CN1490383A - Catfoming process and apparatus for producing high-quality gasoline and increasing light products and propylene - Google Patents
Catfoming process and apparatus for producing high-quality gasoline and increasing light products and propylene Download PDFInfo
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- CN1490383A CN1490383A CNA031158730A CN03115873A CN1490383A CN 1490383 A CN1490383 A CN 1490383A CN A031158730 A CNA031158730 A CN A031158730A CN 03115873 A CN03115873 A CN 03115873A CN 1490383 A CN1490383 A CN 1490383A
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Abstract
A greatly improved catalytic transform process and apparatus for preparing high-quality gasoline and increasing the output of light products and propylene feature that a reactor with serial-parallel structure is provided to make the refined oil and raw oil in different lift tubes, and the relative reaction steps and reaction conditions are optimally designed for increasing the degrees of cracking reaction and catalytic transforming reaction. Its advantages are high output rate increased by 0-3 % for liquefied gas, gasoline and diesel oil, low content of olefine in gasoline, high content of propylene in liquefied gas, and low cost.
Description
Technical field
The invention provides a kind of at the catalytic cracking process of routine and the technology and the device that once improve significantly and optimize on the riser reactor.Particularly under the prerequisite that improves light product (gasoline, diesel oil and liquefied gas) productive rate, produce high-quality product and particularly reach the gasoline and the producing more propylene of new national standard and can improve heavy oil conversion performance and the catalytic conversion process method and the reactor of device working ability.
Background technology
Conventional catalytic cracking process process mainly comprises: 1. the fresh feed oil through heat exchange injects through feed nozzle in the bottom of riser tube, recycle stock on the top of stock oil, the bottom or and stock oil injecting lift pipe together, in riser tube, contact, and vaporize and react with high-temperature regenerated catalyst from revivifier.Various being reflected under the little reaction conditions of variation that oil gas took place carried out.Oil gas enters settling vessel in a short period of time, enters fractionating system after cyclone separator separates.2. isolated carbon deposited catalyst enters revivifier through stripping stage and regenerates.This process produces more coke, dry gas, recycle stock and externally extracting oil when processing heavy oil, simultaneously quality product is obviously relatively poor, wherein too high with content of olefin in gasoline especially, and production of diesel oil and quality are lowly for very.
CN1310223A discloses a kind of catalysis conversion method of producing low-alkene gasoline and high-yield diesel oil.This method is with the reactor subregion, the stock oil of preheating enters first reaction zone with recycle stock and contacts the cracking reaction of generation macromole with the catalyzer of heat, the oil gas that generates and used catalyst is up or with go upward to second reaction zone after lightweight material oil that injects and/or cold shock medium mix and carry out catalytic cracking reaction, reaction product, water and reclaimable catalyst are after gas solid separation, reaction product is separated into dry gas, liquefied gas, gasoline and diesel oil, reclaimable catalyst enters revivifier regeneration behind stripping, the regenerated catalyst Returning reactor of heat recycles.This invention also provides a kind of reaction unit of this method of application simultaneously, from a most preferred embodiment of this device as can be known, reactor is made of thinner pre lift zone of diameter and second reaction zone of first reaction zone and diameter overstriking, and wherein the height of second reaction zone of overstriking is much larger than the height of thin segment.This method has certain effect to falling alkene in theory, but this method requires different stock oil and recycle stock to treat with a certain discrimination for reaction conditions, can only under identical conditions, handle, thereby can not realize optimizing reaction conditions in actual applications, also limit the re-set target of falling alkene.Moreover, catalytic cracking second reaction zone increase the raising that has restricted heavy oil conversion performance on the contrary.In addition,, can only increase height of devices or other facilities, cause installation cost to increase if will reach the purpose of falling alkene.
Summary of the invention
Task of the present invention overcomes the prior art defective exactly, provides a kind of and can produce catalytic conversion process method that is rich in propylene liquefied gas, high-quality gasoline (long inductive phase, low olefin-content, low-sulfur nitrogen content), high light product yield and the device of realizing the low flexible operation of designs simplification cost of this technology.
