CN1986741A - Auxiliary fractional tower and its gasoline catalyzing and olefine reducing modification process - Google Patents
Auxiliary fractional tower and its gasoline catalyzing and olefine reducing modification process Download PDFInfo
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- CN1986741A CN1986741A CN 200610124009 CN200610124009A CN1986741A CN 1986741 A CN1986741 A CN 1986741A CN 200610124009 CN200610124009 CN 200610124009 CN 200610124009 A CN200610124009 A CN 200610124009A CN 1986741 A CN1986741 A CN 1986741A
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Abstract
The present invention discloses a kind of auxiliary fractional tower and its gasoline catalyzing and olefin reducing modification process. The auxiliary fractional tower is provided with 16 tower plates to separate the inside of the tower into 17 layers, one shed angle baffle in the 17-th layer with reaction oil gas inlet, stirring steam inlet, oil slurry inlet and oil slurry outlet, and one liquid separating tank connected through a heat exchanger to the tower top. The auxiliary fractional tower has simplified structure, optimized energy utilization, high heat efficiency and low power consumption.
Description
Technical field
The present invention relates to heavy oil fluid catalytic cracking technical field in the petroleum refining industry, specifically be meant a kind of auxiliary fractional tower and gasoline catalyzing and olefine reducing modification process thereof.
Background technology
In China petroleum refining industry secondary processing technology, catalytic cracking process occupies extremely important position, and the overwhelming majority of gasoline and diesel oil all comes from catalytic cracking in the domestic market; It is again the rich and influential family of refining energy consumption simultaneously, and its power consumption of polymer processing almost accounts for 1/3 of oil refining apparatus total energy consumption.Constantly become the requirement of strictness and high-yield diesel oil, propylene and liquid hydrocarbon day by day of heavy, oil quality index in order to adapt to crude oil, in recent years, catalytic cracking Research on New and use very active." the alkene technology falls in catalytic gasoline auxiliary reactor upgrading " is exactly an example.This technology is a target with olefin(e) centent, the lifting quality of gasoline that reduces catalytic gasoline, on the basis of existing catalytic cracking process, independently raw gasline freshening subsidiary riser reactive system and the auxiliary fractionating system of reformulated gasoline have been set up, allow and fall two different reaction process of alkene and catalytic cracking main reaction and in different reaction zones, carry out, and the gasoline behind the upgrading is independently being separated in the separation column.This technology five covers of PetroChina Company Ltd. on the catalytic cracking unit successful realization industrial applications, obtained that the catalytic gasoline olefin(e) centent is reduced to 20～35%, octane value remains unchanged substantially or had only the good result of less reduction.Owing to set up raw gasline freshening assisted reaction and auxiliary separation system, the more former technology of plant energy consumption is significantly increased.The operation result of existing application apparatus shows: device unit power consumption of polymer processing on average increases by 10～15KgEO/ ton virgin material.Therefore, cutting down the consumption of energy is the key that decision " the alkene technology falls in catalytic gasoline auxiliary reactor upgrading " is further used and developed, and also is present application apparatus problem anxious to be solved.
From existing technological flow analysis, it is irrational that 40 ℃ low temperature liquid phase raw gasline directly enters the subsidiary riser reactor bed.Because the 40 ℃ of chargings of liquid phase raw gasline and the contact of the finish up to the 650 ℃ temperature difference, must cause raw gasline in the uneven distribution of catalyst surface with prolong finish duration of contact, aggravation condensation and scission reaction generate coke and dry gas, thereby improve plant energy consumption and reduce yield of gasoline.Meanwhile, form great raw gasline and high-temperature regenerated catalyst and mix fire, seriously reduce the quality of utilizing of reaction-regeneration system energy with decreasing.So, improve the temperature that raw gasline enters subsidiary riser, realize full vapour phase charging; Reducing the regenerator temperature by the outside heat removing means simultaneously, to reduce the finish contact temperature difference, distribute thereby improve reactor product, is the key that reduces coke and dry gas growing amount, is the core measure that reduces the energy consumption of prior art.Analysis-by-synthesis, there is following unreasonable part in the energy utilization of existing reflux heat:
1, the heat of circulation slurry oil is used by serious degradation.1.0Mpa the temperature of saturation of steam has only 180 ℃, by the existing procedure operation, the mean temperature difference of vapour generator is 150 ℃, causes great heat transfer fire with decreasing.In fact, the heat of slurry oil backflow can be used to take place the middle pressure steam (its temperature of saturation is 243 ℃) of 3.5Mpa fully.
2, the heat of stage casing backflow is also used by serious degradation.In the existing technology, the inlet temperature of deaerated water is 93 ℃, and temperature out is 126 ℃; And the inlet temperature of stage casing recuperator is 250 ℃, and temperature out is 170 ℃, and its mean temperature difference reaches 100 ℃, is higher than the domestic advanced design level about 20 ℃ far away.From the viewpoint of potential temperature step coupling, should arrange more suitable stage casing backflow heat exchange process.
3, not utilization of heat is followed on the top of the suitable potential temperature of part, not only causes calorific loss, has strengthened the cooling load of system simultaneously.In the existing technology, for guarantee to push up follow return the tower temperature, do regulating measure with air cooling, will follow with 95 ℃ top after the heat exchange of deaerated water and directly be cooled to 80 ℃ and return tower, about 100 * 10
4The heat of Kcal/h is wasted.
Summary of the invention
Purpose of the present invention is exactly in order to solve above-mentioned the deficiencies in the prior art part, and a kind of auxiliary fractional tower and gasoline catalyzing and olefine reducing modification process thereof are provided.The gasoline catalyzing and olefine reducing modification process of this auxiliary fractional tower and realization thereof is that the optimization that catalytic gasoline upgrading process energy utilizes is improved, heat preheating raw gasline with auxiliary fractional tower, realize that complete vapour phase enters the service hoisting pipe reactor, reduce the finish contact temperature difference, thereby improving reactor product distributes, reduce coke and dry gas growing amount, and then reduce the energy consumption of whole subsystem.
