described desorb is carried out in desorption tower, the tower top pressure of desorption tower is 1-2MPa, tower top temperature is 50-90 DEG C, column bottom temperature is 100-160 DEG C, and at the bottom of tower, the weight ratio of load and inlet amount is 0.1-0.99:1, and stage number is 30-50 piece.
8. according to the separation method described in claim 1 or 6, wherein, in step (2), carry out containing being separated in gasoline separation tower between the mixture of petroleum naphtha and liquefied gas and heavy petrol, the tower top pressure of described gasoline separation tower is 1-2MPa, tower top temperature is 100-150 DEG C, column bottom temperature is 200-265 DEG C, and trim the top of column is than being 0.2-3, and stage number is 20-50 piece.
9. according to the separation method described in claim 1 or 6, wherein, step (3) is carried out in stabilizer tower, the tower top pressure of described stabilizer tower is 1-2MPa, and tower top temperature is 40-80 DEG C, and column bottom temperature is 100-200 DEG C, trim the top of column is than being 0.5-3, and stage number is 30-50 piece.
10. separation method according to claim 6, wherein, described gas-liquid separation obtains water, condensed oil and top gas, and the method also comprises described top gas and absorption agent counter current contact, to absorb the liquefied gas component in top gas.
11. separation methods according to claim 10, wherein, the described absorption agent of part be successively with the heavy constituent A of described liquid state and described containing the part in the heavy petrol after gasoline mixture heat exchange, and be the 20-90 % by weight of the total consumption of absorption agent as the amount of the heavy petrol of described absorption agent.
12. separation methods according to claim 10, wherein, the described absorption agent of part is described stable petroleum naphtha A, and is the 10-80 % by weight of the total consumption of absorption agent as the amount of the stable petroleum naphtha of described absorption agent.
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| CN1321724A (en) * | 2001-04-30 | 2001-11-14 | 中国石化集团安庆石油化工总厂 | Absorption stabilizing process for refining oil |
| CN1236018C (en) * | 2003-04-29 | 2006-01-11 | 中国石油化工股份有限公司 | Method for separating catalytically cracked gasoline |
| 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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