This technological process realizes by following conversion zone: 1) prepare section in the reaction of the first riser tube bottom and inject quenching medium, this medium is contacted with the regenerated catalyst of heat, and the catalyzer that has had carbon deposit and temperature to decrease slightly enters the heavy oil cracking section with oil gas and lifting medium; 2) the fresh feed oil through heat exchange injects through feed nozzle in the heavy oil cracking section of this riser tube bottom, recycle stock and reprocessed oil slurry then inject the recycle stock cracking zone of second riser tube, reactant contacts with regenerated catalyst respectively in two riser tubes and carries out catalytic cracking reaction, and enters catalytic conversion stage respectively; 3) oil gas that enters catalytic conversion stage carries out dimolecular reaction, aromatization and isomerization reaction under certain condition and with the conversion reaction of sulphur nitrogen; Oil gas, catalyzer in two riser tubes converges or enters settling vessel respectively afterwards; 4) oil gas that enters settling vessel separates through cyclone separator with catalyzer, oil gas enters fractionating system, the catalyzer that contains charcoal enters revivifier regeneration behind stripping, regenerated catalyst enters two riser tubes through regenerator sloped tube and recycles, and reacts incomplete recycle stock and enters second riser tube and recycle.
The concrete operations step of this technology is: 1. the quenching medium reaction that enters first riser tube is prepared section and is contacted with regenerated catalyst, be 500 ℃～800 ℃ in temperature of reaction and be preferably 520 ℃～720 ℃, reaction times be preferably 0.05 second in 0.01 second～3.0 seconds～2.0 seconds, the weight ratio of catalyzer and stock oil is 5～100: 1 is preferably 8～80: 1, it is 0.01%～0.6% to be preferably under 0.05%～0.5% the condition mild cracking reaction takes place that section outlet catalyzer carbon content is prepared in reaction, and the temperature of appropriateness reduction regenerated catalyst, be generally 550 ℃～750 ℃ and be preferably 560 ℃～710 ℃.2. slightly contain the suitable catalyzer of charcoal and temperature and enter the heavy oil cracking section with oil gas, lifting medium, and contact with fresh feed oil, under following condition, carry out cracking reaction: temperature of reaction be 400 ℃～600 ℃ be preferably 450 ℃～580 ℃, reaction times be preferably 0.1 second in 0.01 second～30 seconds～weight ratio of 10 seconds, catalyzer and stock oil is 1～30: 1 is preferably 3～15: 1.The oil gas of 3. heavy oil cracking section enters and carry out conversion reaction after the catalytic conversion stage under following condition: temperature of reaction be 380 ℃～580 ℃ be preferably 430 ℃～560 ℃, reaction times be preferably 0.5 second in 0.1 second～50 seconds～weight ratio of 20 seconds, catalyzer and stock oil is 1～100: 1 is preferably 5～80: 1.4. recycle stock contacts with regenerated catalyst with the pre lift zone of reprocessed oil slurry in the second riser tube bottom, and cracking reaction takes place under following condition: temperature of reaction be 480 ℃～660 ℃ be preferably 490 ℃～580 ℃, reaction times be preferably 0.3 second in 0.01 second～50 seconds～weight ratio of 10 seconds, catalyzer and stock oil is 1～100: 1 is preferably 5～30: 1.5. catalytic conversion reaction takes place in the oil gas that enters catalytic conversion stage from the second riser tube recycle stock cracking zone under following condition: temperature of reaction be 380 ℃～600 ℃ be preferably 400 ℃～580 ℃, reaction times be preferably 0.3 second in 0.1 second～50 seconds～weight ratio of 20 seconds, catalyzer and stock oil is 1～100: 1 is preferably 5～80: 1.
This technology suit processing stock oil identical with conventional catalytic cracking, employed catalyzer is identical with conventional catalytic cracking.Described shock chilling medium can be prepared section in reaction and inject, and also can inject at soaking section and catalytic conversion stage.
Catalytic convention design of the present invention comprises catalytic conversion reactor, settling vessel and revivifier, wherein catalytic conversion reactor is a kind of series parallel structure of compound reducing, have first riser tube and second riser tube of two parallel connections, the upper/lower terminal of described first, second riser tube links with settling vessel and revivifier respectively.
The pipeline that the upper end of first riser tube and second riser tube can be respectively links to each other by vertical, inclination or level is connected with settling vessel, also can converge the back and be connected with settling vessel by the pipeline that vertical a, inclination or level link to each other.
The lower end of first riser tube and second riser tube can be respectively be connected with revivifier with the compound tube of standpipe by inclined tube or standpipe and inclined tube and be convenient to import regenerated catalyst, also can converge and be connected with revivifier with the compound tube of standpipe by an inclined tube or standpipe and inclined tube to be convenient to import regenerated catalyst.