Purpose of the present invention is achieved through the following technical solutions: described a kind of auxiliary fractional tower, comprise tower body, in the described tower body from top to bottom horizontal direction column plate is installed, described column plate has 16, whole tower body inside is divided into 17 layers, described the 17th layer is washing section, this section vertical direction is equipped with chevron shaped baffle plate, the bottom tower body of described chevron shaped baffle plate is respectively arranged with the reaction oil gas opening for feed, stir the steam feed mouth, the top tower body of described chevron shaped baffle plate is provided with the slurry oil opening for feed, described tower body bottom is provided with the slurry oil discharge port, the tower tray of described the 16th block of column plate is provided with the stage casing and diesel oil is extracted mouth out, described the 13rd block of column plate is provided with the stage casing and returns opening for feed, described stage casing and diesel oil are extracted mouth out by the stage casing recycle pump, the stage casing interchanger returns opening for feed with the stage casing and is connected, the tower tray of described the 4th block of column plate is provided with the top and follows the extraction mouth, described the 1st block of column plate is respectively arranged with the trim the top of column opening for feed, the top is followed and is returned the tower opening for feed, described top is followed the extraction mouth and is followed extractor pump by the top, overhead heat exchanger and top are followed and are returned the tower opening for feed and be connected, described tower body top is provided with oil gas vent, described oil gas vent is connected with the branch flow container by interchanger, described separatory pot bottom is respectively arranged with water port, raw gasline is extracted mouth out, and the top is provided with the rich gas discharge port.
In order to realize the present invention better, the external main fractionating tower of slurry oil opening for feed that the top tower body of described chevron shaped baffle plate is provided with; The slurry oil discharge port of described tower body bottom is connected with main fractionating tower by slurry oil extractor pump and slurry heat-exchanger; Pass through the recycle stock return port of the external main fractionating tower of stage casing diesel oil extractor pump between described stage casing recycle pump, the stage casing interchanger; Described raw gasline is extracted mouth, rich gas discharge port external absorbing-stabilizing system respectively out; Flow container also was connected with the trim the top of column opening for feed by pump in described minute.
The gasoline catalyzing and olefine reducing modification process that adopts auxiliary fractional tower of the present invention to realize comprises the steps and processing condition:
The first step enters the bottom of auxiliary fractional tower by the reaction oil gas opening for feed from the pyroreaction oil gas of assisted reaction system, promptly below the chevron shaped baffle plate of the 17th layer of washing section, 1.0MPa superheated vapour enter the bottom of auxiliary fractional tower by stirring the steam feed mouth equally, enter the top of the chevron shaped baffle plate of the 17th layer of washing section in the auxiliary fractional tower by the slurry oil opening for feed from the slurry oil of main fractionating tower, the catalyst dust that process washing reaction oil gas is carried secretly, after the heat exchange of pyroreaction oil gas, slurry oil discharge port at the bottom of tower is extracted out, the feeding temperature of described pyroreaction oil gas is 400～450 ℃, and feed pressure is 0.20～0.23MPa;
The second step pyroreaction oil gas is by the oil gas vent output at tower body top, be divided into two-way, respectively with raw gasline, after condensed water or the deaerated water heat exchange, utilize recirculated water, condensed water or de-mineralized water continue to make the reaction oil gas temperature to drop to 30～40 ℃, enter the branch flow container, 30～40 ℃ upgrading raw gasline is extracted out from the bottom of minute flow container, a part is directly removed absorbing-stabilizing system, another part directly returns the trim the top of column opening for feed of the 1st block of column plate of tower body as the cat head cold reflux, 30～40 ℃ rich gas is extracted out from the top of minute flow container and is also directly removed absorbing-stabilizing system, and the oil gas output pressure at tower body top is 0.16～0.22MPa;
The 3rd step top is followed with pump and is followed extraction mouthful extraction from the top of the 4th block of column plate, through with the heat exchange of cat head oil gas after the raw gasline heat exchange after, with condensed water or de-mineralized water the top is followed again and continued to be cooled to 80～100 ℃, the top of returning the 1st block of column plate is followed and is returned the tower opening for feed, the temperature of returning that the control top is followed is 80～100 ℃, to guarantee the thermal equilibrium of whole tower;
The 4th step diesel oil and stage casing backflow one are reinstated the stage casing recycle pump and are extracted a mouthful extraction out from the stage casing and the diesel oil of the 16th block of column plate, diesel oil directly removes main fractionating tower recycle stock return port by stage casing diesel oil extractor pump, and reflux in the stage casing and the raw gasline heat exchange after preheating is followed on the top is lowered the temperature, be aided with secondary condensed water or de-mineralized water return the tower temperature as the stage casing backflow regulating measure, after making temperature drop to 170～190 ℃, return the stage casing of the 13rd block of column plate and return opening for feed, the tower temperature of returning that refluxes in the control stage casing is 170～190 ℃, to guarantee the thermal equilibrium of whole tower;
The 5th step continued with the slurry oil heat exchange of coming out at the bottom of the tower with the raw gasline that stage casing backflow heat exchange is come out, to utilize the heat of the high potential temperature thermal source of system to greatest extent, fully improve preheating temperature, raw gasline is warmed up to more than the bubble point, realize that complete vapour phase enters subsidiary riser, the circulation slurry oil continues to be used for taking place the low-pressure steam of 1.0MPa, it is cooled to returns main fractionating tower when entering the identical temperature of auxiliary fractional tower, through with the slurry oil heat exchange after the vaporization rate α of raw gasline be 1.
Principle of design of the present invention is analyzed as follows:
1, the present invention proposes the method for the energy-optimised utilization of catalytic gasoline upgrading process.Promptly improve temperature that raw gasline advances subsidiary riser to full vapour phase charging, reduce the finish contact temperature difference, distribute, reduce the growing amount of coke, reach the purpose of the energy consumption that reduces catalytic gasoline upgrading process thereby improve reactor product.