Wherein first riser tube is prepared section, heavy oil cracking section, is radially constituted than the catalytic conversion stage of heavy oil cracking section expansion and the outlet section that is connected with settling vessel that radially dwindles than catalytic conversion stage by pre lift zone, reaction respectively from bottom to top.Wherein catalytic conversion stage accounts for 5%～50% of the first riser tube total height, it is 10%～100% that the intersegmental diameter ratio of section and heavy oil cracking section and radially enlarged catalyzed conversion is prepared in reaction, and section is prepared in described reaction and the heavy oil cracking section accounts for 10%～60% of the first riser tube total height.
Wherein second riser tube is strengthened the riser tube of reaction as recycle stock, constitutes by recycle stock pre lift zone, soaking section, catalytic conversion stage with the catalytic conversion stage of first riser tube outlet section that be connected or that be connected with settling vessel respectively from bottom to top.
The position that described second riser tube is connected with the first riser tube catalytic conversion stage can be in the lower end of catalytic conversion stage, also can be in the middle or the upper end.
Second riser tube can also be isodiametric riser tube in addition, also can radially dwindle or catalytic conversion stage radially exports the riser tube of the change diameter that radially equates with catalytic conversion stage than soaking section expansion for catalytic conversion stage radially enlarges export than catalytic conversion stage than soaking section.This riser tube upper end is connected with the catalytic conversion stage or the outlet section of first riser tube by an inclined tube or level pipe, perhaps the upper end by one vertically, inclined tube or level pipe be connected with settling vessel.
It is 10%～100% that the catalytic conversion stage of described second riser tube accounts for the intersegmental diameter ratio of the pre lift zone of 5%～50%, second riser tube of this riser tube total height and recycle stock cracking zone and radially enlarged recycle stock catalyzed conversion.
The pre lift zone of described second riser tube and recycle stock cracking zone account for 10%～60% of this riser tube total height.
Use the present invention, the purpose product in the products therefrom is liquefied gas, gasoline, the increase of diesel yield sum, generally increases by 0～3 percentage point; Propylene content increases more than 5 percentage points in institute's production fluid gasification, and content is generally 30%～60%; Liquefied gas yield maintains an equal level or improves, generally 5%～20%; Content of olefin in gasoline reduces by 15～35 volume percentage points, and content can drop to below the 20v%, generally below 35v%; Breakdown time increased more than 200 minutes, and the sulphur nitrogen content descends about 20%; Gasoline yield maintains an equal level or improves, generally 40%～60%; Diesel yield maintains an equal level or reduces, generally 18%～30%; Non-ideal product coke yield and dry gas yied maintain an equal level or reduce; The externally extracting oil productive rate reduces.
Thereby the present invention has following advantage:
1. than conventional catalytic cracking, light product (liquefied gas, gasoline, diesel oil) yield can improve 0～3 percentage point, can significantly improve the benefit of enterprise;
2. than conventional catalytic cracking, coke and dry gas yied can keep maintaining an equal level or reducing, thereby a. maintains an equal level the amount of finish of device or improves, and b. needn't improve transformation to main air blower ability, regenerative power, settling vessel and follow up device ability when transforming, and can reduce improvement expenses significantly;
3. gasoline quality improves, and mainly contain content of olefin in gasoline and can drop to below the 35v%, the breakdown time lengthening, the sulphur nitrogen content reduces.
4. liquid gas propylene content can improve more than 5 percentage points, can effectively increase the benefit.
5. the products scheme adjustment is flexible, can realize maximum liquefied gas (propylene) scheme, maximum liquefied gas (propylene) and gasoline scheme, maximum gasoline and diesel oil scheme, maximum liquefied gas (propylene) and diesel oil scheme, maximum diesel oil scheme.
6. when carrying out maximum liquefied gas (propylene) and diesel oil scheme or maximum diesel oil scheme, diesel yield and quality all can improve.
Description of drawings
Fig. 1 is according to catalytic convention design production premium of the present invention and increases production light product and the process principle figure of propylene;
Fig. 2 is an example structure synoptic diagram according to catalytic conversion reactor of the present invention.
Embodiment
The invention will be further described below in conjunction with drawings and Examples.
As shown in Figure 1, at first consult the first riser tube I: the pre lift zone k in this riser tube bottom injects regenerated catalyst, prepare section a in its reaction and inject quenching medium 1, this medium is contacted with the regenerated catalyst 2 of heat, and the catalyzer 2 that has had carbon deposit and temperature to decrease slightly enters heavy oil cracking section b with oil gas and lifting medium; Fresh feed oil 3 through heat exchange injects through feed nozzle in the heavy oil cracking section of riser tube bottom, contacts with regenerated catalyst and carries out catalytic cracking reaction, enters the catalytic conversion stage c of enlarged-diameter with quenching oil, lifting medium then; Enter that oil gas among the catalytic conversion stage c carries out dimolecular reaction, aromatization and isomerization reaction under certain condition and with the conversion reaction of sulphur nitrogen; The oil gas and the catalyzer of reaction gained enter settling vessel f through outlet section e; The oil gas that enters settling vessel f separates through cyclone separator with catalyzer, oil gas enters fractionating system, the catalyzer that contains charcoal enters revivifier g regeneration behind stripping, entering first riser tube through regenerator sloped tube h then recycles, react incomplete recycle stock and then enter the recycle stock riser tube, promptly the second riser tube II recycles.See also the second riser tube II below: the pre lift zone k ' in this riser tube bottom injects regenerated catalyst, 4 recycle stock cracking zone b ' that inject this riser tube II of recycle stock and reprocessed oil slurry strengthen reaction, recycle stock contacts with regenerated catalyst 2 and carries out the macromole cracking reaction in b ', and going upward to the top of the second riser tube II, squeeze into chill oil 5 and enter catalytic conversion stage c ' with oil gas this moment; The oil gas that enters catalytic conversion stage carries out dimolecular reaction, aromatization and isomerization reaction under certain condition and with the conversion reaction of sulphur nitrogen; Oil gas, catalyzer in the first riser tube I converges and enters settling vessel f afterwards; The oil gas that enters settling vessel separates through cyclone separator with catalyzer, oil gas enters fractionating system, the catalyzer that contains charcoal enters revivifier g regeneration behind stripping, gained regenerated catalyst 2 enters the second riser tube II through regenerator sloped tube h ' and recycles, and reacts incomplete recycle stock and also enters the second riser tube II and recycle.
As shown in Figure 2, catalyst cracker combines through series-parallel connection by the first riser tube I that handles stock oil with to the second riser tube II that recycle stock is strengthened reaction, the first riser tube I is respectively pre lift zone k from bottom to top, section a is prepared in reaction, heavy oil cracking section b, the catalytic conversion stage c of enlarged-diameter and the outlet section e that radially dwindles; The second riser tube II then is respectively pre lift zone k ' from bottom to top, recycle stock soaking section b ', the catalytic conversion stage c ' of enlarged-diameter and the communicating pipe d that links to each other with the catalytic conversion stage c top of the first riser tube I.
The specific embodiment of enumerating below will be further specified the present invention:
Present embodiment adopts processing method provided by the invention, is raw material with the grand celebration long residuum, uses conventional catalytic cracking catalyst, produces liquefied gas, gasoline, diesel oil on the small capacity double riser fluid catalytic cracking.Grand celebration long residuum through heating is atomized in riser reactor by high-temperature steam, contacts with high temperature catalyst, and temperature of reaction is 520 ℃, and reaction pressure is 0.18MPa, and agent-oil ratio is 8.Oil gas separates in settling vessel with catalyzer, and oil gas further is separated into product, and catalyzer is regenerated with air combustion behind stripping.And Comparative Examples 1 adopts conventional FCC tests device, and is raw materials used identical with embodiment 1 with catalyzer, produces gasoline, diesel oil, liquefied gas.
Product distribution, product property and test conditions see Table 1.From table 1 as seen, using light product of the present invention (liquefied gas, gasoline, diesel oil) yield compares with Comparative Examples and has improved 1.35 percentage points, olefin(e) centent is reduced to 21v% in the gasoline, compare with Comparative Examples and to have reduced by 33 percentage points, propylene content in the liquefied gas rises, compare with Comparative Examples, improved 8 percentage points.And with respect to the present invention, the light product yield is lower in the Comparative Examples of application ordinary method, and content of olefin in gasoline is very high, and productivity of propylene is lower.