2, the present invention proposes new auxiliary fractional tower separation process, i.e. cancellation has separation column diesel oil now with the segregation section down to slurry oil, and diesel oil is returned main fractionating system freshening.It is consistent with former auxiliary fractionating system to keep the above column plate of diesel oil extraction, simplifies the structure and the operation of auxiliary fractional tower.
3, on the basis of optimizing new auxiliary fractional tower system capacity distribution, it is the heat exchange process of main hot trap that the present invention has set up with raw gasline, and the heat exchange that improves raw gasline is warm eventually.The heat of the new auxiliary fractionating system of utilize optimizing is preheating to 200～250 ℃ with raw gasline from 40 ℃ liquid phase, realize full vapour phase charging, reduce raw gasline with this and contact the temperature difference and improve homogeneity, suppress coke and generate with the finish of regenerated catalyst at subsidiary riser; The heat of high temperature of replacing out regenerated catalyst simultaneously is by means generation middle pressure steams such as inside and outside heat collectors, thereby the upgrading utilization of the auxiliary fractionating system energy of realization reduces the subsystem energy consumption.
4, improved auxiliary fractional tower is established 16 blocks of column plates.Cat head adopts zero cold reflux operation, is intended to reduce overhead oil air pressure and falls.The top pump around circuit is extracted out from the 4th block of column plate, returns the 1st block of column plate of cat head after the heat exchange.Diesel oil and stage casing backflow one arise from the 16th block of column plate and extract out, and diesel oil directly removes main fractionating tower recycle stock return port, reflux through returning the 13rd block of column plate after the heat exchange cooling in the stage casing.Washing oil is used for from main fractionating tower through the about 275 ℃ circulation slurry oil after the heat exchange, by being located at the multilayer herringbone baffle plate of tower bottom, remove catalyzer remnant going along with in the reaction oil gas, at the bottom of tower, extract out, heat exchange cools to 275 ℃ and returns then, to guarantee main fractionating tower thermal equilibrium.Because of the slurry oil internal circulating load of existing process unit seldom, the heat-obtaining amount can not reach the requirement that steam takes place.The design of auxiliary fractional tower does not adopt self tower still slurry oil to do the circulation slurry oil among the present invention, and with the circulation slurry oil after the heat exchange of main fractionating tower as washing medium.Since can to wash away the upgrading slurry oil fully from 275 ℃ of circulation slurry oil amounts of main fractionating tower be good, raw gasline is preheated to full vapour phase charging and gets final product.
The present invention compared with prior art has following advantage and beneficial effect:
1, the present invention has simplified the structure and the operation of existing auxiliary fractional tower, has optimized the energy distribution of system.
2, the present invention has set up the new heat exchange process that utilizes the fractionating system heat to heat raw gasline step by step, has realized the using energy of system.
3, the present invention improves the temperature that raw gasline advances riser reactor, reduces the coke and the dry gas yied of system.Because the present invention has improved the raw gasline feeding temperature, reduce the finish contact temperature difference, the process fire that has reduced the service hoisting pipe reactor is with decreasing.Simultaneously owing to reduced the finish contact temperature difference in the riser tube, for improving the distribution of raw gasline, reduce the residence time, alleviate polymerization and cracking severity, thereby reduced the productive rate of coke and dry gas at catalyst surface.
4, the present invention improves the temperature that raw gasline advances riser reactor, has realized reaction-regeneration system fecund steam, has improved the energy quality of gasoline upgrading process.By utilizing the heat heating raw gasline of reformulated gasoline separation system, raw gasline is heated to 200～250 ℃ from 40 ℃, be actually the high-quality heat that the more inferior heat of the auxiliary fractionating system of equivalent has been converted to reaction-regeneration system equivalent, therefore middle pressure steam can take place, the energy upgrading that has realized whole catalytic cracking unit utilizes, and has improved the energy quality of gasoline upgrading process.
5, the present invention has improved the utilising efficiency of auxiliary fractional tower energy, has reduced plant energy consumption.Heat raw gasline by the heat that utilizes auxiliary separation system, and optimize its heat exchanger network design, the energy that has improved the reformulated gasoline separation system utilizes level.The net heat utilising efficiency of comparing the auxiliary fractionating system of existing technology improves, and has reduced the plant energy consumption of auxiliary fractionating system.
6, the new auxiliary fractional tower of the present invention's design is compared the separation column of existing technology, has not only simplified the structure of tower, and more the actually operating with existing running gear matches.Simultaneously, the heat-obtaining of optimization distributes and also will lay the foundation for utilizing its heat preheating raw gasline.
Description of drawings
Fig. 1 is that the alkene schematic flow sheet falls in existing catalytic gasoline auxiliary reactor upgrading;
Fig. 2 is the structural representation of existing auxiliary fractional tower;
Fig. 3 is the heat exchange process figure of existing fractionating system;
Fig. 4 is the structural representation of auxiliary fractional tower of the present invention;
Fig. 5 is the heat preheating raw gasline that the present invention utilizes new auxiliary fractional tower, realizes the heat exchanger network schema of full vapour phase charging.
Embodiment
Below in conjunction with drawings and Examples, the present invention is done detailed description further, but embodiments of the present invention are not limited to this.