Adopt FCC tests device of the present invention, installing concrete parameter is 2.6 meters of the first riser tube I height overalls, and 0.02 meter of reaction preparation section and heavy oil cracking section diameter highly are 0.6 meter, and the catalytic conversion stage diameter is 0.03 meter, highly is 0.5 meter; The height overall of the second riser tube II is 1.6 meters, and pre lift zone and soaking section diameter are 0.01 meter, highly is 0.9 meter, and passing on of catalysis section diameter is 0.016 meter, highly is 0.5 meter; The outlet section of second riser tube the catalytic conversion stage of first riser tube 3/4 highly the place be communicated with the latter by a level pipe.Present embodiment is raw material with the recycle stock, only enable under the situation of second riser tube, under the process optimized reaction conditions, produce gasoline, diesel oil, liquefied gas, products obtained therefrom distributes and sees Table 2, compares with Comparative Examples 2, and the light product productive rate improves 8.8 percentage points, coke yield descends 2.8 percentage points, and dry gas yied descends 3.1 percentage points.The recycle stock product distribution of Comparative Examples 2 is that the recycle stock charging of conventional catalytic cracking calculates.This shows, be very important for recycle stock provides new reaction environment.
Adopt device substantially the same manner as Example 2, just the exit end of second riser tube does not converge with first riser tube and directly is connected with settling vessel by a tipping tube, use technology of the present invention and different diesel oil scheme are made comparisons and analyze, reaction conditions and product distribution situation are referring to table 3.As can be seen from Table 3, under different production decision conditions, the olefin(e) centent of gasoline all can be controlled in below 35%, when the raising of middle part temperature of reaction, the top temperature of reaction helps obtaining better products distribution, the raising of temperature of reaction when bringing up to 482 ℃, make RON increase
Adopt the device identical, the variation of application products obtained therefrom quality of the present invention is analyzed with embodiment 2.The property analysis data of raw material and product see Table 4, and as can be seen from Table 4: the stable gasoline octane value is 89.9, near No. 90 gasoline standards; Breakdown time is long, and olefin(e) centent can be easy to be controlled at below 35%, and colloid is 0; Diesel cetane-number is lower.
Table 1 adopts the comparison of the present invention and conventional catalytic cracking
| Comparative Examples 1 | | |
| Catalyzer | ????DOCP-1 | ????DOCP-1 |
| The diesel oil model | ????-10 | ????-20 |
| The riser tube type | Conventional | The present invention |
| Operational condition | ||
| Temperature of reaction, ℃ | ????500 | ????490/505/680 |
| Agent-oil ratio | ????6 | ????8 |
| Reaction times, s | ????3 | ????8 |
| Stock oil character: | ||
| Density, kg/m3 | ????899.8 | ????911.3 |
| The residual oil carbon residue, % | ????4.33 | ????4.5 |
| Product distributes: m% | ||
| Dry gas | ????3.24 | ????3.25 |
| Liquefied gas | ????13.83 | ????16.4 |
| Gasoline | ????46.96 | ????47.79 |
| Solar oil | ????20.37 | ????18.32 |
| Slurry oil | ????5.06 | ????4.83 |
| Coke+loss | ????10.54 | ????9.41 |
| Lightweight oil | ????67.33 | ????66.11 |
| Light product | ????81.16 | ????82.51 |
| Gasoline property: sulphur content, % | ||
| ????＞0.01 | ????＜0.008 | |
| Inductive phase, min | ????＜370 | ????＞600 |
| Octane value | ????90.8 | ????90.2 |
| Gasoline is formed, v% | ||
| Stable hydrocarbon | ????36.6 | ????61.6 |
| Alkene | ????53.7 | ????21.6 |
| Aromatic hydrocarbons | ????9.70 | ????16.8 |
| Liquefied gas is formed: % | ||
| Propane | ????4.86 | ????14.33 |
| Propylene | ????30.26 | ????36.52 |
Table 2 recycle stock adopts the situation of different reaction conditionss
| Comparative Examples 2 | | |
| Recycle stock character | ||
| Density g/cm3 | 0.8919 | 0.8921 |
| Carbon residue % | 0.76 | 0.80 |
| ??Nippm | 0.71 | 0.79 |
| ??Hm％ | 11.7 | 11.9 |
| Temperature of reaction ℃ | 500 | 510 |
| Agent-oil ratio | 6 | 8 |
| Reaction times s | 3 | 2 |
| Product distribution % | ||
| Dry gas | 7.3 | 4.2 |
| Liquefied gas | 13.6 | 11.2 |
| Gasoline | 37.6 | 44.1 |
| Diesel oil | 22.3 | 27 |
| Externally extracting oil | 6.9 | 4 |
| Coke | 11.8 | 9 |
| Loss | 0.5 | 0.5 |
| Lightweight oil | 59.9 | 71.1 |
| Light product | 73.5 | 82.3 |
The change of table 3 production decision is to the influence of quality of gasoline and product distribution
| Production decision | -20# diesel oil | -10# diesel oil |
| Operational condition | ||
| Last chilling oil mass, t/h | ????3～4 | ????1～2 |
| Temperature in the reaction, ℃ | ????508±3 | ????512±2 |
| Temperature ℃ in the reaction | ????475±2 | ????481±2 |
| Following chilling oil mass, t/h | ????1～4 | ????0 |
| The regenerator activity | ????56～57 | ????56～58 |
| Regenerator is decided carbon, % | ????0.3 | ????0.3 |
| Product distributes, % | ||
| Dry gas | ????3.2 | ????3.37 |
| Liquefied gas | ????15.47 | ????15.67 |
| Gasoline | ????47.06 | ????49.05 |
| Diesel oil | ????17.95 | ????17.71 |
| Slurry oil | ????6.08 | ????4.75 |
| Coke | ????8.7 | ????8.31 |
| Loss | ????1.54 | ????1.13 |
| Light oil yield | ????65.02 | ????66.76 |
| The light product yield | ????80.49 | ????82.44 |
| Gasoline family forms, v% | ||
| Stable hydrocarbon | ????53 | ????57.9 |
| Alkene | ????33.3 | ????29.7 |
| Aromatic hydrocarbons | ????13.7 | ????12.4 |
| RON | ????89.6 | ????89.9 |
| Gasoline endpoint, ℃ | ????185 | |
| Condensation point of diesel oil, ℃ | ????-20 | ????-1?0 |
| Liquefied gas is formed, % | ||
| Propane | ????15.6 | ????12.97 |
| Propylene | ????35.5 | ????31.4 |
Table 4 raw material and product property
Claims (14)
1. produce premium and increase production light product and the catalytic conversion process of propylene for one kind, it is characterized in that this technological process comprises following conversion zone: 1) prepare section and inject quenching medium in the reaction of the first riser tube bottom, the regenerated catalyst of the heat that makes this medium and come through pre lift zone from revivifier contacts, and the oil gas of generation and catalyzer, lifting medium are advanced into the heavy oil cracking section of riser tube on together; 2) the fresh feed oil through heat exchange injects in the heavy oil cracking section of riser tube bottom, recycle stock and reprocessed oil slurry then inject the top of the second riser tube pre lift zone, reactant contacts with regenerated catalyst respectively in two riser tubes and carries out cracking reaction, and enters catalytic conversion stage respectively; 3) oil gas that enters catalytic conversion stage carries out dimolecular reaction, aromatization and isomerization reaction under certain condition and with the conversion reaction of sulphur nitrogen; Oil gas, catalyzer in two riser tubes converges or enters settling vessel respectively afterwards; 4) oil gas that enters settling vessel separates through cyclone separator with catalyzer, oil gas enters fractionating system, the catalyzer that contains charcoal enters revivifier regeneration behind stripping, regenerated catalyst enters two riser tubes through regenerator sloped tube and recycles, and reacts incomplete recycle stock and enters second riser tube that recycle stock is strengthened reaction and recycle.
2. production premium according to claim 1 is also increased production light product and the catalytic conversion process of propylene, it is characterized in that described shock chilling medium can inject in reaction preparation section, also can inject at soaking section or catalytic conversion stage.
3. production premium according to claim 1 is also increased production light product and the catalytic conversion process of propylene, the reaction conditions that section is prepared in described reaction is: the weight ratio 5～100 of 500 ℃～800 ℃ of temperature of reaction, 0.01 second～3.0 seconds reaction times, catalyzer and stock oil: 1, section outlet catalyzer carbon content 0.01%～0.6%, 550 ℃～750 ℃ of the temperature of regenerated catalyst are prepared in reaction; The reaction conditions of heavy oil cracking section is: the weight ratio 1～30: 1 of 400 ℃～600 ℃ of temperature, 0.01 second～30 seconds reaction times, catalyzer and stock oil; The reaction conditions of catalytic conversion stage is: the weight ratio 1～100: 1 of 380 ℃～580 ℃ of temperature of reaction, 0.1 second～50 seconds reaction times, catalyzer and stock oil; The cracking reaction condition of strengthening the conversion zone bottom is: 480 ℃～660 ℃ of temperature of reaction, 0.01 second～50 seconds reaction times, agent-oil ratio 1～100: 1; The catalytic conversion reaction condition of strengthening conversion zone top is: 380 ℃～600 ℃ of temperature of reaction, 0.1 second～50 seconds reaction times, agent-oil ratio 1～100: 1.