As shown in Figure 1, the flow process of existing raw gasline is: heavy oil reacts with regenerated catalyst in the heavy oil riser reactor, and the reaction oil gas of generation enters main fractionating tower, separates the output slurry oil respectively in the bottom, and output diesel oil is separated at the middle part.Divide 40 ℃ liquid phase raw gasline of flow container under the effect of pump merit from the FCC main fractionating tower cat head, directly enter the service hoisting pipe reactor and contact at pre lift zone without preheating from about 670～690 ℃ regenerated catalyst of revivifier, reactions such as alkene are fallen from bottom to top along pipe, and reaction oil gas is separated with reclaimable catalyst at the special settling section that is provided with, spent agent after the separation goes the revivifier regeneration, and the reformulated gasoline knockout tower (being auxiliary fractional tower) that reaction oil gas then advances special setting separates.About 430 ℃ reaction oil gas behind the upgrading enters auxiliary fractional tower, cat head oil gas is cooled to 40 ℃ through overhead condenser, isolated upgrading raw gasline and rich gas behind minute flow container remove absorbing-stabilizing system from separatory pot bottom and top extraction respectively, and diesel oil is extracted out from the middle part of tower.The slurry oil that comes out at the bottom of the tower, has also been established top pump around circuit and stage casing and has been refluxed in order to guarantee to extract the quality of product and the heat that reclaims fractionating system out by the low-pressure steam cooling back circulation of 1.0Mpa takes place, and the heat of taking-up is used for taking place hot water.
As shown in Figure 2, existing auxiliary fractional tower comprises tower body 1, in the tower body 1 from top to bottom horizontal direction 24 blocks of column plates are installed, whole tower body 1 inside is divided into 25 layers, the 25th layer is washing section, this section vertical direction is equipped with chevron shaped baffle plate 12, the bottom tower body of chevron shaped baffle plate 12 is respectively arranged with reaction oil gas opening for feed 9, stir steam feed mouth 10, the top tower body of chevron shaped baffle plate 12 is provided with slurry oil opening for feed 11 (slurry oil circulation at the bottom of the tower), tower body 1 bottom is provided with slurry oil discharge port 34, be connected with main fractionating tower by slurry oil extractor pump 31 and vapour generator 28, the tower tray of the 20th column plate 1-20 is provided with the stage casing and extracts mouth 4 out, the 16th column plate 1-16 is provided with the stage casing and returns opening for feed 5, the stage casing is extracted mouth 4 out by stage casing recycle pump 30, two placed in-line stage casing interchanger 17,18 and air cooling 42 return opening for feed 5 with the stage casing and be connected, simultaneously, the tower tray of the 16th column plate 1-16 is provided with diesel oil and extracts mouth 6 out, by diesel oil extractor pump 32, opening for feed 7 conducts of returning that the diesel oil part withdrawing device of extracting out, another part return the 14th column plate 1-14 reflux.The tower tray of the 5th column plate 1-5 is provided with the top and follows extraction mouth 3, the 1st column plate 1-1 is respectively arranged with trim the top of column opening for feed 8, the top is followed and is returned tower opening for feed 2, the top is followed and is extracted mouthfuls 3 out and follow extractor pump 29 by the top, two placed in-line overhead heat exchangers 13,14 and air cooling 41 and top follow and return tower opening for feed 2 and be connected, tower body 1 top is provided with oil gas vent 35, oil gas vent 35 is by two strings two, four interchanger 19 also, 20,21, the interchanger 23 of 22 and three parallel connections, 24,25 are connected with branch flow container 27, divide the top of flow container 27 to be provided with oil gas opening for feed 36, rich gas discharge port 37, rich gas discharge port 37 external absorbing-stabilizing systems, divide the bottom of flow container 27 to be respectively arranged with water port 38, the upgrading raw gasline is extracted mouth 39 out, extract of the effect of mouthful 39 upgrading raw gasline that come out out from the upgrading raw gasline through pump 33, a part is connected with trim the top of column opening for feed 8 as the cat head cold reflux, another part goes out device as product, enters rearmounted absorbing-stabilizing system.
Because the raw gasline freshening is finished the olefine reducing modification process, upgraded product, promptly upgrading reaction oil gas component is lighter, and the solar oil produced quantity of the auxiliary fractional tower of actual existing operation is seldom, simultaneously at the bottom of the tower circulation slurry oil extraction heat seldom, oil slurry steam generator is not sent out vapour substantially.Because diesel oil distillate can return main fractionating system freshening less, auxiliary separation system can be strict with the quality of diesel oil, so the fractionation section effect that diesel oil extraction plate to the slurry oil that circulates returns between the tower is little.
As shown in Figure 3, existing heat exchange process is: from the pyroreaction oil gas (79.796t/h of assisted reaction system, 430 ℃, 0.215MPaA) enter the bottom of auxiliary fractional tower, promptly the reaction oil gas opening for feed 9 of chevron shaped baffle plate 12 belows of the 25th layer of washing section enters in the tower, 0.5t/h the superheated vapour of 1.0MPa equally also enter in the tower from the stirring steam feed mouth 10 of the below of the chevron shaped baffle plate 12 of the 25th layer of washing section, from the next 50t/h of main fractionating tower, 275 ℃ slurry oil enters in the tower from the slurry oil opening for feed 11 of the top of the herringbone baffle plate 12 of the 25th layer of washing section, the catalyst dust that process washing reaction oil gas is carried secretly, after the heat exchange of pyritous reaction oil gas, behind slurry oil extractor pump 31 and vapour generator 28, at the bottom of tower, extract out.
Come out from cat head 130 ℃, the cat head oil gas of 0.185MPaA, 74.5t/h are divided into two-way, respectively by two strings two and four interchanger 19,20,21,22 (total heat duties is 576 * 10
4Kcal/hr) with 40 ℃, the condensed water heat exchange of 120t/h after, the temperature of cat head oil gas is reduced to 60 ℃, cat head oil gas continues interchanger 23,24,25 through three parallel connections, and (total heat duties is 374 * 10
4Kcal/hr) continue to make cat head oil gas to drop to 40 ℃ with 28 ℃, the recirculated water of 584t/h, enter the opening for feed 36 of branch flow container, the temperature of recirculated water is upgraded to 34.4 ℃.After 40 ℃ upgrading raw gasline was extracted out from the discharge port 39 usefulness pumps 33 of minute flow container, a part was removed absorbing-stabilizing system, and another part enters the cold reflux of the backflow opening for feed 8 of the 1st column plate 1-1 as cat head.40 ℃ rich gas is extracted mouthful 37 extractions out and is also removed absorbing-stabilizing system from the top of minute flow container.