4. production premium according to claim 3 is also increased production light product and the catalytic conversion process of propylene, the reaction conditions that section is prepared in described reaction is: the weight ratio 8～80 of 520 ℃～720 ℃ of temperature of reaction, 0.05 second～2.0 seconds reaction times, catalyzer and stock oil: 1, section outlet catalyzer carbon content 0.05%～0.5%, 560 ℃～710 ℃ of the temperature of regenerated catalyst are prepared in reaction; The reaction conditions of heavy oil cracking section is: the weight ratio 3～15: 1 of 450 ℃～580 ℃ of temperature, 0.1 second～10 seconds reaction times, catalyzer and stock oil; The reaction conditions of catalytic conversion stage is: the weight ratio 5～80: 1 of 430 ℃～560 ℃ of temperature of reaction, 0.5 second～20 seconds reaction times, catalyzer and stock oil; The cracking reaction condition of strengthening the conversion zone bottom is: 490 ℃～580 ℃ of temperature of reaction, 0.3 second～10 seconds reaction times, agent-oil ratio 5～30: 1; The catalytic conversion reaction condition of strengthening conversion zone top is: 400 ℃～580 ℃ of temperature of reaction, 0.3 second～20 seconds reaction times, agent-oil ratio 5～80: 1.
5. produce premium and increase production light product and the catalytic convention design of propylene for one kind, this device comprises catalytic conversion reactor, settling vessel and revivifier, it is characterized in that described catalytic conversion reactor has first riser tube and second riser tube of two parallel connections, the upper/lower terminal of described first, second riser tube links with settling vessel and revivifier respectively.
6. production premium according to claim 5 is also increased production light product and the catalytic convention design of propylene, it is characterized in that the pipeline that the upper end of first riser tube and second riser tube can be respectively links to each other by vertical, inclination or level is connected with settling vessel, also can converge the back and be connected with settling vessel by the pipeline that vertical a, inclination or level link to each other.
7. production premium according to claim 5 is also increased production light product and the catalytic convention design of propylene, it is characterized in that the lower end of first riser tube and second riser tube can be respectively be connected with revivifier with the compound tube of standpipe by inclined tube or standpipe and inclined tube is convenient to import regenerated catalyst, also can converge and be connected with revivifier with the compound tube of standpipe by an inclined tube or standpipe and inclined tube to be convenient to import regenerated catalyst.
8. according to claim 5,6 or 7 described production premiums and increase production light product and the catalytic convention design of propylene, it is characterized in that described first riser tube prepared section, heavy oil cracking section, radially constituted than the catalytic conversion stage of heavy oil cracking section expansion and the outlet section that is connected with settling vessel that radially dwindles than catalytic conversion stage by pre lift zone, reaction respectively from bottom to top.
9. production premium according to claim 8 is also increased production light product and the catalytic convention design of propylene, it is characterized in that described catalytic conversion stage accounts for 5%～50% of the first riser tube total height, section is prepared in reaction and the heavy oil cracking section accounts for 10%～60% of the first riser tube total height, and the diameter ratio that reaction is prepared section and heavy oil cracking section and radially enlarged catalyzed conversion are intersegmental is 10%～100%.
10. according to claim 5,6 or 7 described production premiums and increase production light product and the catalytic convention design of propylene, it is characterized in that described second riser tube is made of recycle stock pre lift zone, recycle stock soaking section, catalytic conversion stage and the outlet section that is connected with the first riser tube catalytic conversion stage or settling vessel respectively from bottom to top.
11. production premium according to claim 10 is also increased production light product and the catalytic convention design of propylene, it is characterized in that position that described second riser tube is connected with the first riser tube catalytic conversion stage can be in the lower end of catalytic conversion stage, also can be in the middle or the upper end.
12. production premium according to claim 10 is also increased production light product and the catalytic convention design of propylene, it is characterized in that described second riser tube is the equal diameter riser tube.
13. production premium according to claim 10 is also increased production light product and the catalytic convention design of propylene, it is characterized in that described second riser tube is that catalytic conversion stage radially enlarges export than catalytic conversion stage than soaking section and radially dwindles or catalytic conversion stage radially exports the riser tube of the change diameter that radially equates with catalytic conversion stage than soaking section expansion.
14. production premium according to claim 10 is also increased production light product and the catalytic convention design of propylene, it is characterized in that the described second riser tube catalytic conversion stage accounts for 5%～50% of the second riser tube total height, pre lift zone and recycle stock cracking zone account for 10%～60% of the second riser tube total height, and these two sections is 10%～100% with the intersegmental diameter ratio of radially enlarged catalyzed conversion.
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Cited By (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2005085391A1 (en) * | 2004-03-08 | 2005-09-15 | China Petroleum & Chemical Corporation | A process of production of lower olefins and aromaticas |
| CN100393849C (en) * | 2005-08-08 | 2008-06-11 | 洛阳石化设备研究所 | Method and device of heavy oil two stage catalytic cracking reforming and gasoline upgrade coupling |
| CN100393848C (en) * | 2005-08-08 | 2008-06-11 | 洛阳石化设备研究所 | Catalytic cracking conversion method with relay use of catalyst curd its device |
| CN100465250C (en) * | 2004-03-08 | 2009-03-04 | 中国石油化工股份有限公司 | Production of low-carbon olefine and arene |
| CN1888021B (en) * | 2005-06-30 | 2010-04-28 | 洛阳石化设备研究所 | Hydrocarbon material catalytic cracking conversion process and reactor |
| CN102233253A (en) * | 2010-05-06 | 2011-11-09 | 中国石油天然气股份有限公司 | Riser catalysis device for processing heavy oil and application thereof |
| CN101531924B (en) * | 2008-03-13 | 2013-03-06 | 中国石油化工股份有限公司 | Method for preparing light fuel oil and propylene from poor-quality raw oil |
| CN113831937A (en) * | 2020-06-24 | 2021-12-24 | 中国石油天然气集团有限公司 | Method and device for increasing aromatic hydrocarbon content in propylene and gasoline |
| CN115305114A (en) * | 2021-05-07 | 2022-11-08 | 中国石油化工股份有限公司 | Double-riser or multi-riser settler |
| CN115305113A (en) * | 2021-05-07 | 2022-11-08 | 中国石油化工股份有限公司 | Double-riser settler |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| US9771529B2 (en) | 2004-03-08 | 2017-09-26 | China Petroleum & Chemical Corporation | Process for producing light olefins and aromatics |
| CN100465250C (en) * | 2004-03-08 | 2009-03-04 | 中国石油化工股份有限公司 | Production of low-carbon olefine and arene |
| US8778170B2 (en) | 2004-03-08 | 2014-07-15 | China Petroleum Chemical Corporation | Process for producing light olefins and aromatics |
| WO2005085391A1 (en) * | 2004-03-08 | 2005-09-15 | China Petroleum & Chemical Corporation | A process of production of lower olefins and aromaticas |
| CN1888021B (en) * | 2005-06-30 | 2010-04-28 | 洛阳石化设备研究所 | Hydrocarbon material catalytic cracking conversion process and reactor |
| CN100393849C (en) * | 2005-08-08 | 2008-06-11 | 洛阳石化设备研究所 | Method and device of heavy oil two stage catalytic cracking reforming and gasoline upgrade coupling |
| CN100393848C (en) * | 2005-08-08 | 2008-06-11 | 洛阳石化设备研究所 | Catalytic cracking conversion method with relay use of catalyst curd its device |
| CN101531924B (en) * | 2008-03-13 | 2013-03-06 | 中国石油化工股份有限公司 | Method for preparing light fuel oil and propylene from poor-quality raw oil |
| CN102233253A (en) * | 2010-05-06 | 2011-11-09 | 中国石油天然气股份有限公司 | Riser catalysis device for processing heavy oil and application thereof |
| CN102233253B (en) * | 2010-05-06 | 2013-11-06 | 中国石油天然气股份有限公司 | Riser catalysis device for processing heavy oil and application thereof |
| CN113831937A (en) * | 2020-06-24 | 2021-12-24 | 中国石油天然气集团有限公司 | Method and device for increasing aromatic hydrocarbon content in propylene and gasoline |
| CN115305114A (en) * | 2021-05-07 | 2022-11-08 | 中国石油化工股份有限公司 | Double-riser or multi-riser settler |
| CN115305113A (en) * | 2021-05-07 | 2022-11-08 | 中国石油化工股份有限公司 | Double-riser settler |
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