133.5t/h, 149 ℃ top follows to follow from the top of the 5th column plate 1-5 with top recycle pump 29 and extracts mouthfuls 3 out and extract out, (total heat duties is 343 * 10 through two placed in-line interchanger 13,14
4Kcal/hr) with (190t/h, 75 ℃) heat exchange after, the temperature that the top is followed is 95 ℃, the temperature that the top is followed is 95 ℃, regulates to make to push up to follow with air cooling 11 again and continues to be cooled to 80 ℃, the top of returning the 1st plate 1-1 is followed and is returned tower opening for feed 2.
250 ℃, the stage casing of 13t/h reflux to follow from the top of the 20th column plate 1-20 with stage casing recycle pump 30 and extract mouthful 4 extractions out, and (total heat duties is 622 * 10 through two placed in-line interchanger 17,18
4Kcal/hr) with the deaerated water heat exchange of coming out from overhead heat exchanger 13,14 after, after temperature drops to 170 ℃, the stage casing continue with air cooling 12 adjustings make reach 170 ℃ after, return the stage casing of the 16th column plate 1-16 and return opening for feed 5.
(thermal load is 459 * 10 to the slurry oil (340 ℃, 138.361t/h) that comes out with column bottoms pump 31 discharge port 34 at the bottom of the tower through vapour generator 28
4Kcal/hr) steam cooling to 275 that 1.0MPa takes place ℃ returns tower.
Embodiment one
As shown in Figure 4, a kind of auxiliary fractional tower of the present invention comprises tower body 1, in the described tower body 1 from top to bottom horizontal direction 16 blocks of column plates are installed, whole tower body 1 inside is divided into 17 layers, the 17th layer is washing section, this section vertical direction is equipped with chevron shaped baffle plate 12, the bottom tower body of chevron shaped baffle plate 12 is respectively arranged with reaction oil gas opening for feed 9, stir steam feed mouth 10, the top tower body of chevron shaped baffle plate 12 is provided with slurry oil opening for feed 11 (external main fractionating tower), tower body 1 bottom is provided with slurry oil discharge port 34, be connected with main fractionating tower by slurry oil extractor pump 31 and slurry heat-exchanger 48, the tower tray of the 16th column plate 1-16 is provided with the stage casing and diesel oil is extracted mouth 4 out, the 13rd column plate 1-13 is provided with the stage casing and returns opening for feed 5, stage casing and diesel oil are extracted mouth 4 out by stage casing recycle pump 30, three placed in-line stage casing interchanger 15,17,18 return opening for feed 5 with the stage casing is connected, stage casing recycle pump 30, pass through the recycle stock return port of the external main fractionating tower of stage casing diesel oil extractor pump between the stage casing interchanger 17, the tower tray of the 4th column plate 1-4 is provided with the top and follows extraction mouth 3, the 1st column plate 1-1 is respectively arranged with trim the top of column opening for feed 8, the top is followed and is returned tower opening for feed 2, the top is followed and is extracted mouthfuls 3 out and follow extractor pump 29 by the top, four placed in-line overhead heat exchangers 16,12,13,14 follow with the top and to return tower opening for feed 2 and be connected, tower body 1 top is provided with oil gas vent 35, oil gas vent is by two strings two, four interchanger 19 also, 20,21, the interchanger 23 of 22 and three parallel connections, 24,25 are connected with branch flow container 27, divide flow container 27 bottoms to be respectively arranged with water port 38, the upgrading raw gasline is extracted mouth 39 out, the top is provided with rich gas discharge port 37, the upgrading raw gasline is extracted mouth 39 out, rich gas discharge port 37 is external absorbing-stabilizing system respectively, divides flow container 27 also to be connected with trim the top of column opening for feed 8 by pump 33.
As shown in Figure 5, the heat preheating raw gasline of the new auxiliary fractional tower of present embodiment utilization is realized the heat exchanger network of full vapour phase charging.
The first step is from the pyroreaction oil gas (79.796t/h of assisted reaction system, 430 ℃, 0.215MPaA) enter the bottom of auxiliary fractional tower, promptly the reaction oil gas opening for feed 9 of chevron shaped baffle plate 12 belows of the 17th layer of washing section enters in the tower, 0.5t/h the superheated vapour of 1.0MPa equally also enter in the tower from the stirring steam feed mouth 10 of the below of the chevron shaped baffle plate 12 of the 17th layer of washing section, from the next 50t/h of main fractionating tower, 275 ℃ slurry oil enters in the tower from the slurry oil opening for feed 11 of the top of the herringbone baffle plate 12 of the 17th layer of washing section, the catalyst dust that process washing reaction oil gas is carried secretly, after the heat exchange of pyritous reaction oil gas, behind slurry oil extractor pump 31 and slurry heat-exchanger 48, at the bottom of tower, extract out.Operating parameters: 430 ℃ of feeding temperatures, feed pressure 0.215MPa.
The cat head oil gas of second step, 130 ℃ of coming out from cat head discharge port 35,0.185MPaA, 74.3t/h, be divided into two-way, one road flow is 49.54t/h, and another road is 24.77t/h, and (total heat duties is 511.4 * 10 to the cat head oil gas of 49.54t/h by two placed in-line interchanger 19,20
4Kcal/hr) with 40 ℃, the condensed water heat exchange of 140t/h after, the temperature of cat head oil gas is reduced to 57.3 ℃, condensed water and is raised to 76.6 ℃ from 40 ℃; 24.77t/h cat head oil gas (total heat duties is 242.6 * 10 through two placed in-line interchanger 21,22
4Kcal/hr) with divide 40 ℃ of flow container, the liquid phase raw gasline heat exchange of 75t/h from the FCC main fractionating tower cat head after, temperature is reduced to 66.9 ℃, the temperature of raw gasline is upgraded to 98 ℃.Cat head oil gas continues interchanger 23,24,25 through three parallel connections, and (total heat duties is 194.3 * 10
4Kcal/hr) continue to make cat head oil gas to drop to 40 ℃ with 28 ℃, the recirculated water of 350t/h, enter the branch flow container, the temperature of recirculated water is upgraded to 33.5 ℃.40 ℃ upgrading raw gasline is then extracted out by pump 33 from the bottom of minute flow container, a part is advanced trim the top of column opening for feed 8 as the cat head cold reflux, another part is extracted out and directly to be removed absorbing-stabilizing system, and 40 ℃ rich gas has gone out mouthfuls 37 and extracted out and also directly remove absorbing-stabilizing system from the top of minute flow container.Operating parameters: the temperature of advancing minute flow container is 40 ℃.
The 3rd step 135.1t/h, 152.5 ℃ top are followed to follow from the top of the 4th column plate 1-4 with top recycle pump 29 and are extracted mouthful 3 extractions out, and (total heat duties is 201.2 * 10 through two placed in-line interchanger 13,14
4Kcal/hr) with through with the heat exchange of cat head oil gas after 98 ℃ raw gasline heat exchange after, the temperature followed of top is 128.2 ℃, the temperature of raw gasline is 142 ℃, (total heat duties is 297.7 * 10 to use two placed in-line interchanger 11,12 again
4Kcal/hr) continue to follow and the condensed water heat exchange of coming out from interchanger 20,19, make the top follow and continue to be cooled to 90.2 ℃, the top of returning the 1st plate 1-1 is followed and is returned tower opening for feed 2.Operating parameters: control top is followed returns 90 ℃ of temperature, to guarantee the thermal equilibrium of whole tower.
Reflux and one reinstate stage casing recycle pump 30 and extract mouthfuls 4 out from the stage casing of herringbone shelves column plate 12 tops and diesel oil and extract out in the stage casing of the 4th 239.6 ℃ of steps, 4.125t/h diesel oil and 239.6 ℃, 214.7t/h, diesel oil directly removes main fractionating tower recycle stock return port, and (total heat duties is 643.9 * 10 through two placed in-line interchanger 17,18 and reflux in the stage casing
4Kcal/hr) with the raw gasline heat exchange of coming out from overhead heat exchanger 13,14 after, after temperature dropped to 190.5 ℃, raw gasline was 206 ℃, 8.713kgf/cm
2, vaporization rate α is 0.7614.Continue through interchanger 15 and the condensed water heat exchange of coming out from overhead heat exchanger 12,11 in the stage casing, make the temperature in stage casing reach 180 ℃ after, return the stage casing of the 13rd column plate 1-13 and return opening for feed 5.Operating parameters: the control stage casing return 180 ℃ of temperature, to guarantee the thermal equilibrium of whole tower.
The 5th goes on foot the raw gasline continuation of coming out from interchanger 17,18, and (thermal load is 175 * 10 through slurry heat-exchanger 48
4Kcal/hr) with behind 328.3 ℃ that extract out with slurry oil extractor pump 31 discharge port 34 at the bottom of the tower, the heat exchange of 51.87t/h slurry oil, the raw gasline after the heat exchange is 223.3 ℃, and vaporization rate α is 1, pressure is 6.831kgf/cm
2, the temperature of slurry oil is 275 ℃, returns main fractionating tower.Raw gasline realizes that complete vapour phase enters the service hoisting pipe reactor.Operating parameters: through with the slurry oil heat exchange after the final vaporization rate α of raw gasline be 1.
In the design of heat exchange process, in order to conform to practical situation, the present invention has supposed all that between per two groups of raw gasline interchanger the pressure drop of raw gasline pipe fitting and pipeline is 0.3kgf/cm
2Raw gasline in whole heat-processed coabsorption from the heat 1271 * 10 of auxiliary fractionating system
4Kcal/h.
The total heat-obtaining amount of the full tower of new auxiliary fractional tower is 2395 * 10
4Kcal/h.Wherein, reflux and slurry oil backflow heat-obtaining 950 * 10 in the stage casing
4Kcal/h accounts for 39.6% of full tower heat-obtaining.Heat-obtaining 500 * 10 follows on the top
4Kcal/h, it is extracted 153 ℃ of temperature out, returns 90 ℃ of temperature, and potential temperature is higher, is beneficial to energy recovery.Auxiliary fractional tower heat distribution under the new fractionation scheme condition sees Table 1.
Table 1
| Material | Flow (t/h) | The extraction temperature (℃) | Pressure (MPaA) | Return temperature (℃) | Thermal load (10 4kcal/h) |
| The stage casing slurry oil is followed on the cat head top | 74.306 135.4 210.4 51.868 | 130 152.8 240.9 329 | 0.185 | 40 90 180 275 | 945 500 775 175 |
| Add up to | 2395 | ||||
Present embodiment has proposed new auxiliary fractional tower flow process, and has designed the heat exchange new technological process with the auxiliary fractional tower heat preheating raw gasline of optimizing, and this flow process can be preheated to 223 ℃ from 40 ℃ with raw gasline.Energy-saving effect is as follows:
1, improves the temperature that raw gasline advances riser reactor, realized reaction-regeneration system fecund steam.
Present embodiment adds up to the heat 1271 * 10 that utilizes the reformulated gasoline separation system by the heating raw gasline
4Kcal/h has been preheating to 223 ℃ with raw gasline from 40 ℃, has realized that the complete vapour phase state of raw gasline enters the service hoisting pipe reactor.Because the raw gasline feeding temperature improves, and has brought heat into more, keeping under the temperature-resistant condition of assisted reaction system response, the service hoisting guard system needs the then corresponding minimizing of the heat of regenerated catalyst, and reduction is equivalent to raw gasline and brings heat 1271 * 10 into
4Kcal/h.Can utilize in the reaction-regeneration system equipment such as the external warmer about 24t/h of middle pressure steam that mostly occurs.
2, improve the raw gasline temperature, reduce the coke and the dry gas yied 0.5% of system.
3, improve the utilising efficiency of auxiliary fractional tower energy, reduced plant energy consumption.
The new auxiliary fractional tower flow process that the present invention proposes, and designed heat exchange new technological process with the auxiliary fractional tower heat preheating raw gasline of optimizing, the energy that has improved the reformulated gasoline separation system utilizes level.Compare the auxiliary fractionating system heat 2000 * 10 of existing technology net heat utilization
4Kcal/h, the heat of net heat utilization of the present invention are 2395 * 10
4Kcal/h utilizes 395 * 10 more
4Kcal/h.By subsystem raw gasline freshening amount 75t/h, subsystem 5.23 units capable of reducing energy consumption.Raw gasline atomizing steam amount is 1% in the existing technology, will save low pressure atomizing steam amount 750Kg/h, 0.76 unit of corresponding saving subsystem energy consumption after adopting full vapour phase charging.Add up to two measures, add up to descend 6 units of subsystem energy consumption.
The productive rate of subsystem coke has descended 0.5 percentage point.Calculate by reducing coke yield 0.25%, the coke reduction is 187.5kg/h; In catalytic coke energy consumption standard 0.95KgEO/Kg, saving standard fuel oil is 178kg/h; Consider that simultaneously the rate of recovery of coke chemical energy is 50% under the existing processing condition, actual saving standard fuel oil is 89kg/h, and the minimizing of coke can make subsystem energy consumption decline 1.2kgEO/ ton raw material.Add up to the subsystem energy consumption 7.2KgEO/ ton raw material that can descend.
Press 1,500,000 tons of/year (178.6t/h) catalytic cracking unit of amount of finish and calculate whole catalytic cracking system 3 units capable of reducing energy consumption.
4, improved the energy quality of gasoline upgrading process.
Present embodiment utilizes 1271 * 10
4The heat of kcal/h is heated to 223 ℃ with raw gasline from 40 ℃, be actually the high-quality heat that the more inferior heat of the auxiliary fractionating system of equivalent has been converted to reaction-regeneration system equivalent, so middle pressure steam of the 24t/h that can mostly occur, the steam grade changes 3.5MPa into from 1.0MPa steam, has realized that the energy upgrading of whole catalytic cracking unit utilizes.
Embodiment two
The feeding temperature of the pyroreaction oil gas in the first step is 400 ℃, and feed pressure is 0.20MPa; After dropping to 30 ℃, reaction oil gas temperature in second step enters the separatory jar, 30 ℃ upgrading raw gasline is extracted a part out from the bottom of minute flow container and is directly removed absorbing-stabilizing system, 30 ℃ rich gas is extracted out from the top of minute flow container and is also directly removed absorbing-stabilizing system, and the oil gas output pressure at tower body top is 0.16MPa; The temperature of returning that the control top is followed in the 3rd step is 80 ℃, to guarantee the thermal equilibrium of whole tower; The tower temperature of returning that in the 4th step reflux in the control stage casing is 170 ℃, to guarantee the thermal equilibrium of whole tower; All the other conditions are with embodiment one.
Embodiment three
The feeding temperature of the pyroreaction oil gas in the first step is 450 ℃, and feed pressure is 0.23MPa; After dropping to 35 ℃, reaction oil gas temperature in second step enters the separatory jar, 35 ℃ upgrading raw gasline is extracted a part out from the bottom of minute flow container and is directly removed absorbing-stabilizing system, 35 ℃ rich gas is extracted out from the top of minute flow container and is also directly removed absorbing-stabilizing system, and the oil gas output pressure at tower body top is 0.22MPa; The temperature of returning that the control top is followed in the 3rd step is 100 ℃, to guarantee the thermal equilibrium of whole tower; The 4th step tower temperature of returning of control stage casing backflow is 190 ℃, to guarantee the thermal equilibrium of whole tower; All the other conditions are with embodiment one.
As mentioned above, can realize the present invention preferably.
Claims (7)
1, a kind of auxiliary fractional tower, comprise tower body, in the described tower body from top to bottom horizontal direction column plate is installed, it is characterized in that, described column plate has 16, whole tower body inside is divided into 17 layers, described the 17th layer is washing section, this section vertical direction is equipped with chevron shaped baffle plate, the bottom tower body of described chevron shaped baffle plate is respectively arranged with the reaction oil gas opening for feed, stir the steam feed mouth, the top tower body of described chevron shaped baffle plate is provided with the slurry oil opening for feed, described tower body bottom is provided with the slurry oil discharge port, the tower tray of described the 16th block of column plate is provided with the stage casing and diesel oil is extracted mouth out, described the 13rd block of column plate is provided with the stage casing and returns opening for feed, described stage casing and diesel oil are extracted mouth out by the stage casing recycle pump, the stage casing interchanger returns opening for feed with the stage casing and is connected, the tower tray of described the 4th block of column plate is provided with the top and follows the extraction mouth, described the 1st block of column plate is respectively arranged with the trim the top of column opening for feed, the top is followed and is returned the tower opening for feed, described top is followed the extraction mouth and is followed extractor pump by the top, overhead heat exchanger and top are followed and are returned the tower opening for feed and be connected, described tower body top is provided with oil gas vent, described oil gas vent is connected with the branch flow container by interchanger, described separatory pot bottom is respectively arranged with water port, raw gasline is extracted mouth out, and the top is provided with the rich gas discharge port.
2, a kind of auxiliary fractional tower according to claim 1 is characterized in that, the external main fractionating tower of slurry oil opening for feed that the top tower body of described chevron shaped baffle plate is provided with.
3, a kind of auxiliary fractional tower according to claim 1 is characterized in that, the slurry oil discharge port of described tower body bottom is connected with main fractionating tower by slurry oil extractor pump and slurry heat-exchanger.
4, a kind of auxiliary fractional tower according to claim 1 is characterized in that, passes through the recycle stock return port of the external main fractionating tower of stage casing diesel oil extractor pump between described stage casing recycle pump, the stage casing interchanger.
5, a kind of auxiliary fractional tower according to claim 1 is characterized in that, described raw gasline is extracted mouth, rich gas discharge port external absorbing-stabilizing system respectively out.
6, a kind of auxiliary fractional tower according to claim 1 is characterized in that, flow container also was connected with the trim the top of column opening for feed by pump in described minute.
7, the gasoline catalyzing and olefine reducing modification process that adopts the described a kind of auxiliary fractional tower of claim 1 to realize is characterized in that, comprises the steps and processing condition:
The first step enters the bottom of auxiliary fractional tower by the reaction oil gas opening for feed from the pyroreaction oil gas of assisted reaction system, promptly below the chevron shaped baffle plate of the 17th layer of washing section, 1.0MPa superheated vapour enter the bottom of auxiliary fractional tower by stirring the steam feed mouth equally, enter the top of the chevron shaped baffle plate of the 17th layer of washing section in the auxiliary fractional tower by the slurry oil opening for feed from the slurry oil of main fractionating tower, the catalyst dust that process washing reaction oil gas is carried secretly, after the heat exchange of pyroreaction oil gas, slurry oil discharge port at the bottom of tower is extracted out, the feeding temperature of described pyroreaction oil gas is 400～450 ℃, and feed pressure is 0.20～0.23MPa;
The second step pyroreaction oil gas is by the oil gas vent output at tower body top, be divided into two-way, respectively with raw gasline, after condensed water or the deaerated water heat exchange, utilize recirculated water, condensed water or de-mineralized water continue to make the reaction oil gas temperature to drop to 30～40 ℃, enter the branch flow container, 30～40 ℃ upgrading raw gasline is extracted out from the bottom of minute flow container, a part is directly removed absorbing-stabilizing system, another part directly returns the trim the top of column opening for feed of the 1st block of column plate of tower body as the cat head cold reflux, 30～40 ℃ rich gas is extracted out from the top of minute flow container and is also directly removed absorbing-stabilizing system, and the oil gas output pressure at tower body top is 0.16～0.22MPa;
The 3rd step top is followed with pump and is followed extraction mouthful extraction from the top of the 4th block of column plate, through with the heat exchange of cat head oil gas after the raw gasline heat exchange after, with condensed water or de-mineralized water the top is followed again and continued to be cooled to 80～100 ℃, the top of returning the 1st block of column plate is followed and is returned the tower opening for feed, the temperature of returning that the control top is followed is 80～100 ℃, to guarantee the thermal equilibrium of whole tower;
The 4th step diesel oil and stage casing backflow one are reinstated the stage casing recycle pump and are extracted a mouthful extraction out from the stage casing and the diesel oil of the 16th block of column plate, diesel oil directly removes main fractionating tower recycle stock return port by stage casing diesel oil extractor pump, and reflux in the stage casing and the raw gasline heat exchange after preheating is followed on the top is lowered the temperature, be aided with secondary condensed water or de-mineralized water return the tower temperature as the stage casing backflow regulating measure, after making temperature drop to 170～190 ℃, return the stage casing of the 13rd block of column plate and return opening for feed, the tower temperature of returning that refluxes in the control stage casing is 170～190 ℃, to guarantee the thermal equilibrium of whole tower;
The 5th step continued with the slurry oil heat exchange of coming out at the bottom of the tower with the raw gasline that stage casing backflow heat exchange is come out, to utilize the heat of the high potential temperature thermal source of system to greatest extent, fully improve preheating temperature, raw gasline is warmed up to more than the bubble point, realize that complete vapour phase enters subsidiary riser, the circulation slurry oil continues to be used for taking place the low-pressure steam of 1.0MPa, it is cooled to returns main fractionating tower when entering the identical temperature of auxiliary fractional tower, through with the slurry oil heat exchange after the vaporization rate α of raw gasline be 1.
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| CNB2006101240099A CN100519699C (en) | 2006-12-01 | 2006-12-01 | Auxiliary fractional tower and its gasoline catalyzing and olefine reducing modification process |
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101906318A (en) * | 2010-07-30 | 2010-12-08 | 华南理工大学 | Method and device for upgraded recycle of energy of raffinate tower and extract tower |
| CN101381617B (en) * | 2007-09-06 | 2012-09-05 | 中国石油化工股份有限公司 | Fractionation method of hydrocarbon mixtures |
| CN106118714A (en) * | 2016-07-22 | 2016-11-16 | 中石化炼化工程（集团）股份有限公司 | Crude(oil)unit |
| CN113476878A (en) * | 2021-07-09 | 2021-10-08 | 山东金诚重油化工技术研究院 | Method for combined removal of trace nitrogen |
-
2006
- 2006-12-01 CN CNB2006101240099A patent/CN100519699C/en not_active Expired - Fee Related
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101381617B (en) * | 2007-09-06 | 2012-09-05 | 中国石油化工股份有限公司 | Fractionation method of hydrocarbon mixtures |
| CN101906318A (en) * | 2010-07-30 | 2010-12-08 | 华南理工大学 | Method and device for upgraded recycle of energy of raffinate tower and extract tower |
| CN106118714A (en) * | 2016-07-22 | 2016-11-16 | 中石化炼化工程（集团）股份有限公司 | Crude(oil)unit |
| CN106118714B (en) * | 2016-07-22 | 2018-02-13 | 中石化炼化工程（集团）股份有限公司 | Crude(oil)unit |
| CN113476878A (en) * | 2021-07-09 | 2021-10-08 | 山东金诚重油化工技术研究院 | Method for combined removal of trace nitrogen |
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| CN100519699C (en) | 2009-07-29 |
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